WO2024125562A1 - 熔渣粒化方法及装置 - Google Patents

熔渣粒化方法及装置 Download PDF

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Publication number
WO2024125562A1
WO2024125562A1 PCT/CN2023/138507 CN2023138507W WO2024125562A1 WO 2024125562 A1 WO2024125562 A1 WO 2024125562A1 CN 2023138507 W CN2023138507 W CN 2023138507W WO 2024125562 A1 WO2024125562 A1 WO 2024125562A1
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WIPO (PCT)
Prior art keywords
slag
water
gas
pipeline
steam
Prior art date
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Ceased
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PCT/CN2023/138507
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English (en)
French (fr)
Inventor
肖永力
李永谦
谢梦芹
张友平
王英杰
关运泽
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Baoshan Iron and Steel Co Ltd
Original Assignee
Baoshan Iron and Steel Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
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Priority claimed from CN202223349130.5U external-priority patent/CN219174524U/zh
Priority claimed from CN202211604457.4A external-priority patent/CN118186160A/zh
Priority claimed from CN202223349142.8U external-priority patent/CN219174522U/zh
Priority claimed from CN202223367914.0U external-priority patent/CN219174525U/zh
Priority claimed from CN202211604588.2A external-priority patent/CN118186163A/zh
Priority claimed from CN202211603925.6A external-priority patent/CN118186154A/zh
Priority claimed from CN202223349128.8U external-priority patent/CN219174523U/zh
Priority to KR1020257019558A priority Critical patent/KR20250108700A/ko
Priority to JP2025533692A priority patent/JP2026502346A/ja
Priority to EP23902756.8A priority patent/EP4613882A4/en
Application filed by Baoshan Iron and Steel Co Ltd filed Critical Baoshan Iron and Steel Co Ltd
Publication of WO2024125562A1 publication Critical patent/WO2024125562A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B3/00—General features in the manufacture of pig-iron
    • C21B3/04—Recovery of by-products, e.g. slag
    • C21B3/06—Treatment of liquid slag
    • C21B3/08—Cooling slag
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B5/00—Treatment of  metallurgical  slag ; Artificial stone from molten  metallurgical  slag 
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/04—Making slag of special composition
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B7/00—Blast furnaces
    • C21B7/002—Evacuating and treating of exhaust gases
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/005—Preliminary treatment of scrap
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/04—Working-up slag
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2400/00—Treatment of slags originating from iron or steel processes
    • C21B2400/02—Physical or chemical treatment of slags
    • C21B2400/022—Methods of cooling or quenching molten slag
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2400/00—Treatment of slags originating from iron or steel processes
    • C21B2400/02—Physical or chemical treatment of slags
    • C21B2400/022—Methods of cooling or quenching molten slag
    • C21B2400/024—Methods of cooling or quenching molten slag with the direct use of steam or liquid coolants, e.g. water
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2400/00—Treatment of slags originating from iron or steel processes
    • C21B2400/05—Apparatus features
    • C21B2400/062—Jet nozzles or pressurised fluids for cooling, fragmenting or atomising slag
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2400/00—Treatment of slags originating from iron or steel processes
    • C21B2400/08—Treatment of slags originating from iron or steel processes with energy recovery

Definitions

  • the present application relates to the technical field of steel smelting, and in particular to a slag granulation method and device.
  • Blast furnace slag is a molten waste slag discharged from the blast furnace when smelting pig iron. Its main components are CaO, SiO 2 , Al 2 O 3 , and MgO. Its output is huge and it is the largest by-product in the metallurgical industry. About 350 kg of blast furnace slag is produced for every ton of iron produced. The furnace temperature can reach 1450-1650°C. Each ton of slag contains (1260-1880) ⁇ 10 3 kJ of sensible heat, which is equivalent to the calorific value of 60kg of standard coal. There is great potential, economy and feasibility in the recovery of waste heat. Under this situation, the research on the recovery and utilization of waste heat from blast furnace slag has become the focus of attention of enterprises in recent years.
  • blast furnace slag mostly adopts the water quenching process.
  • the slag is washed into water slag by high-pressure water, and the high-grade sensible heat is transferred to the water slag and wastewater at about 80°C, which loses its recycling value.
  • 0.4-0.5 tons of water are consumed for each ton of blast furnace slag treated, and a large amount of waste steam rich in pollutants such as H2S and SO2 is discharged.
  • the subsequent resource utilization such as micronization
  • 15-20% of the water in the water slag needs to be dried, and each ton of blast furnace slag needs to consume about 1000m3 of 500°C hot air.
  • blast furnace slag Due to the low thermal conductivity of blast furnace slag and the fact that its viscosity increases sharply with decreasing temperature, the heat exchange of blast furnace slag is slow and waste heat recovery is difficult. Rapidly micronizing blast furnace slag, increasing the heat exchange area and improving the heat transfer efficiency can quickly and efficiently recover the sensible heat of blast furnace slag.
  • the rapid cooling of slag particles not only creates conditions for heat recovery, but also keeps the glass content and activity of the cooled slag particles to meet the requirements of slag micropowder raw materials, thus maintaining the smoothness of the existing slag resource recovery pathway.
  • centrifugal granulation mainly uses a rotating disc or a rotating cup as a granulator, and uses centrifugal force to disperse and break the slag into fine droplets for rapid cooling, so as to keep the glass content and activity of the slag particles after cooling to meet the requirements of slag micropowder raw materials.
  • the centrifugal granulation process is still in the laboratory exploration stage, and there are still problems such as slag crusting, uneven particle size of granulated slag, and easy generation of slag wool, which need further research and improvement.
  • Chinese patent application CN201010566938.1 is titled "Metallurgical slag dry granulation and heat recovery system", which proposes a metallurgical slag dry granulation and heat recovery system.
  • the liquid slag is dry granulated by centrifugal rotation and air flow pulse
  • the sensible heat in the slag is transferred to the hot air by the pulse air flow and fluidizing gas
  • the heat in the hot air is recovered by the waste heat boiler to form medium and low pressure steam for steam turbine power generation.
  • Chinese patent CN101736101B entitled “System and method for power generation based on waste heat recovery from semi-wet slag treatment”
  • Chinese patent CN102433401B entitled “System and method for power generation based on rapid cooling and dry granulation of molten slag and sensible heat recovery”
  • blast furnace slag is mainly carried out by water quenching process.
  • the simple wind crushing process is not very suitable, and the centrifugal granulation process is still under development.
  • the utilization of waste heat of blast furnace slag is limited to conversion into steam and power generation through hot air/nitrogen, which is inefficient.
  • the present invention provides a variety of slag granulation methods and devices, which can achieve safe granulation of blast furnace slag and optionally recover the heat generated during the granulation process and utilize it simultaneously or for subsequent utilization.
  • a first aspect of the present invention provides a slag granulation method, which comprises crushing slag to obtain slag particles, then cooling the slag particles, and collecting the granulated slag obtained thereby.
  • the above slag granulation method can be performed in the following manner.
  • the slag is jet granulated to obtain surface-solidified particles and steam, and then the surface-solidified particles are cooled in a cyclone field to obtain solid slag particles.
  • a jet refers to a high-speed aerosol fluid, which is a gas-water mixture, in which water is ejected together with compressed air to form a mixture of high-speed moving gas and water droplets with a particle size between 0.01 and 0.20 mm.
  • the lower limit of the speed of the gas-water mixture is 20 m/s, preferably 50 m/s, more preferably 70 m/s, and most preferably 90 m/s.
  • the upper limit of the water droplet speed is usually not limited. Considering the power consumption of the equipment, the upper limit of the water droplet speed can be 150 m/s, preferably 120 m/s.
  • the slag in the present invention refers to blast furnace slag, and its temperature after being discharged from the furnace is between 1300 and 1500° C.
  • the slag is firstly crushed and granulated by the jet, and after contacting with the jet (high-speed gas-water mixture), the heat is partially transferred to the water droplets, and the slag surface is solidified in the fine water droplets to form surface-solidified particles.
  • the temperature of the particles is between about 800 and 1000° C., so the core of the particles is still molten, and the high-speed water droplets absorb heat to form water vapor.
  • the particles with solidified surface enter the cyclone field and perform high-speed revolution and rotation under the action of the cyclone field.
  • the revolution speed of the particles in the cyclone field is 5-25rad/s
  • the revolution radius is 80-120mm
  • the rotation speed is 100-400rad/s.
  • the cyclone field is provided by a cyclone, which increases the movement path of the slag and enhances the heat exchange efficiency between the slag particles and the ambient atmosphere. Therefore, compared with other cooling methods in the prior art, the cooling effect is better.
  • a method for recovering and utilizing slag waste heat comprising the following steps:
  • the slag enters the guide hood and is impacted, crushed, and granulated into granular droplets with a particle size of less than 5 mm by the aerosol fluid sprayed from the granulator.
  • the granular droplets fly along the guide hood in a directional manner with the aerosol fluid.
  • the granular droplets exchange heat with the aerosol fluid to be cooled and solidified, generating granulated slag below 1000°C (the morphology of the slag particles depends on its temperature.
  • the granulated slag is only surface-solidified particles that have not been completely cooled into solid slag particles) and an airflow of 300-600°C, thereby achieving granulation and cooling and solidification of the slag;
  • the separated airflow flows through the cyclone and the overflow pipe, and the temperature is reduced to 150-300°C after heat exchange with the cooling water in the spiral heat exchange tube in the overflow pipe.
  • the waste heat recovery device After being discharged from the cyclone and the overflow pipe, it enters the waste heat recovery device, and contacts with the heat exchange pipe with cooling water in the waste heat recovery device to further recover the waste heat, forming tail gas with a temperature of 130-150°C.
  • the cooling water in the heat exchange pipe of the waste heat recovery device absorbs heat and vaporizes, and then obtains saturated water vapor with a pressure of 0.4-0.5 MPa through steam-water separation, and returns to the granulator as a fluid for granulating the slag;
  • the cooling water in the spiral heat exchange tube absorbs heat and vaporizes, and then generates saturated steam with a pressure of 1.2-1.6MPa and a temperature of 188-201°C through steam-water separation.
  • the saturated steam enters the superheated steam generator and obtains superheated steam with a pressure of 1.2-1.6MPa and a temperature of 250-350°C after supplementary heat.
  • the cooling water in the heat exchange pipe of the drum bed absorbs heat and vaporizes, and generates saturated steam with a pressure of 1.2-1.6MPa and a temperature of 188-201°C after steam-water separation.
  • the saturated steam enters the superheated steam generator and obtains superheated steam with a pressure of 1.2-1.6MPa and a temperature of 250-350°C after supplementary heat.
  • the pressure of the superheated steam is reduced to normal pressure, and the temperature is reduced to 150-250°C. Then, it enters the waste heat recovery device, and contacts with the heat exchange pipe with cooling water in the waste heat recovery device to further recover the waste heat, forming tail gas with a temperature of 130-150°C.
  • the cooling water in the heat exchange pipe of the waste heat recovery device absorbs heat and vaporizes, and then obtains saturated water vapor with a pressure of 0.4-0.5 MPa through steam-water separation, and returns to the granulator as a fluid for granulating the slag.
  • the exhaust gas is discharged after dust removal and desulfurization by an exhaust gas purification device.
  • the aerosol fluid is selected from one or more of compressed air with a pressure of 0.5-0.8 MPa, high-pressure water mist with a pressure of 0.4-0.5 MPa, low-pressure steam with a pressure of 0.4-0.8 MPa, and mixtures thereof.
  • the solidification rate of particles with a particle size of less than 2 mm is above 80%.
  • the saturated steam is supplemented with heat in the superheated steam generator using natural gas or mixed coal gas produced in the steelmaking process.
  • the granulated slag entering the slag bin is transported to a slag fine powder production line and directly ground into slag fine powder with a specific surface area of 420-440 m 2 /kg.
  • the specific surface area of the ultrafine powder is 450-750 m 2 /kg.
  • the slag waste heat recovery coupled utilization method of the present invention can also be implemented as follows.
  • the slag waste heat recovery coupled utilization method provided according to another embodiment of the present invention includes the following steps:
  • the slag enters the guide hood and is impacted, broken, and granulated into granular droplets with a particle size of less than 5 mm by the aerosol fluid sprayed from the granulator.
  • the granular droplets fly along the guide hood in a directional manner with the aerosol fluid.
  • the granular droplets exchange heat with the aerosol fluid to be cooled and solidified, generating granulated slag with surface solidification (about 1250°C) and airflow of about 100°C, thereby achieving granulation and cooling and solidification of the slag;
  • the airflow is heated to 200-600°C by the slag particles in the cyclone and then enters the waste heat boiler through the overflow pipe.
  • the cooling water in the heat exchange pipe of the waste heat recovery device absorbs heat and vaporizes, and then obtains saturated water vapor with a pressure of 0.4-0.5 MPa through steam-water separation, and returns to the granulator as a fluid for granulating the slag;
  • the cooling water in the waste heat boiler absorbs heat and vaporizes, and then generates saturated steam with a pressure of 1.2-1.6 MPa and a temperature of 188-201°C through steam-water separation.
  • the saturated steam enters the superheated steam generator and obtains superheated steam with a pressure of 1.2-1.6 MPa and a temperature of 250-350°C after supplementary heat.
  • the cooling water in the heat exchange pipe of the drum bed absorbs heat and vaporizes, and generates saturated steam with a pressure of 1.2-1.6MPa and a temperature of 188-201°C after steam-water separation.
  • the saturated steam enters the superheated steam generator and obtains superheated steam with a pressure of 1.2-1.6MPa and a temperature of 250-350°C after supplementary heat.
  • step 5 The granulated slag in the slag bin is transported to the air jet mill, and is impacted and ground into ultrafine powder by the superheated steam obtained in step 2) and step 3);
  • the superheated steam pressure drops to normal pressure, and the temperature drops to 150-250°C, and then enters the waste heat recovery device, and contacts with the heat exchange pipe with cooling water in the waste heat recovery device to further recover the waste heat, forming tail gas with a temperature of 130-150°C;
  • the cooling water in the heat exchange pipe of the waste heat recovery device absorbs heat and vaporizes, and then obtains saturated water vapor with a pressure of 0.4-0.5 MPa through steam-water separation, and returns to the granulator as a fluid for granulating the slag.
  • a blast furnace slag granulation method is provided with a blast furnace slag granulation device with a high-speed steam nozzle.
  • the water entering the pipeline is pressurized by a water pump and then enters the heat exchanger.
  • the heat source from the waste heat recovery pipeline increases the water temperature in the heat exchanger.
  • the water is in a high-temperature and high-pressure state that is higher than the atmospheric pressure and higher than the boiling point at normal pressure. After being sprayed out through the nozzle, the water is instantly vaporized at normal pressure to form a high-speed jet containing steam (for example, the spray speed is 90 to 110 m/s) to impact the slag flowing out of the slag flow trough.
  • the high-speed jet cools the slag and breaks it into small particles that fall into the bottom of the slag granulation body.
  • the mixed jet sprayed from the nozzle is completely converted into steam after impacting the slag and flows out from the top of the device as a waste heat resource for subsequent utilization.
  • the water entering the pipeline is pressurized by a water pump, and the pressure in the pipeline is raised to 0.1-1 MPa; the heat energy from the waste heat recovery pipeline raises the water temperature in the heat exchanger to 100-182°C.
  • Another embodiment of the present invention provides a gas-water mixed horizontal slag granulation process, which is characterized in that a high-speed airflow provided by an air nozzle array assembly composed of gas nozzles is used to crush the falling slag to obtain slag particles; at the same time, a row of gas-liquid dual-fluid nozzles are used to spray water mist on the slag particles to quickly cool the slag particles and apply an auxiliary driving force to the slag particles so that they fall more accurately into the rear slag particle collection section.
  • the speed of the high-speed airflow is 90-110 m/s.
  • a second aspect of the present invention provides a slag granulation device, comprising:
  • a granulation mechanism used for granulating the slag to obtain broken slag particles
  • the cooling mechanism is used for cooling the slag particles to obtain granulated slag.
  • the above-mentioned slag granulation device can be arranged in the following manner.
  • a device for implementing a method for coupled utilization of slag waste heat recovery comprising:
  • the flow guide cover is a cylindrical structure; preferably, its cross section is rectangular, and the aspect ratio is 2:1 to 5:1; more preferably, an online weighing device is installed at the inlet end of the flow guide cover;
  • a granulator the outlet of which is connected to the inlet of the guide cover;
  • the cyclone has a material inlet on its side wall and a material outlet at its bottom; the material inlet is connected to the outlet end of the guide cover.
  • the overflow pipe the lower part of which is vertically inserted into the cyclone, and a spiral heat exchange tube is arranged in the overflow pipe;
  • the first steam-water separator is provided with a cooling water inlet, a cooling water outlet, a steam inlet and a steam outlet; the cooling water inlet is connected to the cooling water pipeline, the cooling water outlet is connected to the inlet end of the spiral heat exchange tube in the overflow pipe through a pipeline and a water pump, and the steam inlet is connected to the outlet end of the spiral heat exchange tube in the overflow pipe.
  • a waste heat recovery device wherein an air inlet and an air outlet are arranged on the shell, a heat exchange pipe is arranged inside, and the air inlet is connected to the outlet end of the overflow pipe;
  • a second steam-water separator on which a cooling water inlet, a cooling water outlet, a steam inlet and a steam outlet are arranged;
  • the cooling water inlet is connected to a cooling water pipeline, the cooling water outlet is connected to the inlet end of the heat exchange pipe in the waste heat recovery device through a pipeline and a water pump, the steam inlet is connected to the outlet end of the heat exchange pipe of the waste heat recovery device through a pipeline, and the steam outlet is connected to the inlet end of the granulator through a pipeline;
  • the drum bed is a cylindrical structure with a heat exchange pipe inside.
  • the inlet end of the drum bed is connected to the material outlet of the cyclone, and the outlet end of the drum bed is connected to the slag bin.
  • the drum bed is provided with a driving device that can drive it to rotate;
  • the third steam-water separator is provided with a cooling water inlet, a cooling water outlet, a steam inlet and a steam outlet;
  • the cooling water inlet is connected to the cooling water pipeline, the cooling water outlet is connected to the inlet end of the heat exchange pipeline of the roller bed through a pipeline and a water pump, and the steam inlet is connected to the outlet end of the heat exchange pipeline of the roller bed;
  • a jet mill wherein a feed pipe, an air inlet pipe and an air outlet pipe are arranged on the shell, wherein the feed pipe of the jet mill is connected to the slag bin, and the air outlet pipe of the jet mill is connected to the air inlet of the waste heat recovery device;
  • the superheated steam generator has an air inlet pipe and an air outlet pipe on its shell.
  • the air inlet pipe of the superheated steam generator is connected to the steam outlet of the first steam-water separator and the steam outlet of the third steam-water separator, and the air outlet pipe of the superheated steam generator is connected to the air inlet pipe of the air flow mill.
  • a vibrator is provided on the slag bin.
  • a blast furnace slag granulation device with a high-speed steam nozzle comprising:
  • the slag granulation body is a box structure, one side of the upper part of which is provided with a slag flow channel for the slag to enter, and the top of the slag granulation body is provided with a steam outflow channel;
  • the steam spray mechanism comprises a first control valve, a water pump, a second control valve, a pressure gauge, a heat exchanger, a thermometer and a nozzle which are sequentially arranged along a pipeline; the inlet end of the pipeline is connected to a water source; the nozzle is arranged on a side wall of the slag granulation body on a side where a slag flow channel is arranged, and the axial direction of the nozzle forms an angle with the axial direction of the slag flow channel, and the outlet direction of the nozzle faces the slag flowing out of the slag flow channel;
  • the heat exchanger is provided with a waste heat recovery pipeline and a heat exchange fluid outflow pipeline; wherein, a valve is installed on the waste heat recovery pipeline.
  • the axial direction of the nozzle forms an angle of 30 to 60 degrees with the axial direction of the slag flow channel.
  • the water entering the pipeline is pressurized by a water pump, and then enters the heat exchanger.
  • the heat source from the waste heat resource recovery pipeline increases the water temperature in the heat exchanger.
  • the water is in a high-temperature and high-pressure state that is higher than the external atmospheric pressure and higher than the boiling point temperature under normal pressure.
  • the water is then sprayed out through the nozzle. After being sprayed out, the high-temperature and high-pressure water is instantly vaporized at normal pressure to form steam.
  • a high-speed jet containing steam is formed to impact the high-temperature molten liquid slag flowing out of the slag flow trough (for example, the injection speed is 90-110 m/s).
  • the high-speed jet cools the liquid slag and breaks it into small particles that fall into the bottom of the slag granulation body.
  • the mixed jet sprayed from the nozzle impacts the high-temperature slag to generate steam that flows out from the top of the device as a waste heat recovery resource.
  • the first control valve is an electro-hydraulic gate valve.
  • the water entering the pipeline is pressurized by a water pump, and the pressure in the pipeline reaches 0.1-1 MPa; the heat source from the waste heat resource recovery pipeline increases the water temperature in the heat exchanger, and the water temperature is 100-182°C.
  • a device for the above-mentioned gas-water mixing horizontal slag granulation process comprising:
  • the slag granulation body is a box structure with a slag flow inlet at the top;
  • High-speed air jet mechanism comprising:
  • the gas storage tank is provided with a pressure gauge, an air intake pipe and an air intake valve;
  • the air nozzle array assembly includes a plurality of air flow nozzles and corresponding branch pipes, wherein the branch pipes are connected to the gas delivery pipe; the air flow nozzles are arranged on an upper part of a side wall of the slag granulation body;
  • the spray mechanism comprises: a second control valve, a water pump, a third control valve, a pressure gauge, a flow meter and a plurality of gas-liquid dual-fluid nozzles which are sequentially arranged along a water pipeline; the inlet end of the water pipeline is connected to a water source; the gas-liquid dual-fluid nozzles are arranged at the inner upper part and the bottom of the slag granulation body, and the gas-liquid dual-fluid nozzles are connected to the gas pipeline and the water pipeline through connecting pipes.
  • the axial direction of the air nozzle array assembly forms an angle of 0 to 20 degrees with the horizontal direction.
  • the width of the air nozzle array assembly is greater than the width of the slag flow inlet.
  • the second control valve is an electro-hydraulic gate valve.
  • the slag granulation body is semi-enclosed, and a slag particle collecting section is provided at the rear thereof.
  • the air flow nozzle is a supersonic nozzle.
  • the high-speed air injection mechanism provides the main power for the slag crushing and granulation
  • the atomization mechanism provides the main heat exchange medium for the slag crushing and granulation
  • the slag granulation process is carried out in the slag granulation body.
  • the compressor pressurizes the gas and sends it into the gas tank, which provides gas with stable pressure to the air nozzle array assembly, and then injects a high-speed airflow (for example, a jet speed of 90 to 110 m/s) into the slag granulation body to crush the slag; at the same time, the water pump pressurizes the water in the water pipeline, and then sprays it out through the gas-liquid dual-fluid nozzle together with the airflow sprayed out of the gas pipeline. After spraying, the droplet particles impact the granulated slag particles, quickly cool the slag particles and cool them into stable small particles.
  • a high-speed airflow for example, a jet speed of 90 to 110 m/s
  • an apparatus for granulating blast furnace slag using a gas nozzle array comprising:
  • the slag granulation body is a box structure, with a slag inlet and a steam outlet channel on the top;
  • High-speed air jet mechanism comprising:
  • the nozzle array comprises a plurality of nozzles and corresponding branch pipes, each branch pipe is connected to the gas pipeline respectively; the nozzle is arranged on a side wall of the slag granulation body.
  • the above device further comprises:
  • the nozzle atomizing mechanism comprises a second control valve, a water pump, a third control valve, a pressure gauge, a flow meter and a plurality of atomizing nozzles which are sequentially arranged along a water delivery pipeline; the inlet end of the water delivery pipeline is connected to a water source; the atomizing nozzles are arranged at the inner bottom of the slag granulating body and are arranged in at least two rows, and the water mist is sprayed in a direction facing the slag flowing in from the slag inlet.
  • the above device further comprises a waste heat recovery system, which comprises:
  • a heat exchange box wherein the upper part of one side wall is provided with a feed port connected to the discharge port of the slag granulation body; the top of the heat exchange box is provided with a heat exchange air flow outlet; a plurality of perforated bed plates are provided in the heat exchange box along the height direction; the bottom of the heat exchange box is provided with a slag particle outlet;
  • a gas nozzle array is arranged at the inner bottom of the heat exchange box and below the perforated bed plate, and the gas nozzles in the gas nozzle array are arranged opposite to the perforated bed plate; or,
  • the waste heat recovery system adopts a cyclone separator.
  • the perforated bed plate is arranged in a Z-shape along the vertical direction in the heat exchange box.
  • the cyclone separator comprises a separator body, and a gas-solid medium inlet connected to a discharge port of the slag granulation body is provided on one side of the upper portion of the separator body; an air outlet is provided on the top of the separator body, and an ash hopper is provided on the bottom of the separator body.
  • the nozzles in the nozzle array are one or more selected from supersonic nozzles, atomizing nozzles or gas-liquid dual-fluid nozzles; preferably, the axial directions of the nozzles in the nozzle array are perpendicular to the side walls of the slag granulation body.
  • the nozzles in the nozzle array are arranged in multiple rows and columns, or in an arc shape; preferably, the nozzles in two adjacent rows are staggered in the vertical direction; more preferably, the number of nozzles gradually decreases or increases in the vertical direction.
  • the nozzles in the nozzle array are gas-liquid dual-fluid nozzles; accordingly, the device is also provided with a nozzle water supply mechanism, which includes a fourth control valve, a water pump, a fifth control valve, a pressure gauge, and a flow meter arranged in sequence along the water supply pipeline; the inlet end of the water supply pipeline is connected to a water source, and the outlet end is connected to the inlet end of the gas-liquid dual-fluid nozzle.
  • a nozzle water supply mechanism which includes a fourth control valve, a water pump, a fifth control valve, a pressure gauge, and a flow meter arranged in sequence along the water supply pipeline; the inlet end of the water supply pipeline is connected to a water source, and the outlet end is connected to the inlet end of the gas-liquid dual-fluid nozzle.
  • the compressor pressurizes the air and sends it into the air tank, which then sprays the air through a pipeline and a (supersonic) nozzle into the slag granulation body for granulation.
  • the liquid slag is granulated in the granulation body.
  • the high-speed airflow (for example, the injection speed is 90 to 110 m/s or more) sprayed from the supersonic nozzle impacts the liquid slag to break it, and quickly exchanges heat and cools the granulated slag particles to facilitate rapid slag formation.
  • the device in this embodiment adopts a supersonic nozzle array to further improve the slag treatment capacity, and the injection of droplets improves the heat exchange effect of slag particles and reduces the waste of water resources.
  • a device for gas mist slag granulation capable of cleaning slag comprising:
  • the slag granulation body is a box structure with a slag inlet at the top and a slag particle collection section at the tail;
  • a gas nozzle array is arranged on a side wall of the slag granulation body
  • An atomizing nozzle array is arranged at the inner bottom of the slag granulating body, and the atomizing nozzle array has an atomizing nozzle array arranged at the inner bottom of the slag granulating body, and the atomizing nozzle array array is ...
  • the slag cleaning nozzle is arranged at the inner bottom of the slag granulation body, and the outlet of the slag cleaning nozzle faces the inner bottom of the slag granulation body and the slag particle collecting section.
  • the axial direction of the gas nozzle array is perpendicular to the side wall of the slag granulation body.
  • baffles are respectively provided on both sides of the outlet of the gas nozzle array, and liquid/atomizing nozzles are respectively installed on the outer sides of the baffles.
  • the slag cleaning nozzle is one or more selected from a water atomizing nozzle, a steam atomizing nozzle, a high-speed air flow nozzle or a gas-liquid dual-fluid nozzle.
  • the above device is further provided with:
  • the high-speed air injection mechanism comprises a compressor, an air storage tank, an air pipeline connected to the air storage tank, and a gas nozzle array connected to one end of the air pipeline; a first control valve and a flow meter are sequentially arranged on the air pipeline at the outlet end of the air storage tank; a pressure gauge, an air intake pipeline and an air intake valve are arranged on the air storage tank; the nozzle array comprises a plurality of nozzles and corresponding branch pipelines, and the branch pipelines are connected to the air pipeline; the slag cleaning nozzle is connected to the air pipeline through a connecting pipeline and a valve;
  • the nozzle atomization mechanism comprises a second control valve, a water pump, a third control valve, a pressure gauge and a flow meter which are sequentially arranged along a water delivery pipeline; the inlet end of the water delivery pipeline is connected to a water source, and the outlet end thereof is connected to the atomization nozzle array.
  • the nozzles in the atomizing nozzle array are gas-liquid dual-fluid nozzles, and their inlet ends are respectively connected to the gas pipeline and the water pipeline.
  • At least two slag inlet ports are provided on the top of the slag granulation body.
  • the gas mist slag granulation device capable of cleaning fallen slag in this embodiment includes a slag granulation system and a slag particle collection system.
  • the slag granulation system is divided into two parts, one part is a gas nozzle array assembly, which sprays a high-speed airflow (for example, a spray speed of 90-110 m/s) for granulation, and the other part is an atomizing nozzle array, which sprays droplets for granulation in the slag granulation device.
  • the high-speed airflow sprayed by the gas nozzle array impacts the liquid slag to break it, and the high-density droplets sprayed by the atomizing nozzle array quickly heat exchange and cool the broken slag, so that it can be quickly slaged.
  • a slag cleaning nozzle is arranged at the bottom of the slag granulation body, which can cool down the slag particles falling to the bottom and blow them to the tail slag collection section to prevent the slag particles from sticking to the wall and falling into the slag collection section quickly.
  • the present invention adopts a gas nozzle array to further improve the slag processing capacity, and adopts an atomizing nozzle array to spray aerosol, which improves the heat exchange effect of slag particles and reduces the waste of water resources.
  • the bottom nozzle for sweeping the slag can prevent the slag particles from sticking to the wall and quickly fall into the collection section.
  • a device for rapidly cooling slag using an atomizing nozzle comprising:
  • the slag granulation body is a box structure with a slag flow inlet at the top;
  • a gas nozzle array is arranged on a side wall of the slag granulation body, wherein the axial directions of the gas nozzles in the gas nozzle array are perpendicular to the side wall of the slag granulation body;
  • a flow field optimization nozzle array is arranged at the inner upper part of the slag granulation body, near the slag flow inlet;
  • a slag cleaning nozzle array is arranged at the inner lower part or the bottom of the slag granulation body
  • An atomizing nozzle array is disposed in the slag granulation body and arranged radially around the slag flow on the inner wall of the slag granulation body.
  • the axial direction of the atomizing nozzles in the atomizing nozzle array is perpendicular to the axial direction of the gas nozzle.
  • a slag collecting section is provided at the tail of the slag granulation body.
  • the nozzles of the flow field optimization nozzle array are gas nozzles or gas-liquid dual-fluid nozzles.
  • the nozzles of the slag cleaning nozzle array are gas nozzles.
  • the nozzles of the atomizing nozzle array are water atomizing nozzles.
  • the device of this embodiment adopts a nozzle array to further improve the slag treatment capacity.
  • the spraying of droplets improves the heat exchange effect of slag particles, reduces the waste of water resources, and fully recovers the waste heat of slag.
  • a water mist granulation device for granulating blast furnace slag comprising:
  • the rack is a frame structure
  • a water nozzle array assembly comprising:
  • the main body is a box structure, which is arranged in the middle of the frame; a flow equalizing plate and a flow guide plate are arranged in sequence at intervals;
  • the rear end of the body is connected to a water source
  • An array of water nozzles is evenly distributed on the front end surface of the body
  • Gas-liquid dual-fluid nozzle assembly comprising:
  • Gas-liquid dual-fluid nozzles are arranged in parallel on both sides of the water nozzle array and fixed on the frame;
  • the gas pipeline and the water pipeline are fixed on the frame and connected with the gas-liquid dual-fluid nozzle.
  • the gas-liquid dual-fluid nozzles are arranged in parallel on both sides of the water nozzle array.
  • FIG1 is a schematic structural diagram of a slag granulation device according to an embodiment of the present invention.
  • FIG2 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG3 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG4 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG5 is a schematic structural diagram of a gas nozzle array assembly in another embodiment of the present invention.
  • FIG6 shows the flight trajectory of slag particles when the device in FIG4 uses different gas nozzle array assemblies at different inclination angles
  • FIG. 7 shows the flight trajectory of slag particles when the inclination angle of the gas nozzle array assembly used in the device of FIG. 4 is too large
  • FIG8 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG9 is a schematic diagram showing the arrangement of a nozzle array in a slag granulation device according to another embodiment of the present invention.
  • FIG10 is a schematic diagram showing the arrangement of a nozzle array in a slag granulation device according to another embodiment of the present invention.
  • FIG11 is a schematic diagram showing the arrangement of a nozzle array in a slag granulation device according to another embodiment of the present invention.
  • FIG12 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG13 is a top view showing a nozzle array in a slag granulation device according to another embodiment of the present invention.
  • FIG14 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG15 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG16 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG17 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG18 is a schematic diagram showing the arrangement of nozzles for cleaning slag in a slag granulation device according to another embodiment of the present invention.
  • FIG19 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG20 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG21 is a top view showing a gas nozzle array in a slag granulation device according to another embodiment of the present invention.
  • FIG22 is a schematic diagram showing the structure of nozzles in a gas nozzle array of a slag granulation device according to another embodiment of the present invention.
  • FIG23 is another schematic diagram showing the structure of a gas nozzle array in a slag granulation device according to another embodiment of the present invention.
  • FIG24 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG25 is a schematic diagram showing the arrangement of the atomizing nozzles in FIG24 ;
  • FIG26 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention.
  • FIG. 27 shows a side view of the slag granulation device in FIG. 26 .
  • the terms “upper”, “lower”, “inner”, “bottom”, etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, or are the orientations or positional relationships in which the inventive product is usually placed when used. They are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present invention.
  • the present invention provides a slag granulation method, which includes crushing slag to obtain slag particles, then cooling the slag particles, and collecting the granulated slag obtained thereby.
  • the present invention provides a slag granulation device, including: a granulation mechanism for granulating slag to obtain broken slag particles; and a cooling mechanism for cooling the slag particles to obtain granulated slag.
  • a method for coupled utilization of slag waste heat recovery wherein the slag is jet granulated to obtain surface-solidified particles and steam, and then the surface-solidified particles are cooled in a cyclone field to obtain solid slag particles.
  • the method provided by this embodiment can achieve rapid and safe granulation of blast furnace slag while also achieving multi-stage recovery and same-stage utilization of sensible heat of blast furnace slag, thereby greatly improving the recovery rate of waste heat from high-temperature slag.
  • the granulated slag is directly ground into ultrafine slag powder, thereby achieving high-value productization of blast furnace slag.
  • FIG. 1 shows a device for implementing the slag granulation method according to this embodiment.
  • this embodiment provides a device for the above-mentioned slag waste heat recovery coupled utilization method, comprising:
  • the deflector 16 is a cylindrical structure; preferably, its cross section is rectangular, and the aspect ratio is 2:1 to 5:1; more preferably, an online weighing device 14 is installed at the inlet end of the deflector 16;
  • the granulator 15 has an outlet end connected to an inlet end of the flow guide hood 16;
  • the cyclone 17 has a material inlet on its side wall and a material outlet on its bottom; the material inlet is connected to the outlet end of the guide cover 16.
  • the overflow pipe the lower part of which is vertically inserted into the cyclone 17, and a spiral heat exchange tube is arranged in the overflow pipe;
  • the first steam-water separator 127 is provided with a cooling water inlet, a cooling water outlet, a steam inlet and a steam outlet; the cooling water inlet is connected to the cooling water pipeline, the cooling water outlet is connected to the inlet end of the spiral heat exchange tube in the overflow pipe through a pipeline and a water pump 128, and the steam inlet is connected to the outlet end of the spiral heat exchange tube in the overflow pipe.
  • the waste heat recovery device 123 has an air inlet and an air outlet on its shell, and a heat exchange pipeline is arranged inside, and the air inlet is connected to the outlet end of the overflow pipe;
  • the second steam-water separator 125 is provided with a cooling water inlet, a cooling water outlet, a steam inlet and a steam outlet;
  • the cooling water inlet is connected to the cooling water pipeline, the cooling water outlet is connected to the inlet end of the heat exchange pipe of the waste heat recovery device 123 through a pipeline and a water pump 124, the steam inlet is connected to the outlet end of the heat exchange pipe of the waste heat recovery device 123 through a pipeline, and the steam outlet is connected to the inlet end of the granulator 17 through a pipeline;
  • the drum bed 18 is a cylindrical structure with a heat exchange pipe inside.
  • the inlet end of the drum bed 18 is connected to the material outlet of the cyclone 17, and the outlet end of the drum bed 18 is connected to the slag bin 112.
  • the drum bed is provided with a driving device that can drive it to rotate;
  • the third steam-water separator 19 is provided with a cooling water inlet, a cooling water outlet, a steam inlet and a steam outlet;
  • the cooling water inlet is connected to the cooling water pipeline, the cooling water outlet is connected to the inlet end of the heat exchange pipeline of the roller bed through the pipeline and the water pump 110, and the steam inlet is connected to the outlet end of the heat exchange pipeline of the roller bed;
  • the air flow mill 117 has a feed pipe, an air inlet pipe and an air outlet pipe on its shell.
  • the feed pipe of the air flow mill 117 is connected to the slag bin 112, and the air outlet pipe of the air flow mill 117 is connected to the air inlet 123 of the waste heat recovery device;
  • the superheated steam generator 126 has an air inlet pipe and an air outlet pipe on its shell.
  • the air inlet pipe of the superheated steam generator 126 is connected to the steam outlet of the first steam-water separator 127 and the steam outlet of the third steam-water separator 19, and the air outlet pipe of the superheated steam generator 126 is connected to the air inlet pipe of the air flow mill 117.
  • a vibrator 113 is provided on the slag bin 112 .
  • the above-mentioned slag waste heat recovery coupled utilization method can be performed as follows. Specifically, the slag waste heat recovery coupled utilization method includes the following steps:
  • a blast furnace with a volume of 1250m3 in a steel plant when tapping iron, slag with a temperature of about 1500°C enters the main slag groove 11 at an average slag discharge rate of about 2.5t/min (maximum slag discharge rate of 5t/min), and the slag in the main slag groove 11 is put into the slag discharge groove 13 by the slag taker 12, and then flows into the guide cover 16 through the online weighing device 14, wherein the cross section of the guide cover 16 is rectangular, 300mm long and 100mm wide; the slag entering the guide cover 16 is sprayed by the gas mist from the granulator 15.
  • the body is impacted, crushed, and granulated into particle droplets with a particle size of less than 5 mm.
  • the particle droplets fly along the guide cover 16 at a high speed with the aerosol fluid.
  • the particle droplets exchange heat with the aerosol fluid during the formation and flight process and are quickly cooled and solidified.
  • the cooling rate is more than 20°C/second, and granulated slag below 1000°C and above 800°C (at this time, only the surface solidified particles, and the core is molten) and an air flow of about 300°C (ambient temperature) are generated.
  • the solidification rate of particles with a particle size of less than 2 mm is about 80%, and the granulation and cooling solidification of the slag are realized;
  • the granulated slag and air flow out of the guide cover 16 and directly enter the cyclone 17, where the slag and air are separated under the combined action of centrifugal force and gravity.
  • the temperature of the separated granulated slag drops to 700-800°C and flows out from the bottom of the cyclone 17.
  • the separated airflow flows through the cyclone 17 and the overflow pipe, and the temperature is reduced to below 150°C after heat exchange with the cooling water in the spiral heat exchange pipe in the overflow pipe.
  • the cooling water in the heat exchange pipe of the waste heat recovery device 123 absorbs heat and vaporizes, and then passes through the second steam-water separator 125 to separate steam and water to obtain saturated water vapor with a pressure of about 0.5 MPa, which is returned to the granulator 15 as an aerosol fluid for granulating the above slag;
  • the cooling water in the spiral heat exchange tube absorbs heat and vaporizes, and then passes through the first steam-water separator 127 to separate steam and water to generate saturated steam with a pressure of 1.2-1.6 MPa and a temperature of 188-201°C.
  • the saturated steam enters the superheated steam generator 126, and after supplementary heating, superheated steam with a pressure of 1.2-1.6 MPa and a temperature of 250-350°C is obtained.
  • natural gas or mixed coal gas generated in the steel smelting process is used to supplement the heat of the saturated steam entering the superheated steam generator 126.
  • the granulated slag is slowly pushed by the pushing mechanism in the drum along with the rotation of the drum bed 18, and is discharged from the drum bed 18 after the temperature drops below 180°C, and is sequentially sent to the slag bin 112 for storage through the chute and bucket elevator 111; a vibrator 113 is installed on the slag bin 112 to vibrate the slag bin 112 to prevent the granulated slag from blocking the slag bin outlet, bridging, and arching in the slag bin;
  • the cooling water in the heat exchange pipe of the roller bed 8 absorbs heat and vaporizes. After the water and gas are separated in the third steam-water separator 19, saturated steam with a pressure of 1.2-1.6 MPa and a temperature of 188-201°C is generated.
  • the saturated steam enters the superheated steam generator 126 and is supplemented with heat by natural gas or mixed coal gas generated in the steel smelting process. After the supplementary heat, superheated steam with a pressure of 1.2-1.6 MPa and a temperature of 250-350°C is obtained.
  • the granulated slag in the slag bin 112 is transported to the air flow mill 117 through the slag discharge valve 114 and the conveying mechanism 116, and is impacted and ground into ultrafine powder by the superheated steam obtained in step 2) and step 3).
  • the ultrafine powder is collected by the powder collecting device 118 and directly sold as a high-quality product;
  • the superheated steam pressure drops to normal pressure, and the temperature drops to below 150°C, and then enters the waste heat recovery device 123, and contacts with the heat exchange pipe with cooling water in the waste heat recovery device 123 to further recover waste heat, forming tail gas with a temperature of about 130°C;
  • the cooling water in the heat exchange pipe of the waste heat recovery device 123 absorbs heat and vaporizes, and then passes through the second steam-water separator 125 to separate steam and water to obtain saturated water vapor with a pressure of about 0.4 MPa, which is returned to the granulator 15 as an aerosol fluid for granulating the slag.
  • the granulated slag in the slag bin 112 is transported to a slag fine powder production line by a truck 115 and directly ground into slag fine powder with a specific surface area of about 420 m 2 /kg.
  • the waste gas generated during the production process is sent to the tail gas purification device 120, and after dust removal and desulfurization treatment to meet the relevant emission standards, it is extracted by the fan 121 and discharged through the chimney 122.
  • the circulation pump 119 circulates the desulfurization and dust removal liquid into the tail gas purification device 120. When the concentration of the circulating liquid reaches a certain value (depending on the actual treatment scenario), part of it is discharged and fresh alkali liquid is added from the outside to maintain normal and efficient desulfurization and dust removal effects.
  • the method for coupled utilization of slag waste heat recovery using the device shown in FIG1 can be performed as follows.
  • the method for coupled utilization of slag waste heat recovery includes the following steps:
  • the particle droplets are formed into particle droplets with a particle size of less than 5 mm.
  • the particle droplets fly along the guide cover 16 at a high speed with the aerosol fluid.
  • the particle droplets exchange heat with the aerosol fluid during the formation and flight process and are rapidly cooled and solidified, generating granulated slag below 1000°C and above 750°C (at this time, only the surface of the particles is solidified, and the core is molten) and an air flow of about 300°C (ambient temperature).
  • the solidification rate of particles with a particle size of less than 2 mm is about 90%, thereby realizing the granulation and cooling and solidification of the slag;
  • the granulated slag and air flow out of the guide cover 16 and directly enter the cyclone 17, where the slag and air are separated under the combined action of centrifugal force and gravity.
  • the temperature of the separated granulated slag drops below 750°C and flows out from the bottom of the cyclone 17.
  • the separated airflow flows through the cyclone 17 and the overflow pipe, and the temperature is reduced to below 200°C after heat exchange with the cooling water in the spiral heat exchange pipe in the overflow pipe.
  • the cooling water in the heat exchange pipe of the waste heat recovery device 123 absorbs heat and vaporizes, and then passes through the second steam-water separator to separate steam and water to obtain saturated steam with a pressure of about 0.45 MPa, which is returned to the granulator 15 as an aerosol fluid for granulating the above-mentioned slag;
  • the cooling water in the spiral heat exchange tube absorbs heat and vaporizes, and then passes through the first steam-water separator to separate steam and water to generate saturated steam with a pressure of about 1.4 MPa and a temperature of about 190°C.
  • the saturated steam enters the superheated steam generator 126, and after supplementary heating, superheated steam with a pressure of about 1.4 MPa and a temperature of about 300°C is obtained.
  • natural gas or mixed coal gas generated in the steel smelting process is used to supplement the heat of the saturated steam entering the superheated steam generator 126.
  • the granulated slag is slowly pushed by the pushing mechanism in the drum along with the rotation of the drum bed 18, and is discharged from the drum bed 18 after the temperature drops below 180°C, and is sequentially sent to the slag bin 112 for storage through the chute and bucket elevator 111; a vibrator 113 is installed on the slag bin 112 to vibrate the slag bin 112 to prevent the granulated slag from blocking the slag bin outlet, bridging, and arching in the slag bin 112;
  • the cooling water in the heat exchange pipe of the roller bed 18 absorbs heat and vaporizes.
  • the cooling water is forced to circulate by a booster pump, and after the steam and water are separated in the third steam-water separator 19, saturated steam with a pressure of about 1.4 MPa and a temperature of about 190°C is generated.
  • the saturated steam enters the superheated steam generator 126 and is supplemented with heat by natural gas or mixed coal gas generated in the steel smelting process. After the supplementary heat, superheated steam with a pressure of about 1.4 MPa and a temperature of about 300°C is obtained.
  • the granulated slag in the slag bin 112 is transported to the air flow mill 117 through the slag discharge valve 114 and the conveying mechanism 116, and is impacted and ground into ultrafine powder by the superheated steam obtained in step 2) and step 3).
  • the ultrafine powder is collected by the powder collecting device 118 and directly sold as a high-quality product;
  • the superheated steam pressure drops to normal pressure, and the temperature drops to below 200°C, and then enters the waste heat recovery device 123, and contacts with the heat exchange pipe with cooling water in the waste heat recovery device 123 to further recover waste heat, forming tail gas with a temperature of about 140°C;
  • the cooling water in the heat exchange pipe of the waste heat recovery device 123 absorbs heat and vaporizes, and then passes through the second steam-water separator to obtain saturated water vapor with a pressure of about 0.45 MPa, which is returned to the granulator 15 as an aerosol fluid for granulating the slag.
  • the granulated slag in the slag bin 112 is transported to a slag fine powder production line by a truck 115 and directly ground into slag fine powder with a specific surface area of about 420 m 2 /kg.
  • the waste gas generated during the production process is sent to the tail gas purification device 120, and after dust removal and desulfurization treatment to meet the relevant emission standards, it is extracted by the fan 121 and discharged through the chimney 122.
  • the circulation pump 119 circulates the desulfurization and dust removal liquid into the tail gas purification device 120.
  • the concentration of the circulating liquid reaches a certain value (depending on the actual treatment scenario), part of it is discharged and fresh alkaline solution is added from the outside to maintain normal and efficient desulfurization and dust removal effects.
  • the method for coupled utilization of slag waste heat recovery using the device shown in FIG1 can be performed as follows.
  • the method for coupled utilization of slag waste heat recovery includes the following steps:
  • the particle droplets fly along the aerosol fluid in a directional high-speed manner along the guide cover 16 (for example, the flight speed is above 10m/s, which is determined according to actual conditions).
  • the particle droplets exchange heat with the aerosol fluid during the formation and flight process and are rapidly cooled and solidified, generating granulated slag below 1000°C and above 800°C (at this time, only the surface of the particles is solidified, and the core is molten) and an airflow of about 300°C (ambient temperature).
  • the solidification rate of particles with a particle size of less than 2mm is about 85%, thereby achieving granulation and cooling and solidification of the slag;
  • the granulated slag and air flow out of the guide cover 16 and directly enter the cyclone 17, where the slag and air are separated under the combined action of centrifugal force and gravity.
  • the temperature of the separated granulated slag drops below 800°C and flows out from the bottom of the cyclone 17.
  • the separated airflow flows through the cyclone 17 and the overflow pipe, and the temperature is reduced to below 300°C after heat exchange with the cooling water in the spiral heat exchange pipe in the overflow pipe.
  • the cooling water in the heat exchange pipe of the waste heat recovery device 123 absorbs heat and vaporizes, and then passes through the second steam-water separator to obtain saturated water vapor with a pressure of about 0.5 MPa, which is returned to the granulator 15 as an aerosol fluid for granulating the above-mentioned slag;
  • the cooling water in the spiral heat exchange tube absorbs heat and vaporizes, and then passes through the first steam-water separator to separate steam and water to generate saturated steam with a pressure of about 1.6 MPa and a temperature of about 201°C.
  • the saturated steam enters the superheated steam generator 126, and after supplementary heating, superheated steam with a pressure of about 1.6 MPa and a temperature of about 350°C is obtained.
  • natural gas or mixed coal gas generated in the steel smelting process is used to supplement the heat of the saturated steam entering the superheated steam generator 126.
  • the granulated slag flowing out from the bottom of the cyclone 17 enters the drum bed 18, where it contacts and exchanges heat with the heat exchange pipe with cooling water.
  • the drum bed 18 rotates at a low speed in the set direction under the action of the driving mechanism, and the speed is controlled at 3rpm.
  • the granulated slag is slowly pushed by the pushing mechanism in the drum as the drum bed 18 rotates, and is discharged from the drum bed after the temperature drops below 180°C.
  • a vibrator 113 is installed on the slag bin 112 to vibrate the slag bin 112 to prevent the granulated slag from blocking the slag bin outlet, bridging, or arching in the slag bin 112;
  • the cooling water in the heat exchange pipe of the roller bed 18 absorbs heat and then vaporizes.
  • the cooling water is forced to circulate by a booster pump, and after the steam and water are separated in the third steam-water separator 19, saturated steam with a pressure of about 1.6 MPa and a temperature of about 201°C is generated.
  • the saturated steam enters the superheated steam generator 126 and is supplemented with heat by natural gas or mixed coal gas generated in the steel smelting process. After the supplementary heat, superheated steam with a pressure of about 1.6 MPa and a temperature of about 350°C is obtained.
  • the granulated slag in the slag bin 112 is transported to the air flow mill 117 through the slag discharge valve 114 and the conveying mechanism 116, and is impacted and ground into ultrafine powder by the superheated steam obtained in step 2) and step 3).
  • the ultrafine powder is collected by the powder collecting device 118 and directly sold as a high-quality product;
  • the superheated steam pressure drops to normal pressure, and the temperature drops to below 250°C, and then enters the waste heat recovery device 123, and contacts with the heat exchange pipe with cooling water in the waste heat recovery device 123 to further recover waste heat, forming tail gas with a temperature of about 150°C;
  • the cooling water in the heat exchange pipe of the waste heat recovery device 123 absorbs heat and vaporizes, and then passes through the second steam-water separator to obtain saturated water vapor with a pressure of about 0.5 MPa, which is returned to the granulator 15 as an aerosol fluid for granulating the slag.
  • the granulated slag in the slag bin 112 is transported to a slag fine powder production line by a truck 115 and directly ground into slag fine powder with a specific surface area of about 420 m 2 /kg.
  • the waste gas generated during the production process is sent to the tail gas purification device 120, and after dust removal and desulfurization treatment to meet the relevant emission standards, it is extracted by the fan 121 and discharged through the chimney 122.
  • the circulation pump 119 circulates the desulfurization and dust removal liquid into the tail gas purification device 120. When the concentration of the circulating liquid reaches a certain value (depending on the actual treatment scenario), part of it is discharged and fresh alkali liquid is added from the outside to maintain normal and efficient desulfurization and dust removal effects.
  • This embodiment uses the high-speed aerosol fluid sprayed from the granulator to impact, crush, and granulate the blast furnace slag.
  • the flow rate of the high-speed aerosol fluid is controllable, and its flow rate varies with the amount of blast furnace slag weighed by the online weighing device.
  • the blast furnace slag flow rate is small, the flow rate of the aerosol fluid is appropriately reduced, and when the slag flow rate increases, the flow rate of the aerosol fluid increases accordingly.
  • the maximum flow rate of the aerosol fluid can ensure the safe granulation of the blast furnace slag when the blast furnace slag is at its maximum amount.
  • the cooling water in the cyclone and drum bed coil absorbs heat to form 1.2-1.6MPa saturated steam, which is then sent to the superheated steam generator.
  • Natural gas or mixed coal gas produced during steel smelting is used for appropriate heat supplementation.
  • the saturated steam is heated to 1.2-1.6MPa and 250-350°C superheated steam.
  • the superheated steam is directly sent to the air mill as the power for slag pulverization. After the superheated steam expands and works in the air mill, its quality decreases, the pressure drops to normal pressure, and the temperature drops to 150-250°C. This part of the gas enters the waste heat recovery device and is heat exchanged through shell and tube partitions to prepare 0.4-0.5MPa saturated steam.
  • the saturated water vapor formed can be directly sent back to the granulator as the aerosol fluid for granulating the blast furnace slag. After the aerosol fluid reacts with the blast furnace slag, it is separated from the slag gas and then enters the waste heat recovery device for treatment and can be reused.
  • This embodiment can realize the gradient recovery of the sensible heat of the blast furnace slag, and the recovered heat can be used at the same level nearby.
  • the device of the above-mentioned method for coupled utilization of slag waste heat recovery utilizes an aerosol granulation method that combines water quenching and wind crushing to recover the sensible heat of blast furnace slag step by step, and directly utilizes the recovered heat in the blast furnace slag treatment process nearby, which can not only realize the safe and rapid granulation of blast furnace slag, but also improve the utilization rate of the recovered waste heat, avoiding the problem of low efficiency of utilizing the sensible heat of blast furnace slag after conventional methods.
  • water vapor can be recycled, avoiding waste of water resources, reducing the granulation cost of blast furnace slag, making the treatment process environmentally friendly, achieving safe and rapid granulation of blast furnace slag, and obtaining high-quality productized granulated slag, which can realize high-value resource utilization of blast furnace slag and efficient recovery of sensible heat of blast furnace slag.
  • a blast furnace slag granulation device and process with a high-speed steam nozzle which has the advantages of both water quenching and wind quenching granulation technology, and utilizes high-speed steam with water mist to cool and granulate the slag, which can not only appropriately reduce the consumption of new water to reduce costs, but also take into account the cooling rate of the slag to facilitate the formation of glass in the solid slag, and the device can make full use of the waste heat of the slag to reduce energy loss; it has the advantages of fast cooling rate, good slag crushing effect, low energy consumption, etc.
  • FIG2 it shows a device for implementing the slag granulation method according to the present embodiment.
  • the present embodiment provides a blast furnace slag granulation device with a high-speed steam nozzle, comprising: a slag granulation body 21, which is a box structure, a slag flow trough 211 for slag 2100 to enter is arranged on one side of the upper part, and a steam outflow channel 212 is arranged on the top of the slag granulation body 21;
  • the heat exchanger 223 is provided with a waste heat recovery pipeline 23 and a heat exchange fluid outflow pipeline 24 ; wherein, a valve F23 is installed on the waste heat recovery pipeline 23 .
  • the first control valve F21 is an electro-hydraulic gate valve.
  • the axial direction of the nozzle 225 forms an angle of 30 to 60 degrees with the axial direction of the slag flow channel 211 .
  • the slag granulation method using the slag granulation device with high-speed steam nozzle is implemented as follows: the water entering the pipeline is pressurized by a water pump and then enters the heat exchanger.
  • the heat source from the waste heat resource recovery pipeline increases the temperature of the water in the heat exchanger.
  • the water is in a state of being higher than the atmospheric pressure and higher than the boiling point under normal pressure. After being ejected from the nozzle, it is instantly heated under normal pressure.
  • the intermediate gasification forms a high-speed jet containing steam (for example, the injection speed is 90-110 m/s) to impact the slag flowing out of the slag flow trough.
  • the high-speed jet cools the slag and breaks it into small particles that fall into the bottom of the slag granulation body; the mixed jet sprayed from the nozzle impacts the slag and then turns into steam and flows out from the top of the above-mentioned device as waste heat resource for subsequent utilization.
  • the water entering the pipeline is pressurized by a water pump, and the pressure in the pipeline is raised to 0.1-1 MPa; the heat energy from the waste heat recovery pipeline raises the water temperature in the heat exchanger to 100-182°C.
  • the high-speed jet ejected from the nozzle crushes the blast furnace slag and generates water vapor after heat exchange.
  • the water resource consumption is greatly reduced compared with the traditional wet process, which reduces water pollution and the emission of harmful gases. There is no need to dry the cooled blast furnace slag.
  • the sensible heat of the slag is exchanged with the jet ejected from the nozzle, and the thermal enthalpy of the high-temperature water vapor generated is higher than the thermal enthalpy of the hot air generated by the traditional wind quenching process, which makes the recovery efficiency of the sensible heat of the slag higher and has more potential for waste heat recovery;
  • the device consumes less energy to make the fluid in the pipeline have a higher pressure, has low cost, and has less noise pollution.
  • the heat exchange medium is water
  • the cooling rate of the high-temperature slag is also faster than the cooling rate of wind quenching, which is more conducive to the formation of glass. The better the quality of the glass and the higher the content, the higher the recycling rate of the blast furnace slag.
  • the waste heat is used to heat the pipeline.
  • the energy for generating steam comes entirely from the waste heat and waste heat of the steel plant, thus improving the energy utilization rate.
  • a gas-water mixed horizontal slag granulation process and device in which a high-speed airflow sprayed from a gas nozzle array assembly is used to impact liquid slag to break it, and high-density droplet particles sprayed from a gas-liquid dual-fluid nozzle quickly exchange heat and cool the granulated slag particles and assist in granulation, thereby facilitating rapid slag formation; atomization is used instead of the direct water spraying form of water quenching, which can not only appropriately reduce the consumption of new water to reduce costs, but also take into account the cooling rate of the slag to facilitate the formation of a glassy body of the solid slag, and the process can make full use of the waste heat of the slag to reduce energy loss; it has the advantages of faster cooling rate, good slag crushing effect, and low energy consumption.
  • the present embodiment provides a horizontal slag granulation process of gas-water mixing, which uses a high-speed airflow provided by an air nozzle array assembly composed of gas nozzles to crush the falling slag to obtain slag particles; at the same time, a row of gas-liquid dual-fluid nozzles are used to spray water mist on the slag particles to quickly cool the slag particles and apply an auxiliary driving force to the slag particles so that they fall more accurately into the slag particle collection section at the rear.
  • the high-speed gas nozzle is a supersonic nozzle.
  • the device for the above-mentioned gas-water mixing horizontal slag granulation process comprises:
  • the slag granulation body 61 is a box structure, with a slag inlet 611 on the top and a slag chute 612 above it;
  • the high-speed air injection mechanism 62 comprises:
  • the gas storage tank 622 is provided with a pressure gauge 625, an air intake pipe 626 and an air intake valve 6261;
  • the air nozzle array assembly 623 is connected to the air delivery pipeline 620;
  • the spray mechanism 63 includes: a second control valve F62, a water pump 631, a third control valve F63, a pressure gauge 632, a flow meter 633 and a plurality of gas-liquid dual-fluid nozzles 634, 634' which are sequentially arranged along a water pipeline 630; the inlet end of the water pipeline 630 is connected to a water source 6100; the gas-liquid dual-fluid nozzles 634, 634' are arranged at the inner upper part and the bottom of the slag granulation body 61, and the gas-liquid dual-fluid nozzles 634, 634' are connected to the gas pipeline 620 and the water pipeline 630 through a connecting pipe 635.
  • the gas-liquid dual-fluid nozzles 634, 634' are arranged in an array.
  • the axial direction of the air nozzle array assembly 623 forms an angle of 0 to 20 degrees with the horizontal direction; preferably, the width of the air nozzle array assembly 623 is greater than the width of the slag flow inlet 611 .
  • the second control valve F62 is an electro-hydraulic gate valve.
  • the slag granulation body 61 is semi-enclosed, and a slag particle collecting section is provided at the rear thereof.
  • the outlet of the air nozzle array assembly 623 includes a plurality of uniformly distributed spray holes 6231 .
  • the speed of the high-speed airflow ejected by the air nozzle array assembly is preferably 90-110 m/s. If the airflow speed is too low, the slag cannot be fully broken, and the slag will fall quickly and adhere to the inner wall of the slag granulation body; if the airflow speed is too high, the granulation effect and the slag particle size may not be significantly improved.
  • the high-speed jets ejected from the air nozzles of the air nozzle array assembly break up the blast furnace slag, which greatly reduces water resource consumption compared to the traditional wet process, reduces water pollution, and reduces the emission of harmful gases.
  • the gas pipeline is not easy to wear and tear, the maintenance cost is low, and no additional energy is needed to dry the cooled blast furnace slag.
  • the sensible heat of the slag is exchanged with a large number of droplets sprayed from the atomizing nozzle, and the thermal enthalpy of the generated high-temperature water vapor is higher than the thermal enthalpy of the hot air generated by the traditional wind quenching process, which makes the recovery efficiency of the sensible heat of the slag higher and has more potential for waste heat recovery;
  • the heat exchange medium of the device according to this embodiment is mainly droplet particles formed by water crushing, and the cooling rate of the high-temperature slag is also faster than the cooling rate of the wind quenching, which is more conducive to the formation of glass.
  • the bottom and top of the slag granulation body are equipped with multiple rows of gas-liquid dual-fluid atomizing nozzles to form evenly distributed mist droplets for heat exchange with the slag.
  • the heat exchange between the even mist droplets and the slag is more sufficient, and the even air flow field makes the granulation effect more uniform and the slag forming effect better.
  • the droplets sprayed by the atomizing nozzle have a certain auxiliary effect on the granulation and flight of slag particles, and the effect is better than that of pure gas quenching.
  • the slag granulation body is a horizontal semi-enclosed device, with a slag collection section at the rear, which can more conveniently collect the granulated slag and prevent the slag from sticking to the wall due to difficulty in collection;
  • Nozzle arrays are arranged near the slag flow inlet, in the middle of the granulation device, and at the bottom of the granulation device to impact, thin, and granulate the slag flow in sections to prevent insufficient granulation due to excessive slag flow.
  • a device for granulating blast furnace slag using a gas nozzle array wherein the high-speed airflow ejected from the high-speed gas nozzle is used to impact the liquid slag to break it, and the granulated slag particles are quickly cooled to facilitate rapid slag formation, and water consumption can be appropriately reduced to reduce costs, while taking into account the cooling rate of the slag to facilitate the formation of a glassy body of the solid slag.
  • the device can make full use of the waste heat of the slag to reduce energy loss, and has the advantages of both water quenching and air quenching granulation technologies; the cooling rate is relatively fast, the slag crushing effect is good, and the energy consumption is low.
  • the device for granulating blast furnace slag using a gas nozzle array includes:
  • the slag granulation body 31 is a box structure, and a slag inlet 311 and a steam outflow channel 312 are arranged on the top.
  • the blast furnace slag 3100 passes through the slag chute 313 and the slag inlet 311 into the slag granulation body 31;
  • the high-speed air injection mechanism 32 comprises:
  • the gas storage tank 322 is provided with a pressure gauge 326, an air intake pipe 327 and an air intake valve F32;
  • the nozzle array 324 includes a plurality of nozzles 3241 and corresponding branch pipes 3242 .
  • Each branch pipe 3242 is connected to the gas pipeline 323 .
  • the nozzle 3241 is disposed on a side wall of the slag granulation body 31 .
  • the nozzles 3241 in the nozzle array 324 are one or more selected from supersonic nozzles, atomizing nozzles or gas-liquid dual-fluid nozzles; the axial direction of the nozzles 3241 in the nozzle array 324 is perpendicular to the side wall of the slag granulation body 31 .
  • the nozzles 3241 in the nozzle array 324 are arranged in multiple rows and columns.
  • the nozzles 3241 in the nozzle array 324 are arranged in multiple rows and columns, and the nozzles in two adjacent rows are staggered in the vertical direction.
  • the nozzles 3241 in the nozzle array 324 are arranged in multiple rows and columns, and the number of nozzles gradually decreases or increases along the vertical direction.
  • the high-speed jet (for example, the jet speed is 90-110 m/s) ejected from the high-speed gas nozzle breaks up the blast furnace slag, reduces water resource consumption, reduces water pollution, and reduces the emission of harmful gases. Therefore, the gas pipeline is not easy to wear and tear, the maintenance cost is low, and no additional energy is required to dry the cooled blast furnace slag.
  • the device according to this embodiment can reach a higher speed at the same pressure by arranging high-speed gas nozzles with less energy consumption, low cost, and less noise pollution.
  • the cooling rate of high-temperature slag is also faster than that of traditional wind quenching, which is more conducive to the formation of glass.
  • the slag granulation device further includes: a nozzle atomizing mechanism 33, which includes a second control valve F32, a water pump 331, a third control valve F33, a pressure gauge 332, a flow meter 333 and a plurality of atomizing nozzles 334 which are sequentially arranged along a water supply pipe 330; the inlet end of the water supply pipe 330 is connected to a water source 3200; the atomizing nozzles are arranged at the inner bottom of the slag granulation body 31 and are arranged in at least two rows, and the direction in which the water mist is sprayed is directly facing the slag flowing in from the slag inlet 311.
  • a nozzle atomizing mechanism 33 which includes a second control valve F32, a water pump 331, a third control valve F33, a pressure gauge 332, a flow meter 333 and a plurality of atomizing nozzles 334 which are sequentially arranged along a water supply pipe 330; the inlet end
  • FIG. 14 it is a schematic diagram of the structure of a slag granulation device according to another embodiment of the present invention, wherein the nozzles in the nozzle array 324 are gas-liquid dual-fluid nozzles; accordingly, the slag granulation device is further provided with a nozzle water supply mechanism 36, which includes a fourth control valve F34, a water pump 361, a fifth control valve F35, a pressure gauge 360, and a pressure gauge 361 arranged in sequence along a water delivery pipeline 360. 362, flow meter 363; the inlet end of the water delivery pipeline 360 is connected to the water source 3200, and the outlet end is connected to the inlet end of the gas-liquid dual-fluid nozzle.
  • a nozzle water supply mechanism 36 which includes a fourth control valve F34, a water pump 361, a fifth control valve F35, a pressure gauge 360, and a pressure gauge 361 arranged in sequence along a water delivery pipeline 360.
  • flow meter 363 the inlet end of the water delivery
  • FIG. 15 it is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention, wherein the slag granulation device further includes a waste heat recovery system 34, which includes:
  • the heat exchange box 341 has a feed port 3411 connected to the discharge port of the slag granulation body 31 on the upper part of one side wall; a heat exchange air flow outlet 3412 is provided on the top of the heat exchange box 341; a plurality of perforated bed plates 342 are provided in the height direction of the heat exchange box 341; a slag particle outlet 3413 is provided at the bottom of the heat exchange box 341;
  • the gas nozzle array 343 is arranged at the inner bottom of the heat exchange box 341 and below the perforated bed plate 342.
  • the gas nozzles in the gas nozzle array are arranged opposite to the perforated bed plate 342.
  • the sprayed gas can further cool the slag particles falling along the perforated bed plate 342.
  • the perforated bed plate 342 is arranged in a Z-shape along the vertical direction in the heat exchange box 341, as shown in FIG. 15, which can extend the falling path of the slag particles and is conducive to the effective cooling of the slag particles.
  • the slag granulation process is carried out in the slag granulation body.
  • the high-speed air injection mechanism and the atomizing nozzle mechanism provide the main power for crushing and granulating the slag and for primary heat exchange.
  • the waste heat recovery system separates the slag particles and gas and performs secondary heat exchange.
  • the nozzle array in the high-speed air injection mechanism provides uniform high-speed airflow to evenly break the falling blast furnace slag, and obtain high-temperature slag particles moving in a parabola; the atomizing nozzle in the nozzle atomizing mechanism sprays water mist on the slag particles moving in a parabola at the bottom of the slag granulation body, which increases the heat exchange efficiency and quickly cools the slag particles, and exerts a driving force on the slag.
  • a slag particle collection section is provided at the tail of the slag granulation body, which brings the slag particles and the high-temperature airflow formed by cooling the slag into the heat exchange box of the waste heat recovery system for gas-solid separation.
  • the slag particles pass through multiple perforated bed plates and are fully heat-exchanged with the cold air ejected by the gas nozzles of the gas nozzle array below.
  • the heat exchange air flows out from the upper outlet, and the cold slag falls from the lower outlet of the heat exchange box.
  • the compressor When in use, the compressor is turned on, the compressor pressurizes the gas and sends the gas into the gas tank, and the gas tank provides stable pressure gas to the (supersonic gas) nozzle array, and the nozzle injects high-speed airflow into the slag granulation body to crush the slag entering from the slag inlet; at the same time, the water pump is turned on, the water pump pressurizes the water in the water pipeline, and then sprays it out through the atomizing nozzle.
  • the droplet particles impact the granulated slag particles, and the slag particles are quickly cooled and cooled into stable small particles; the mixed jets sprayed by the nozzles in the nozzle array and the atomizing nozzles in the nozzle atomizing mechanism impact the high-temperature slag, which are all converted into a mixture of high-temperature air and water vapor, and flow out from the top of the slag granulation body as a waste heat resource to be subsequently recycled.
  • FIG. 16 is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention, wherein the waste heat recovery system 34 adopts a cyclone separator 35 .
  • the cyclone separator 35 includes a separator body 351 , an upper side of which is provided with a gas-solid medium inlet 3511 connected to the discharge port 314 of the slag granulation body 31 ; an air outlet 3512 is provided at the top of the separator body 351 , and an ash hopper 352 is provided at the bottom of the separator body 351 .
  • the slag particles and the high-temperature air flow enter the cyclone separator 35 for gas-solid separation.
  • the cyclone separator 35 can separate a clean high-temperature air flow, which can fully recover the waste heat generated during the slag granulation process for subsequent use.
  • the high-speed jet ejected from the high-speed gas nozzle breaks up the blast furnace slag, which reduces water resource consumption, reduces water pollution, and reduces the emission of harmful gases.
  • the gas pipeline is not easy to wear and tear, the maintenance cost is low, and no additional energy is required to dry the cooled blast furnace slag.
  • this device uses less energy consumption by arranging high-speed gas nozzles to make the gas in the tube reach a higher speed under the same pressure, with low cost and less noise pollution.
  • the cooling rate of high-temperature slag is also faster than that of traditional wind quenching, which is more conducive to the formation of glass. The better the quality and content of the glass, the higher the recycling rate of blast furnace slag.
  • a uniformly distributed high-speed gas flow (for example, a jet speed of 90 to 110 m/s) is formed to exchange heat with the slag.
  • the arrangement of the nozzle array can exchange heat with the slag more fully.
  • the gas flow area formed by the array can evenly and fully cover the range of the slag flow, making the granulation effect more uniform and the slag formation effect better;
  • the method of installing multiple atomizing nozzles at the bottom of the slag granulation body forms evenly distributed mist droplets to exchange heat with the slag.
  • the heat exchange between the mist droplets and the slag is more sufficient; and the spraying of the mist droplets provides a driving force for the slag particles after gas quenching, so that they do not fall into the bottom of the device too early and stick together;
  • the high-speed gas is arranged in the form of a (supersonic) nozzle array, and the gas flow domain formed by the array can evenly and fully cover the range of the slag flow, so that the granulation effect is more uniform and the slag forming effect is better;
  • a multi-layer arrangement is designed through the waste heat recovery section.
  • the slag particles and high-temperature airflow enter the heat exchange box for secondary waste heat gas recovery, heat exchange and gas-solid separation, which greatly improves the waste heat recovery efficiency.
  • the gas nozzles arrayed at the bottom can quickly cool the slag particles and separate the high-temperature airflow, so that the waste heat of the slag can be fully recovered.
  • a device for aerosol slag granulation that can clean up fallen slag.
  • the high-speed airflow sprayed by the high-speed nozzle array assembly is used to impact the liquid slag to break it.
  • the high-density droplet particles sprayed by the atomizing nozzle quickly cool the granulated slag particles to facilitate rapid slag formation.
  • the atomization form replaces the form of direct water spraying for water quenching, which can appropriately reduce the consumption of new water to reduce costs, and can also take into account the cooling rate of the slag to facilitate the formation of a glass body in the solid slag.
  • the device can make full use of the waste heat of the slag to reduce energy loss; it has the advantages of fast cooling rate, good slag crushing effect, low energy consumption, etc.
  • the device for granulating gas mist slag that can clean the fallen slag in this embodiment includes:
  • the slag granulation body 41 is a box structure, with a slag inlet 411 at the top and a slag collecting section 412 at the tail.
  • the slag 4100 enters the slag granulation body 41 from the slag inlet 411 through the slag chute 413.
  • a gas nozzle array 42 is disposed on a side wall of the slag granulation body 41;
  • the atomizing nozzle array 43 is arranged at the inner bottom of the slag granulating body 41, and the atomizing nozzle array 43 sprays the atomizing nozzle in a direction corresponding to the slag flowing in from the slag inlet 411;
  • the slag cleaning nozzle 44 is disposed at the bottom of the slag granulation body 41 , and the outlet of the slag cleaning nozzle faces the bottom of the slag granulation body 41 and the slag particle collecting section 412 .
  • the axial direction of the gas nozzle array 42 is perpendicular to the side wall of the slag granulation body 41 .
  • the slag cleaning nozzle 44 is one or more selected from a water atomizing nozzle, a steam atomizing nozzle, a high-speed air flow nozzle or a gas-liquid dual-fluid nozzle.
  • the gas nozzle array provides a uniform high-speed airflow (for example, the injection speed is 90-110 m/s), which evenly breaks the falling blast furnace slag to obtain broken slag particles in parabolic motion; the atomizing nozzle sprays water mist at the inner bottom of the slag granulating body towards the slag particles in parabolic motion, which on the one hand increases the heat exchange efficiency and quickly cools the broken slag particles, and on the other hand exerts a driving force on the slag.
  • the injection speed is 90-110 m/s
  • a slag collection section is provided at the tail of the slag granulating body, and a slag cleaning nozzle (atomizing nozzle) is used to heat and purge the slag particles that fall to the inner bottom of the slag granulating body to prevent the slag particles from sticking to the wall.
  • a slag cleaning nozzle atomizing nozzle
  • FIG. 19 and FIG. 20 are schematic diagrams of the structure of a slag granulation device according to another embodiment of the present invention, the device is further provided with:
  • the high-speed air injection mechanism 420 comprises:
  • the gas storage tank 422 is provided with a pressure gauge 426, an air intake pipe 427 and an air intake valve F42;
  • the gas nozzle array 42 includes nozzles and corresponding branch pipes 4231 and 4232, and the branch pipes are connected to the gas pipeline 423; the slag cleaning nozzle 44 is connected to the gas pipeline 423 through a connecting pipe 441 and a valve;
  • the nozzle atomizing mechanism 430 includes a second control valve F42, a water pump 432, a third control valve F43, a pressure gauge 433, and a flow meter 434 which are sequentially arranged along a water delivery pipe 431; the inlet end of the water delivery pipe 431 is connected to a water source 4200, and the outlet end thereof is connected to the atomizing nozzle array 43.
  • the nozzles of the atomizing nozzle array 43 are gas-liquid dual-fluid nozzles, and their inlet ends are connected to the gas pipeline 423 and the water pipeline 431 respectively.
  • FIG. 20 which is a schematic structural diagram of a slag granulation device according to another embodiment of the present invention, wherein a plurality of slag inlets 411, 411' are provided on the top of a slag granulation body 41.
  • FIG. 21 one arrangement of the slag inlet in the top view of the slag granulation body 41 in FIG. 20 is shown.
  • a plurality of slag inlet ports 411, 411′, 411′′ are provided on the top of the slag granulation body 41.
  • FIG. 22 shows a schematic diagram of the structure of the nozzles in the gas nozzle array 42 in this embodiment, wherein a large number of gas injection holes 4201 are evenly arranged at the center, and the number of holes and the number of rows can be adjusted according to actual conditions.
  • FIG 23 shows another structural design of the gas nozzle array 42 in this embodiment, in which baffles 428 are respectively provided on both sides of the outlet position of the gas nozzle array 42, and liquid/atomizing nozzles 429 are respectively installed on the outer sides of the baffles 428.
  • the high-speed air ejected by the gas nozzle array 42 is used to break up and atomize the water ejected by the liquid/atomizing nozzle 429.
  • the high-speed jet ejected from the gas nozzle array breaks up the slag, which greatly reduces water consumption compared to the traditional wet process, reduces water pollution, and reduces the emission of harmful gases.
  • the gas pipeline is not easy to wear and tear, the maintenance cost is low, and no additional energy is required to dry the cooled blast furnace slag.
  • the sensible heat of the slag is exchanged with a large number of droplets sprayed from the atomizing nozzle array, and the thermal enthalpy of the generated high-temperature water vapor is higher than the thermal enthalpy of the hot air generated by the traditional wind quenching process, which makes the recovery efficiency of the sensible heat of the slag higher and has more potential for waste heat recovery and utilization;
  • the heat exchange medium in this embodiment uses water to break up the droplet particles, and the cooling rate of the slag is faster than that of the wind quenching, which is more conducive to the formation of glass.
  • mist droplets By installing multiple atomizing nozzles at the bottom, evenly distributed mist droplets are formed to exchange heat with the slag. Compared with the general water flow impact, the heat exchange between the mist droplets and the slag is more sufficient.
  • the spray of mist droplets provides a driving force for the slag particles after gas quenching, preventing them from falling to the bottom of the device too early and causing adhesion.
  • the gas nozzles are arranged in the form of a gas nozzle array.
  • the gas flow field formed by the array can evenly and fully cover the range of slag flow, making the granulation effect more uniform and the slag forming effect better;
  • An atomizing nozzle for cleaning slag is arranged at the bottom of the slag granulation body, which can clean the slag that falls to the bottom of the granulation device to prevent the slag from sticking to the wall;
  • the top of the slag granulation body is provided with a plurality of slag inlets, which divide the slag into small-flow slag flows, thereby greatly improving the slag processing capacity of the nozzle and the slag granulation efficiency.
  • a device for rapidly cooling molten slag by using an atomizing nozzle wherein a high-speed airflow ejected from a high-speed gas nozzle is used to impact liquid molten slag to break it, and high-density droplet particles ejected from the atomizing nozzle rapidly cool down the granulated slag particles to facilitate rapid slag formation, and the form of direct water spraying in water quenching is replaced by atomization, which can not only appropriately reduce the consumption of new water to reduce costs, but also take into account the cooling rate of the slag to facilitate the formation of a glass body of the solid slag, and the device can make full use of the waste heat of the slag to reduce energy loss; it has the advantages of faster cooling rate, good slag crushing effect, and low energy consumption.
  • the device for rapidly cooling slag using an atomizing nozzle includes:
  • the slag granulation body 71 is a box structure, and a slag inlet 711 is provided on the top;
  • a gas nozzle array 72 wherein the gas nozzles are arranged on a side wall of the slag granulation body 71, and the axial directions of the gas nozzles in the gas nozzle array are perpendicular to the side wall of the slag granulation body;
  • the flow field optimization nozzle array 73 is arranged at the inner upper part of the slag granulation body 71, near the slag flow inlet 711;
  • a slag cleaning nozzle array 74 is disposed at the inner lower portion or bottom of the slag granulation body 71;
  • the atomizing nozzle array 75 is disposed in the slag granulating body 71 and arranged radially around the slag flow 7100 on the inner wall of the slag granulating body 71.
  • the axial direction of the atomizing nozzles in the atomizing nozzle array is perpendicular to the axial direction of the gas nozzles.
  • a slag collecting section 76 is provided at the tail of the slag granulation body 71 .
  • the nozzles of the flow field optimization nozzle array 73 are gas nozzles or gas-liquid dual-fluid nozzles.
  • the nozzles of the slag cleaning nozzle array 74 are gas nozzles.
  • the nozzles of the atomizing nozzle array 75 are water atomizing nozzles.
  • the slag falling from the slag container 77 into the slag granulation body 71 is evenly crushed by a uniform high-speed airflow (for example, a jet speed of 90 to 110 m/s) provided by a gas nozzle array 72, thereby obtaining slag particles moving in a parabolic motion.
  • the flow field optimized nozzle array 73 further sprays the slag particles moving in a parabolic motion on the upper part of the slag granulation body 71, thereby increasing the flight speed of the slag to enhance the heat exchange on the one hand, and preventing the slag from sticking to the wall and damaging the device on the other hand.
  • a plurality of layers of atomizing nozzles are arranged on the periphery of the inner wall of the slag granulation body 71, and the atomizing nozzles are evenly arranged around the inner wall of the slag granulation body 71, so that the slag particles are cooled rapidly, and the slag particles and the high-temperature gas generated by the heat exchange are collected by the slag particle collection section at the tail of the slag granulation body 71.
  • this embodiment has the following advantages:
  • the high-speed jet ejected from the high-speed gas nozzle breaks up the blast furnace slag, which greatly reduces water resource consumption compared with the traditional wet process, reduces water pollution, and reduces the emission of harmful gases.
  • the gas pipeline is not easy to wear and tear, the maintenance cost is low, and no additional energy is required to dry the cooled blast furnace slag;
  • the sensible heat of the slag is exchanged with a large number of droplets sprayed from the atomizing nozzle, and the thermal enthalpy of the generated high-temperature water vapor is higher than the thermal enthalpy of the hot air generated by the traditional wind quenching process, which makes the recovery efficiency of the sensible heat of the slag higher and has more potential for waste heat recovery;
  • the cooling rate of high-temperature slag is also faster than that of wind quenching, which is more conducive to the formation of glass.
  • the inner wall of the slag granulation body is uniformly surrounded by multiple atomizing nozzles to form evenly distributed mist droplets for heat exchange with the slag. Compared with the general water flow impact, the heat exchange between the mist droplets and the slag is more sufficient.
  • the optimized nozzle array is used to provide a driving force to the initially crushed slag particles again, so as to prevent them from falling to the bottom of the device too early and causing adhesion;
  • the high-speed gas is arranged in the form of a nozzle array.
  • the gas flow field formed by the array can evenly and fully cover the range of slag flow, making the granulation effect more uniform and the slag forming effect better.
  • a water mist granulation device for granulating blast furnace slag which uses a high-speed water flow (for example, a spraying speed of 90-110 m/s) sprayed by a water nozzle array assembly and a water mist (for example, a spraying speed of 90-110 m/s) sprayed by a gas-liquid dual-fluid nozzle to impact the liquid slag to break it, and the high-density droplet particles sprayed by the atomizing nozzle quickly heat exchange and cool the broken slag particles and assist in granulation, so as to facilitate rapid slag formation.
  • a high-speed water flow for example, a spraying speed of 90-110 m/s
  • a water mist for example, a spraying speed of 90-110 m/s
  • Replacing the form of direct water spraying with water quenching with atomization can not only appropriately reduce the consumption of new water to reduce costs, but also take into account the cooling rate of the slag to facilitate the formation of glass in the solid slag, and the device can make full use of the waste heat of the slag to reduce energy loss; it has the advantages of fast cooling rate, good slag crushing effect, and low energy consumption.
  • this embodiment provides a water mist granulation device for granulating blast furnace slag, which includes:
  • the frame 51 is a frame structure
  • the water nozzle array assembly 52 includes:
  • the body 521 is a box structure, which is arranged in the middle of the frame 51; a flow equalizing plate 522 and a flow guide plate 523 are arranged in sequence therein; the rear end of the body 521 is connected to a water source;
  • a water nozzle array 524 is evenly distributed on the front end surface of the body 521;
  • the gas-liquid dual-fluid nozzle assembly 53 comprises:
  • Gas-liquid dual-fluid nozzles 531 are arranged in parallel on both sides of the water nozzle array 524 and fixed on the frame 51;
  • the gas pipeline 532 and the water pipeline 533 are fixed on the frame 51 and connected to the gas-liquid dual-fluid nozzle 531 .
  • the gas-liquid dual-fluid nozzles 53 , 53 ′ are arranged in parallel on both sides of the water nozzle array 524 .
  • the rear end of the main body 521 of the water nozzle array assembly 52 is connected to the water source through a flange. After the water enters the main body 521, it passes through the flow equalizer 522 and the guide plate 523, so that the water pressure is evenly distributed and enters the water nozzle array 524 to spray the water out; at the same time, the gas and liquid enter the gas-liquid dual-fluid nozzle 531 from the gas pipeline 532 and the water pipeline 533 respectively for atomization.
  • the high-speed jets ejected by the water nozzle array assembly break up the blast furnace slag, which greatly reduces water resource consumption compared to the traditional wet process, reduces water pollution, and reduces the emission of harmful gases;
  • the sensible heat of the slag is exchanged with a large number of droplets sprayed from the atomizing nozzle, and the thermal enthalpy of the generated high-temperature water vapor is higher than the thermal enthalpy of the hot air generated by the traditional wind quenching process, which makes the recovery efficiency of the sensible heat of the slag higher and has more potential for waste heat recovery;
  • the heat exchange medium of this device is mainly droplet particles formed by water fragmentation.
  • the cooling rate of high-temperature slag is also faster than that of wind quenching, which is more conducive to the formation of glass.
  • the jet flow field formed by the array can evenly and fully cover the range of slag flow, making the granulation effect more uniform and the slag forming effect better.

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Abstract

熔渣粒化方法，包括破碎熔渣得到熔渣颗粒，然后对熔渣颗粒进行冷却，并收集由此获得的粒化渣。以及实施相应熔渣粒化方法的熔渣粒化装置，包括：粒化机构，用于粒化熔渣获得破碎的熔渣颗粒；以及冷却机构，用于冷却熔渣颗粒获得粒化渣。

Description

熔渣粒化方法及装置 技术领域
本申请涉及钢铁冶炼技术领域，特别涉及熔渣粒化方法及装置。
背景技术
高炉熔渣是冶炼生铁时从高炉中排出的一种熔融状态的废渣，其成分主要为CaO、SiO2、Al2O3、MgO，其产量庞大，是冶金行业中产生数量最多的一种副产物。每生产1吨铁产生350公斤左右的高炉熔渣。出炉温度高可达1450～1650℃。每吨渣含(1260-1880)×103kJ的显热，相当于60kg标准煤的发热量，在余热回收的方面存在着较大的潜力、济性与可行性，在这种现状下，对高炉渣余热回收利用的研究成为近年来企业关注的焦点。
目前高炉熔渣的处理多采用水淬工艺，熔渣被高压水冲制成水渣，高品位的显热随之转移到80℃左右的水渣和废水中，失去回收利用价值，且每处理1吨高炉熔渣需要消耗0.4～0.5吨水、同时排放大量富含H2S、SO2等污染物的废蒸汽。在后续资源化利用(如微粉化)时，还需要将水渣中15～20％的水分烘干，每吨高炉熔渣又需要消耗大约1000m3的500℃的热风。
由于高炉熔渣导热系数低、粘度具有随温度降低而急剧升高的特性，造成高炉熔渣的换热慢，余热回收难度高。将高炉熔渣快速微粒化，增加换热面积，提高传热效率，可以快速、高效地回收高炉熔渣显热。熔渣颗粒的快速冷却不仅为回收热量创造条件，同时可以保持冷却后渣粒的玻璃体含量和活性能够达到矿渣微粉原料的要求，维持现有炉渣资源化途径的畅通。
到目前为止，能够对熔渣快速干式粒化的工艺主要有风碎法和离心粒化法。风碎法因噪音大、易产生渣棉而未能在高炉熔渣的处理领域推广应用，只有个别钢厂利用该方法用于处理流动性好的钢渣。离心粒化主要采用转碟或转杯为粒化器，利用离心力将熔渣分散、碎裂成细小的熔滴以便快速冷却，保持冷却后渣粒的玻璃体含量和活性能够达到矿渣微粉原料的要求，但离心粒化工艺还处于实验室探索阶段，尚存在炉渣结壳、粒化渣粒度不均匀、易产生渣棉等问题，有待进一步研究改进。
中国专利申请CN201410755689.9名称为“高温熔渣余热回收系统及方法”，公开了利用转盘来粒化熔渣的方法及装置，通过余热锅炉回收高温粒渣的热量。
中国专利申请CN201010566938.1名称为“冶金熔渣干式粒化及热能回收系统”，提出了一种冶金熔渣干式粒化及热能回收系统。其中，液态熔渣采用离心旋转和气流脉冲的方式进行干式粒化，通过脉冲气流和流化气体将熔渣中显热转移到热空气中，利用余热锅炉回收热空气中的热量，形成中低压蒸汽，用于汽轮机发电。
中国专利CN101736101B名称为“半湿法炉渣处理余热回收发电系统及方法”以及中国专利CN102433401B名称为“熔融炉渣急冷干式粒化及显热回收发电系统及其方法”，提供了在风碎的基础上引入水雾的方案，利用高压水-空气雾化装置将熔融炉渣急冷粒化，使其迅速冷却为玻璃体态小颗粒，再通过流化床或振动床实现高温粒渣的余热回收。
目前高炉熔渣的粒化主要是水淬工艺，单纯的风碎工艺不太适合，离心粒化工艺尚在开发中；高炉熔渣的余热利用局限在通过热空气/氮气转化成蒸汽及发电，效率低下。
发明内容
为了克服现有技术中存在的问题，本发明提供了多种熔渣粒化方法及装置，可以实现对高炉熔渣的、安全粒化，并可选地回收粒化过程中产生的热量并同时进行利用或待后续利用。
本发明的第一方面提供一种熔渣粒化方法，破碎熔渣得到熔渣颗粒，然后对所述熔渣颗粒进行冷却，并收集由此获得的粒化渣。
具体地，上述熔渣粒化方法可通过以下方式进行。
熔渣通过射流粒化获得表面固化的颗粒和蒸汽，随后所述表面固化的颗粒在旋流场中进行冷却，获得固态渣粒。
在本发明中，如无特殊说明，射流是指高速气雾流体，为气水混合物，水与压缩空气一起喷出形成高速运动的气体和粒径在0.01-0.20mm之间的水滴的混合物。气水混合物运动速度的下限为20m/s，优选50m/s，更优选70m/s，最优选90m/s。水滴运动速度的上限通常不作限定，出于设备功耗考虑，水滴运动速度的上限可为150m/s，优选120m/s。
如无特殊说明，本发明中的熔渣指高炉熔渣，其出炉后温度在1300～1500℃。在本发明的熔渣粒化过程中，熔渣先被射流破碎粒化，在与射流(高速气水混合物)接触后，热量会部分转移给水滴，熔渣表面在细密的水滴中固化，形成表面固化的颗粒，此时颗粒的温度约在800～1000℃之间，因此颗粒芯部仍是熔融态，而高速水滴吸收热量后形成水蒸气。 随后，表面固化的颗粒进入旋流场中，在旋流场的作用下进行高速公转和自转。颗粒在旋流场中的公转速度为5～25rad/s，公转半径为80-120mm，自转速度为100～400rad/s。随着颗粒高速公转和自转，加速颗粒表面边界层的分离和剥落，边界层厚度减薄，换热界面快速更新，从而减小热阻，提高换热效率，在此过程中被环境气氛冷却，形成固态渣粒。
在本发明中，旋流场由旋流器提供，旋流场增加了熔渣的运动路径，增强了熔渣颗粒与环境气氛的换热效率，因此与现有技术中的其他冷却方式相比，冷却效果更佳。
根据本发明的一种实施方式提供一种熔渣余热回收耦合利用方法，包括如下步骤：
1)熔渣进入导流罩内，被从粒化器喷出的气雾流体冲击、破碎、粒化成粒径在5mm以内的颗粒熔滴，所述颗粒熔滴随气雾流体沿着导流罩定向飞行，颗粒熔滴在形成和飞行过程中与气雾流体换热得到冷却固化，生成1000℃以下的粒化渣(渣粒的形态取决于其温度，此时的粒化渣是仅表面固化的颗粒，未被完全冷却为固态渣粒)和300～600℃的气流，实现对所述熔渣的粒化和冷却固化；
2)所述粒化渣和所述气流从导流罩内流出后直接进入旋流器内，在离心力和重力共同作用下实现渣、气分离，分离后的粒化渣温度下降到700～800℃，从所述旋流器的底部流出；
分离后的气流流经旋流器和溢流管，经溢流管内的螺旋换热管的冷却水换热后温度降到150～300℃，从旋流器和溢流管排出后进入余热回收装置，与余热回收装置内通有冷却水的换热管道接触换热进一步回收余热，形成温度为130～150℃的尾气；
所述余热回收装置的换热管道内的冷却水吸收热量后汽化，之后经过汽水分离获得压强在0.4～0.5MPa的饱和水蒸汽，返回所述粒化器作为流体用于粒化所述熔渣；
螺旋换热管内的冷却水吸收热量汽化，随后经过汽水分离生成压强为1.2～1.6MPa、温度在188～201℃的饱和蒸汽，所述饱和蒸汽进入过热蒸汽发生器，补热后获得压强为1.2～1.6MPa、温度为250～350℃的过热蒸汽；
3)自旋流器的底部流出的粒化渣进入滚筒床，在滚筒床内与通有冷却水的换热管道接触换热，温度降至150～300℃，随后排出进入渣仓储存；
滚筒床的换热管道内的冷却水吸收热量后汽化，经过汽水分离生成压强为1.2～1.6MPa、温度在188～201℃饱和蒸汽，所述饱和蒸汽进入过热蒸汽发生器，补热后获得压强为1.2～1.6MPa、温度在250～350℃的过热蒸汽；
4)渣仓内的粒化渣输送进入气流磨，利用步骤2)和步骤3)获得的过热蒸汽冲击、研磨成超细微粉；
过热蒸汽的压强降为常压，温度降至150～250℃，随后进入余热回收装置，与余热回收装置内通有冷却水的换热管道接触换热进一步回收余热，形成温度为130～150℃的尾气；
所述余热回收装置的换热管道内的冷却水吸收热量后汽化，之后经过汽水分离获得压强为0.4～0.5MPa的饱和水蒸汽，返回所述粒化器作为流体用于粒化所述熔渣。
优选地，所述尾气经尾气净化装置除尘、脱硫后排放。
优选地，在上述步骤1)中，所述气雾流体选自压强为0.5-0.8MPa的压缩空气、压强为0.4-0.5MPa的高压水雾、压强为0.4-0.8MPa的低压蒸汽，以及它们的混合物中的一种以上。
优选地，在上述在步骤1)中，所述颗粒熔滴冷却固化后粒径为2mm以内的颗粒的凝固率在80％以上。
优选地，在上述步骤3)中，在所述过热蒸汽发生器中利用天然气或钢铁冶炼过程中产生的混合煤气对所述饱和蒸汽进行补热。
优选地，在上述步骤3)中，将进入渣仓的粒化渣运送至矿渣微粉生产线，直接研磨成比表面积为420～440m2/kg的矿渣微粉。
优选地，在上述步骤4)中，所述超细微粉的比表面积为450-750m2/kg。
当然，本发明的熔渣余热回收耦合利用方法还可以按如下实施。具体地，根据本发明的另一实施方式提供的熔渣余热回收耦合利用方法，包括如下步骤：
1)熔渣进入导流罩内，被从粒化器喷出的气雾流体冲击、破碎、粒化成粒径在5mm以内的颗粒熔滴，所述颗粒熔滴随气雾流体沿着导流罩定向飞行，颗粒熔滴在形成和飞行过程中与气雾流体换热得到冷却固化，生成表面固化(约1250℃左右)的粒化渣和100℃左右的气流，实现对所述熔渣的粒化和冷却固化；
2)所述粒化渣和所述气流从导流罩内流出后直接进入旋流器内，在离心力和重力共同作用下实现渣、气换热和分离，分离后的粒化渣温度下降到650～850℃，从所述旋流器的底部流出；
所述气流在旋流器内被渣粒加热到200-600℃后，经溢流管进入余热锅炉。
3)所述气流经过余热锅炉换热后温度降到150～300℃后进入余热回收装置，与余热回收装置内通有冷却水的换热管道接触换热进一步回收余热，气流温度降为130～150℃；
所述余热回收装置的换热管道内的冷却水吸收热量后汽化，之后经过汽水分离获得压强在0.4～0.5MPa的饱和水蒸汽，返回所述粒化器作为流体用于粒化所述熔渣；
余热锅炉内的冷却水吸收热量汽化，随后经过汽水分离生成压强为1.2～1.6MPa、温度在188～201℃的饱和蒸汽，所述饱和蒸汽进入过热蒸汽发生器，补热后获得压强为1.2～1.6MPa、温度为250～350℃的过热蒸汽；
4)自旋流器的底部流出的粒化渣进入滚筒床，在滚筒床内与通有冷却水的换热管道接触换热，温度降至150～300℃，随后排出进入渣仓储存；
滚筒床的换热管道内的冷却水吸收热量后汽化，经过汽水分离生成压强为1.2～1.6MPa、温度在188～201℃饱和蒸汽，所述饱和蒸汽进入过热蒸汽发生器，补热后获得压强为1.2～1.6MPa、温度在250～350℃的过热蒸汽；
5)渣仓内的粒化渣输送进入气流磨，利用步骤2)和步骤3)获得的过热蒸汽冲击、研磨成超细微粉；
过热蒸汽压强降为常压，温度降至150～250℃，随后进入余热回收装置，与余热回收装置内通有冷却水的换热管道接触换热进一步回收余热，形成温度为130～150℃的尾气；
所述余热回收装置的换热管道内的冷却水吸收热量后汽化，之后经过汽水分离获得压强为0.4～0.5MPa的饱和水蒸汽，返回所述粒化器作为流体用于粒化所述熔渣。
根据本发明的另一实施方式提供一种带有高速蒸汽喷嘴的高炉熔渣粒化装置的高炉熔渣粒化方法，通过水泵给进入管道的水加压，然后进入换热器内，来自余热回收管道的热源使换热器内的水温度升高，水处于高于大气压且高于常压下沸点温度的高温高压状态，经过喷嘴喷出后在常压下瞬间气化，形成含有蒸汽的高速射流(例如喷射速度为90～110m/s)冲击从渣流槽流出的熔渣，高速射流将熔渣冷却，并破碎成小颗粒落入熔渣粒化本体的底部；喷嘴喷出的混合射流冲击熔渣后全部变成蒸汽从所述装置上方流出作为余热资源待后续利用。
优选地，通过水泵给进入管道的水加压，管道内压强升至0.1～1MPa；来自余热回收管道的热能使换热器内的水温度升高至100～182℃。
本发明的又一实施方式提供一种气水混合的卧式熔渣粒化工艺，其特征是，采用由气体喷嘴组成的空气喷嘴阵列组件提供的高速气流对下落的熔渣进行破碎，得到熔渣颗粒；同时，采用成排的气液双流体喷嘴对所述熔渣颗粒进行水雾喷吹，使所述熔渣颗粒快速降温，并给所述熔渣颗粒施加一个辅助推动力，使其更准确地落入后部的渣粒收集段。
优选地，上述高速气流的速度为90～110m/s。
本发明的第二方面提供一种熔渣粒化装置，包括：
粒化机构，用于粒化熔渣获得破碎的熔渣颗粒；
冷却机构，用于冷却所述熔渣颗粒获得粒化渣。
具体地，上述熔渣粒化装置可以以下方式设置。
根据本发明的一种实施方式提供一种实施熔渣余热回收耦合利用方法的装置。具体地，本实施方式提供用于高炉熔渣余热回收耦合利用方法的装置，包括：
导流罩，其为一筒体结构；优选其横截面呈矩形，长宽比为2:1～5:1；更优选，所述导流罩的进口端安装有在线称量装置；
粒化器，其出口端连接导流罩的进口端；
旋流器，其侧壁设有物料进口，底部设有物料出口；所述物料进口与所述导流罩的出口端相连，
溢流管，其下部竖直插置于旋流器内，溢流管内设置螺旋换热管；
第一汽水分离器，其上设冷却水进口、冷却水出口、蒸汽进口及蒸汽出口；所述冷却水进口连接冷却水管路，所述冷却水出口通过管道及水泵连接所述溢流管内的螺旋换热管的进口端，所述蒸汽进口与所述溢流管内的螺旋换热管的出口端连接，
余热回收装置，其壳体上设有进气口及出气口，内部设有换热管道，该进气口与所述溢流管的出口端相连；
第二汽水分离器，其上设冷却水进口、冷却水出口、蒸汽进口及蒸汽出口；该冷却水进口连接冷却水管路，冷却水出口通过管道及水泵与所述余热回收装置内换热管道的进口端连接，蒸汽进口通过管道与所述余热回收装置的换热管道的出口端连接，蒸汽出口通过管道与所述粒化器的进口端连接；
滚筒床，其为一筒体结构，内部设有换热管道，所述滚筒床的进口端与所述旋流器的物料出口相连，所述滚筒床的出口端与渣仓相连，所述滚筒床上设有一可带动其转动的驱动装置；
第三汽水分离器，其上设冷却水进口、冷却水出口、蒸汽进口及蒸汽出口；该冷却水进口连接冷却水管路，冷却水出口通过管道及水泵与所述滚筒床的换热管道的进口端连接，蒸汽进口与所述滚筒床的换热管道的出口端连接；
气流磨，其壳体上设有进料管、进气管和出气管，所述气流磨的进料管与渣仓相连，所述气流磨的出气管与所述余热回收装置的进气口相连；
过热蒸汽发生器，其壳体上设有进气管道和出气管道，所述过热蒸汽发生器的进气管道与所述第一汽水分离器的蒸汽出口及所述第三汽水分离器的蒸汽出口相连，所述过热蒸汽发生器的出气管道与所述气流磨的进气管相连。
优选地，上述渣仓上设有振动器。
根据本发明的另一实施方式，提供一种带有高速蒸汽喷嘴的高炉熔渣粒化装置，包括：
熔渣粒化本体，为一箱体结构，其上部一侧设供熔渣进入的渣流槽，熔渣粒化本体顶部设有蒸汽流出通道；
蒸汽喷雾机构，包括沿管道依次设置的第一控制阀、水泵、第二控制阀、压力表、换热器、温度计和喷嘴；所述管道的进口端接水源；所述喷嘴设置于所述熔渣粒化本体设有渣流槽一侧的侧壁，且所述喷嘴的轴向与渣流槽的轴向成一夹角，喷嘴的出口方向正对渣流槽流出的熔渣；
所述换热器上设余热回收管道和换热流体流出管道；其中，所述余热回收管道上安装有阀门。
优选地，所述喷嘴的轴向与所述渣流槽的轴向成30～60°夹角。
本实施方式的带有高速蒸汽喷嘴的高炉熔渣粒化装置的高炉熔渣处理工艺，通过水泵给进入管道的水加压，然后进入换热器内，来自余热资源回收管道的热源使换热器内的水温度升高，水处于高于外界大气压且高于常压下沸点温度的高温高压状态，然后再经过喷嘴喷出，高温高压的水喷出后在常压下瞬间气化形成蒸汽，经喷嘴喷出后形成含有蒸汽的高速射流冲击(例如喷射速度为90～110m/s)从渣流槽流出的高温熔融液态熔渣，高流速的射流将液态熔渣冷却，并破碎成小颗粒落入熔渣粒化本体底部；喷嘴喷出的混合射流经过冲击高温熔渣全部生成蒸汽从装置上方流出作为余热回收资源。
优选地，所述第一控制阀为电液闸阀。
优选地，通过水泵给进入管道的水加压，管内压强达0.1～1MPa；来自余热资源回收管道的热源使换热器内的水温度升高，水温为100～182℃。
根据本发明的又一实施方式提供一种用于上述气水混合的卧式熔渣粒化工艺的装置，包括：
熔渣粒化本体，为箱体结构，其顶部设有渣流入口；
高速空气喷射机构，包括：
压缩机、储气罐、连接储气罐的输气管道及连接输气管道一端的空气喷嘴阵列组件；与储气罐的出口端相连的输气管道上依次设置第一控制阀及流量计；
所述储气罐上设有压力表、进气管道及进气阀；
所述空气喷嘴阵列组件包括多个气流喷嘴及相应的支流管道，所述支流管道与所述输气管道相连；所述气流喷嘴设置于所述熔渣粒化本体的一侧壁上部；
喷雾机构，包括：沿输水管道依次设置的第二控制阀、水泵、第三控制阀、压力表、流量计和多个气液双流体喷嘴；所述输水管道的进口端与水源相连；所述气液双流体喷嘴设置于所述熔渣粒化本体的内上部及底部，且，所述气液双流体喷嘴通过连接管道与所述输气管道及输水管道相连。
优选地，所述空气喷嘴阵列组件的轴向与水平方向成0～20°夹角。
优选地，所述空气喷嘴阵列组件的宽度大于所述渣流入口的宽度。
优选地，所述第二控制阀为电液闸阀。
优选地，所述熔渣粒化本体为半封闭的，其后部设有渣粒收集段。
优选地，所述气流喷嘴为超音速喷嘴。
在上述的气水混合的卧式熔渣粒化工艺的装置中：
高速空气喷射机构提供熔渣破碎粒化的主要动力，雾化机构提供熔渣破碎粒化的主要换热介质，熔渣粒化过程在熔渣粒化本体内进行。
压缩机给气体加压将气体送入储气罐，通过储气罐提供稳定压强的气体给空气喷嘴阵列组件，然后将高速气流(例如喷射速度为90～110m/s)射入熔渣粒化本体内对熔渣进行破碎；同时，水泵给输水管道内水加压，然后与气体管道喷出的气流共同经气液双流体喷嘴喷出，喷出后雾滴颗粒冲击粒化后的熔渣颗粒，将熔渣颗粒快速降温并冷却成稳定小颗粒。
根据本发明的又一实施方式提供一种利用气体喷嘴阵列将高炉熔渣粒化的装置，包括：
熔渣粒化本体，为箱体结构，其顶部设渣流入口、蒸汽流出通道；
高速空气喷射机构，包括：
压缩机、储气罐、连接储气罐的输气管道及连接输气管道一端的喷嘴阵列；储气罐出口端的输气管道中依次设置第一控制阀及流量计；所述储气罐上设压力表、进气管道及进气阀；
所述喷嘴阵列包括多个喷嘴及相应的支流管道，各支流管道分别与所述输气管道相连；所述喷嘴设置于所述熔渣粒化本体的一侧壁上。
优选地，上述装置还包括：
喷嘴雾化机构，包括沿输水管道依次设置的第二控制阀、水泵、第三控制阀、压力表、流量计和多个雾化喷嘴；所述输水管道进口端与水源相连；所述雾化喷嘴设置于所述熔渣粒化本体的内底部，且至少排布为两排，水雾喷出方向正对自所述渣流入口流入的熔渣。
优选地，上述装置还包括余热回收系统，其包括：
换热箱体，其一侧壁上部设有与所述熔渣粒化本体的出料口相连的进料口；所述换热箱体的顶部设有换热气流出口；换热箱体内沿高度方向设有多个开孔床板；所述换热箱体的底部设有熔渣颗粒出口；
气体喷嘴阵列，设置于所述换热箱体的内底部、开孔床板的下方，所述气体喷嘴阵列中的气体喷嘴与所述开孔床板相对设置；或者，
所述余热回收系统采用旋风分离器。
优选地，所述开孔床板在换热箱体内沿竖直方向呈Z字形布置。
优选地，所述旋风分离器包括分离器本体，所述分离器本体的上部一侧设有与所述熔渣粒化本体的出料口连通的气固介质入口；所述分离器本体的顶部设有空气出口，所述分离器本体的底部设有灰斗。
优选地，所述喷嘴阵列中的喷嘴为选自超音速喷嘴、雾化喷嘴或气液双流体喷嘴中的一种以上；优选地，所述喷嘴阵列中喷嘴的轴向与所述熔渣粒化本体的侧壁互相垂直。
优选地，所述喷嘴阵列中喷嘴的排布方式为多行多列，或呈弧形排列；优选地，相邻两行的喷嘴在竖直方向上错开；更优选地，喷嘴数量沿竖直方向逐步减少或增加。
优选地，所述喷嘴阵列中的喷嘴为气液双流体喷嘴；相应地，所述装置还设有喷嘴供水机构，所述喷嘴供水机构包括沿输水管道依次设置的第四控制阀、水泵、第五控制阀、压力表、流量计；所述输水管道的进口端与水源相连，出口端与气液双流体喷嘴的进口端相连。
压缩机将空气加压后送入储气罐，由储气罐将空气通过管道和(超音速)喷嘴喷射到熔渣粒化本体内进行粒化，液态熔渣在粒化本体内粒化；超音速喷嘴喷出的高速气流(例如喷射速度为90～110m/s或以上)冲击液态熔渣将其破碎，并对所粒化的渣粒迅速换热降温，便于其快速成渣。
本实施方式中的装置相比于传统风淬和水淬工艺，采用超音速喷嘴阵列的方式使渣处理能力进一步提高，雾滴的喷射提升渣粒换热效果，减少了水资源的浪费。
根据本发明的又一实施方式，提供一种可清理落渣的气雾熔渣粒化的装置，包括：
熔渣粒化本体，为箱体结构，其顶部设有渣流入口，其尾部设有渣粒收集段；
气体喷嘴阵列，设置于所述熔渣粒化本体的一侧壁上；
雾化喷嘴阵列，设置于所述熔渣粒化本体的内底部，气雾喷出方向对应从所述渣流入口流入的熔渣；
清理落渣喷嘴，设置于所述熔渣粒化本体的内底部，所述清理落渣喷嘴的出口对着所述熔渣粒化本体的内底部及所述渣粒收集段方向。
优选地，所述气体喷嘴阵列的轴向与熔渣粒化本体的侧壁相互垂直。
优选地，所述气体喷嘴阵列的出口两侧分别设有挡板，所述挡板的外侧分别安装有液体/雾化喷嘴。
优选地，所述清理落渣喷嘴为选自水雾化喷嘴、蒸汽雾化喷嘴、高速气流喷嘴或气液双流体喷嘴中的一种以上。
优选地，上述装置还设有：
高速空气喷射机构，其包括，压缩机、储气罐、连接储气罐的输气管道及连接输气管道一端的气体喷嘴阵列；储气罐的出口端的输气管道上依次设置第一控制阀及流量计；所述储气罐上设有压力表、进气管道及进气阀；所述喷嘴阵列包括若干喷嘴及相应的支流管道，支流管道接入输气管道；所述清理落渣喷嘴通过连接管道及一阀门连接至所述输气管道；
喷嘴雾化机构，包括沿输水管道依次设置的第二控制阀、水泵、第三控制阀、压力表、流量计；所述输水管道的进口端与水源相连，其出口端连接至所述雾化喷嘴阵列。
优选地，所述雾化喷嘴阵列中的喷嘴为气液双流体喷嘴，其进口端分别连接输气管道和输水管道。
优选地，所述熔渣粒化本体的顶部设有至少两个渣流入口。
本实施方式的可清理落渣的气雾熔渣粒化的装置，包括熔渣粒化系统和渣粒收集系统。
熔渣粒化系统分为两部分，一部分为气体喷嘴阵列组件，其喷射出高速气流(例如喷射速度为90～110m/s)用于粒化，另一部分为雾化喷嘴阵列，其喷出的雾滴颗粒在熔渣粒化装置内用于粒化。气体喷嘴阵列喷出的高速气流冲击液态熔渣将其破碎，雾化喷嘴阵列喷出的高密度雾滴颗粒使破碎的熔渣迅速换热降温，便于其快速成渣。
在熔渣粒化本体的底部设置清理落渣喷嘴，其可将落到底部的渣粒进行降温和吹扫到尾部渣粒收集段，以防止熔渣颗粒粘壁并迅速落入渣粒收集段。
相比于传统风淬和水淬工艺，本发明采用气体喷嘴阵列使渣处理能力进一步提高，同时采用雾化喷嘴阵列喷射气雾，提升了渣粒换热效果，减少了水资源的浪费，并且底部吹扫落渣的喷嘴可使熔渣颗粒防止粘壁迅速落入收集段。
根据本发明的又一实施方式提供一种利用雾化喷嘴将熔渣快速冷却的装置，包括：
熔渣粒化本体，为箱体结构，其顶部设有渣流入口；
气体喷嘴阵列，设置于所述熔渣粒化本体的一侧壁上，所述气体喷嘴阵列中气体喷嘴的轴向与所述熔渣粒化本体的侧壁相互垂直；
流场优化喷嘴阵列，设置于所述熔渣粒化本体的内上部，近所述渣流入口处；
清渣喷嘴阵列，设置于所述熔渣粒化本体的内下部或底部；
雾化喷嘴阵列，设置于所述熔渣粒化本体内，在所述熔渣粒化本体的内壁上环绕渣流的径向布置，所述雾化喷嘴阵列中雾化喷嘴的轴向与所述气体喷嘴的轴向相互垂直。
优选地，所述熔渣粒化本体的尾部设有渣粒收集段。
优选地，所述流场优化喷嘴阵列的喷嘴为气体喷嘴或气液双流体喷嘴。
优选地，所述清渣喷嘴阵列的喷嘴为气体喷嘴。
优选地，所述雾化喷嘴阵列的喷嘴为水雾化喷嘴。
本实施方式的装置相比于传统风淬和水淬工艺，采用喷嘴阵列的方式使渣处理能力进一步提高，雾滴的喷射提升了渣粒换热效果，减少了水资源的浪费，使熔渣余热得到充分回收。
根据本发明的又一实施方式提供一种用于高炉熔渣粒化的水雾粒化装置，包括：
机架，为框架结构；
水喷嘴阵列组件，包括，
本体，为箱体结构，设置于所述机架中部；其内依次间隔设置有均流板、导流板；
所述本体的后端与水源相连；
水喷嘴阵列，均布于所述本体的前端面；
气液双流体喷嘴组件，包括，
气液双流体喷嘴，平行设置于所述水喷嘴阵列的两侧，并固定于所述机架上；
气体管道、输水管道，固定于机架上，并与所述气液双流体喷嘴相连。
优选地，所述气液双流体喷嘴平行设置于所述水喷嘴阵列的两侧。
附图说明
图1示出本发明一实施例的熔渣粒化装置的结构示意图；
图2示出本发明另一实施例的熔渣粒化装置的结构示意图；
图3示出本发明又一实施例的熔渣粒化装置的结构示意图；
图4示出本发明又一实施例的熔渣粒化装置的结构示意图；
图5示出本发明又一实施例中气体喷嘴阵列组件的结构示意图；
图6示出图4中的装置采用不同气体喷嘴阵列组件在不同倾角时渣粒的飞行轨迹；
图7示出图4中的装置采用的气体喷嘴阵列组件倾角过大时渣粒的飞行轨迹；
图8示出本发明又一实施例的熔渣粒化装置的结构示意图；
图9示出本发明又一实施例的熔渣粒化装置中喷嘴阵列的排布示意图；
图10示出本发明又一实施例的熔渣粒化装置中喷嘴阵列的排布示意图；
图11示出本发明又一实施例的熔渣粒化装置中喷嘴阵列的排布示意图；
图12示出本发明又一实施例的熔渣粒化装置的结构示意图；
图13示出本发明又一实施例的熔渣粒化装置中喷嘴阵列的俯视图；
图14示出本发明又一实施例的熔渣粒化装置的结构示意图；
图15示出本发明又一实施例的熔渣粒化装置的结构示意图；
图16示出本发明又一实施例的熔渣粒化装置的结构示意图；
图17示出本发明又一实施例的熔渣粒化装置的结构示意图；
图18示出本发明又一实施例的熔渣粒化装置中清理落渣喷嘴的排布示意图；
图19示出本发明又一实施例的熔渣粒化装置的结构示意图；
图20示出本发明又一实施例的熔渣粒化装置的结构示意图；
图21示出本发明又一实施例的熔渣粒化装置中气体喷嘴阵列的俯视图；
图22示出本发明又一实施例的熔渣粒化装置的气体喷嘴阵列中喷嘴的结构示意图；
图23示出本发明又一实施例的熔渣粒化装置中气体喷嘴阵列的另一结构示意图；
图24示出本发明又一实施例的熔渣粒化装置的结构示意图；
图25示出图24中雾化喷嘴的排布示意图；
图26示出本发明又一实施例的熔渣粒化装置的结构示意图；
图27示出图26中熔渣粒化装置的侧视图。
具体实施方式
以下由特定的具体实施例说明本发明的实施方式，本领域技术人员可由本说明书所揭示的内容轻易地了解本发明的其他优点及功效。虽然本发明的描述将结合较佳实施例一起介绍，但这并不代表此发明的特征仅限于该实施方式。恰恰相反，结合实施方式作发明介绍的目的是为了覆盖基于本发明的权利要求而有可能延伸出的其它选择或改造。为了提供对本发明的深度了解，以下描述中将包含许多具体的细节。本发明也可以不使用这些细节 实施。此外，为了避免混乱或模糊本发明的重点，有些具体细节将在描述中被省略。需要说明的是，在不冲突的情况下，本发明中的实施例及实施例中的特征可以相互组合。
应注意的是，在本说明书中，相似的标号和字母在下面的附图中表示类似项，因此，一旦某一项在一个附图中被定义，则在随后的附图中不需要对其进行进一步定义和解释。
在本实施例的描述中，需要说明的是，术语“上”、“下”、“内”、“底”等指示的方位或位置关系为基于附图所示的方位或位置关系，或者是该发明产品使用时惯常摆放的方位或位置关系，仅是为了便于描述本发明和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本发明的限制。
术语“第一”、“第二”等仅用于区分描述，而不能理解为指示或暗示相对重要性。
在本实施例的描述中，还需要说明的是，除非另有明确的规定和限定，术语“设置”、“相连”、“连接”应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或一体地连接；可以是机械连接，也可以是电连接；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通。对于本领域的普通技术人员而言，可以具体情况理解上述术语在本实施例中的具体含义。
为使本发明的目的、技术方案和优点更加清楚，下面将结合附图对本发明的实施方式作进一步地详细描述。
首先，本发明提供熔渣粒化方法，包括破碎熔渣得到熔渣颗粒，然后对熔渣颗粒进行冷却，并收集由此获得的粒化渣。
其次，本发明提供熔渣粒化装置，包括：粒化机构，用于粒化熔渣获得破碎的熔渣颗粒；以及冷却机构，用于冷却熔渣颗粒获得粒化渣。
根据本发明的一种实施方式提供一种熔渣余热回收耦合利用的方法，其中，熔渣通过射流粒化获得表面固化的颗粒和蒸汽，随后表面固化的颗粒在旋流场中进行冷却，获得固态渣粒。采用本实施方式提供的方法，在实现高炉熔渣的快速、安全粒化的同时，也实现高炉熔渣显热的多级回收和同级利用，从而大大提高了高温熔渣余热回收利用率。通过回收蒸汽作动力，直接将粒化渣磨成超细矿渣微粉，实现高炉熔渣的高值产品化。
参见图1，其显示了实施根据本实施方式的熔渣粒化方法的装置。具体地，本实施方式提供了一种用于上述熔渣余热回收耦合利用方法的装置，包括：
导流罩16，其为一筒体结构；优选其横截面呈矩形，长宽比为2:1～5:1；更优选，所述导流罩16的进口端安装有在线称量装置14；
粒化器15，其出口端连接导流罩16的进口端；
旋流器17，其侧壁设有物料进口，底部设有物料出口；所述物料进口与所述导流罩16的出口端相连，
溢流管，其下部竖直插置于旋流器17内，溢流管内设置螺旋换热管；
第一汽水分离器127，其上设冷却水进口、冷却水出口、蒸汽进口及蒸汽出口；所述冷却水进口连接冷却水管路，所述冷却水出口通过管道及水泵128连接所述溢流管内的螺旋换热管的进口端，所述蒸汽进口与所述溢流管内的螺旋换热管的出口端连接，
余热回收装置123，其壳体上设有进气口及出气口，内部设有换热管道，该进气口与所述溢流管的出口端相连；
第二汽水分离器125，其上设冷却水进口、冷却水出口、蒸汽进口及蒸汽出口；该冷却水进口连接冷却水管路，冷却水出口通过管道及水泵124与余热回收装置123的换热管道的进口端连接，蒸汽进口通过管道与余热回收装置123的换热管道的出口端连接，蒸汽出口通过管道与粒化器17的进口端连接；
滚筒床18，其为一筒体结构，内部设有换热管道，所述滚筒床18的进口端与所述旋流器17的物料出口相连，所述滚筒床18的出口端与渣仓112相连，所述滚筒床上设有一可带动其转动的驱动装置；
第三汽水分离器19，其上设冷却水进口、冷却水出口、蒸汽进口及蒸汽出口；该冷却水进口连接冷却水管路，冷却水出口通过管道及水泵110与所述滚筒床的换热管道的进口端连接，蒸汽进口与所述滚筒床的换热管道的出口端连接；
气流磨117，其壳体上设有进料管、进气管和出气管，所述气流磨117进料管与渣仓112相连，所述气流磨117的出气管与余热回收装置的123进气口相连；
过热蒸汽发生器126，其壳体上设有进气管道和出气管道，过热蒸汽发生器126的进气管道与第一汽水分离器127的蒸汽出口及第三汽水分离器19的蒸汽出口相连，过热蒸汽发生器126的出气管道与气流磨117的进气管相连。
优选地，渣仓112上设有振动器113。
继续参考图1，上述熔渣余热回收耦合利用方法可按如下进行。具体地，熔渣余热回收耦合利用的方法包括如下步骤：
1)某钢厂一座容积为1250m3的高炉，出铁时，温度在1500℃左右的熔渣以平均约2.5t/min(最大出渣量5t/min)的出渣量进入主渣沟11，利用取渣器12将主渣沟11内的熔渣放入取渣沟13内，之后经过在线称量装置14流入导流罩16内，其中导流罩16的横截面为矩形，长300mm，宽100mm；进入导流罩16内的熔渣被从粒化器15喷出的气雾流 体冲击、破碎、粒化成粒径在5mm以内的颗粒熔滴，颗粒熔滴随气雾流体沿着导流罩16定向高速飞行，颗粒熔滴在形成和飞行过程中与气雾流体换热并得到快速冷却固化，例如冷却速率为20℃/秒以上，生成1000℃以下800℃以上的粒化渣(此时为仅表面固化的颗粒，芯部为熔融态)和约300℃(环境温度)的气流，此时粒径在2mm以内的颗粒的凝固率约为80％，实现了对熔渣的粒化和冷却固化；
2)渣气分离
上述粒化渣和气流从导流罩16内流出后直接进入旋流器17内，在离心力和重力共同作用下实现渣、气分离，分离后的粒化渣温度下降到700～800℃，从旋流器17的底部流出；
分离后的气流流经旋流器17和溢流管，经溢流管内的螺旋换热管的冷却水换热后温度降到150℃以下，从旋流器17和溢流管排出后进入余热回收装置123，与余热回收装置123内通有冷却水的换热管道接触换热进一步回收余热，形成温度为130℃以下的尾气；
余热回收装置123的换热管道内的冷却水吸收热量后汽化，之后经过第二汽水分离器125汽水分离获得压强在约0.5MPa的饱和水蒸汽，返回所述粒化器15作为气雾流体用于粒化上述熔渣；
螺旋换热管内的冷却水吸收热量汽化，随后经过第一汽水分离器127汽水分离生成压强为1.2～1.6MPa、温度在188～201℃的饱和蒸汽，该饱和蒸汽进入过热蒸汽发生器126，补热后获得压强为1.2～1.6MPa、温度在250～350℃的过热蒸汽；在上述过程中，利用天然气或钢铁冶炼过程中产生的混合煤气对进入过热蒸汽发生器126中的饱和蒸汽进行补热；
3)自旋流器17的底部流出的粒化渣进入滚筒床18，在滚筒床18内与通有冷却水的换热管道接触换热，滚筒床18在驱动机构的作用下沿设定方向低速旋转，转速控制在3rpm，粒化渣随滚筒床18的转动被筒内推进机构缓慢推进，温度降到180℃以下后排出滚筒床18，依次经过溜槽及斗提机111送入渣仓112储存；渣仓112上安装有振动器113对渣仓112进行振动，防止粒化渣在渣仓内堵塞渣仓出口、架桥、起拱；
滚筒床8的换热管道内的冷却水吸收热量后汽化，经过第三汽水分离器19汽水分离后生成压强为1.2～1.6MPa、温度在188～201℃饱和蒸汽，饱和蒸汽进入过热蒸汽发生器126，利用天然气或钢铁冶炼过程中产生的混合煤气进行补热，补热后获得压强为1.2～1.6MPa、温度在250～350℃的过热蒸汽；
4)渣仓112内的粒化渣经过出渣阀114、输送机构116输送进入气流磨117，利用步骤2)和步骤3)获得的过热蒸汽冲击、研磨成超细微粉，超细微粉经过收粉装置118收集后作为高品质产品直接销售；
过热蒸汽压强降为常压，温度降至150℃以下，随后进入余热回收装置123，与余热回收装置123内通有冷却水的换热管道接触换热进一步回收余热，形成温度为约130℃的尾气；
所述余热回收装置123的换热管道内的冷却水吸收热量后汽化，之后经过第二汽水分离器125汽水分离获得压强为约0.4MPa的饱和水蒸汽，返回粒化器15作为气雾流体用于粒化熔渣。
或者，渣仓112内粒化渣由卡车115运送至矿渣微粉生产线，直接研磨成比表面积为约420m2/kg的矿渣微粉。
生产过程中产生的废气一并送入尾气净化装置120，经过除尘、脱硫处理达到相关排放标准后由风机121抽出，经烟囱122排放。循环泵119将脱硫除尘液循环泵入尾气净化装置120内，当循环液浓度达到一定值(取决于实际处理场景)时，部分外排，从外部补充新鲜碱液，以维持正常、高效的脱硫、除尘效果。
根据本发明的另一实施方式，利用图1所示的装置进行的熔渣余热回收耦合利用方法可按如下进行。熔渣余热回收耦合利用的方法包括如下步骤：
1)某钢厂一座容积为2500m3的高炉，出铁时，温度在约1500℃的熔渣以平均约3.0t/min(最大出渣量6t/min)的出渣量进入主渣沟11，利用取渣器12将主渣沟11内的熔渣放入取渣沟内，之后经过在线称量装置流入导流罩内，其中导流罩16的横截面为矩形，长400mm，宽100mm；进入导流罩16内的熔渣被从粒化器15喷出的气雾流体冲击、破碎、粒化成粒径在5mm以内的颗粒熔滴，颗粒熔滴随气雾流体沿着导流罩16定向高速飞行，颗粒熔滴在形成和飞行过程中与气雾流体换热并得到快速冷却固化，生成1000℃以下750℃以上的粒化渣(此时为仅表面固化的颗粒，芯部为熔融态)和约300℃(环境温度)的气流，此时粒径在2mm以内的颗粒的凝固率约为90％，实现了对熔渣的粒化和冷却固化；
2)渣气分离
上述粒化渣和气流从导流罩16内流出后直接进入旋流器17内，在离心力和重力共同作用下实现渣、气分离，分离后的粒化渣温度下降到750℃以下，从旋流器17的底部流出；
分离后的气流流经旋流器17和溢流管，经溢流管内的螺旋换热管的冷却水换热后温度降到200℃以下，从旋流器17和溢流管排出后进入余热回收装置123，与余热回收装置123内通有冷却水的换热管道接触换热进一步回收余热，形成温度为140℃以下的尾气；
余热回收装置123的换热管道内的冷却水吸收热量后汽化，之后经过第二汽水分离器汽水分离获得压强为约0.45MPa的饱和水蒸汽，返回粒化器15作为气雾流体用于粒化上述熔渣；
螺旋换热管内的冷却水吸收热量汽化，随后经过第一汽水分离器汽水分离生成压强为约1.4MPa、温度为约190℃的饱和蒸汽，该饱和蒸汽进入过热蒸汽发生器126，补热后获得压强为约1.4MPa、温度为约300℃的过热蒸汽；在上述过程中，利用天然气或钢铁冶炼过程中产生的混合煤气对进入过热蒸汽发生器126中的饱和蒸汽进行补热；
3)自旋流器17的底部流出的粒化渣进入滚筒床18，在滚筒床18内与通有冷却水的换热管道接触换热，滚筒床18在驱动机构的作用下沿设定方向低速旋转，转速控制在3rpm，粒化渣随滚筒床18的转动被筒内推进机构缓慢推进，温度降到180℃以下后排出滚筒床18，依次经过溜槽及斗提机111送入渣仓112储存；渣仓112上安装有振动器113对渣仓112进行振动，防止粒化渣在渣仓112内堵塞渣仓出口、架桥、起拱；
滚筒床18的换热管道内的冷却水吸收热量后汽化，冷却水利用增压泵强制循环，经过第三汽水分离器19汽水分离后生成压强为约1.4MPa、温度为约190℃的饱和蒸汽，该饱和蒸汽进入过热蒸汽发生器126，利用天然气或钢铁冶炼过程中产生的混合煤气进行补热，补热后获得压强为约1.4MPa、温度为约300℃的过热蒸汽；
4)渣仓112内的粒化渣经过出渣阀114、输送机构116输送进入气流磨117，利用步骤2)和步骤3)获得的过热蒸汽冲击、研磨成超细微粉，超细微粉经过收粉装置118收集后作为高品质产品直接销售；
过热蒸汽压强降为常压，温度降至200℃以下，随后进入余热回收装置123，与余热回收装置123内通有冷却水的换热管道接触换热进一步回收余热，形成温度为约140℃的尾气；
所述余热回收装置123的换热管道内的冷却水吸收热量后汽化，之后经过第二汽水分离器汽水分离获得压强为约0.45MPa的饱和水蒸汽，返回粒化器15作为气雾流体用于粒化熔渣。
或者，渣仓112内粒化渣由卡车115运送至矿渣微粉生产线，直接研磨成比表面积为约420m2/kg的矿渣微粉。
生产过程中产生的废气一并送入尾气净化装置120，经过除尘、脱硫处理达到相关排放标准后由风机121抽出，经烟囱122排放。循环泵119将脱硫除尘液循环泵入尾气净化 装置120内，当循环液浓度达到一定值(取决于实际处理场景)时，部分外排，从外部补充新鲜碱液，以维持正常、高效的脱硫、除尘效果。
根据本发明的又一实施方式，利用图1所示的装置进行的熔渣余热回收耦合利用方法可按如下进行。熔渣余热回收耦合利用的方法包括如下步骤：
1)某钢厂一座容积为1250m3的高炉，出铁时，温度在约1500℃的熔渣以平均约3.0t/min(最大出渣量6t/min)的出渣量进入主渣沟11，利用取渣器12将主渣沟11内的熔渣放入取渣沟13内，之后经过在线称量装置14流入导流罩16内，其中导流罩16的横截面为矩形，长400mm，宽100mm；进入导流罩16内的熔渣被从粒化器15喷出的气雾流体冲击、破碎、粒化成粒径在5mm以内的颗粒熔滴，颗粒熔滴随气雾流体沿着导流罩16定向高速飞行(例如飞行速度为10m/s以上，根据实际情况测定)，颗粒熔滴在形成和飞行过程中与气雾流体换热并得到快速冷却固化，生成1000℃以下800℃以上的粒化渣(此时为仅表面固化的颗粒，芯部为熔融态)和约300℃(环境温度)的气流，此时粒径在2mm以内的颗粒的凝固率为约85％，实现了对熔渣的粒化和冷却固化；
2)渣气分离
上述粒化渣和气流从导流罩16内流出后直接进入旋流器17内，在离心力和重力共同作用下实现渣、气分离，分离后的粒化渣温度下降到800℃以下，从旋流器17的底部流出；
分离后的气流流经旋流器17和溢流管，经溢流管内的螺旋换热管的冷却水换热后温度降到300℃以下，从旋流器17和溢流管排出后进入余热回收装置123，与余热回收装置123内通有冷却水的换热管道接触换热进一步回收余热，形成温度为150℃以下的尾气；
余热回收装置123的换热管道内的冷却水吸收热量后汽化，之后经过第二汽水分离器汽水分离获得压强为约0.5MPa的饱和水蒸汽，返回粒化器15作为气雾流体用于粒化上述熔渣；
螺旋换热管内的冷却水吸收热量汽化，随后经过第一汽水分离器汽水分离生成压强为约1.6MPa、温度为约201℃的饱和蒸汽，该饱和蒸汽进入过热蒸汽发生器126，补热后获得压强为约1.6MPa、温度为约350℃的过热蒸汽；在上述过程中，利用天然气或钢铁冶炼过程中产生的混合煤气对进入过热蒸汽发生器126中的饱和蒸汽进行补热；
3)自旋流器17的底部流出的粒化渣进入滚筒床18，在滚筒床18内与通有冷却水的换热管道接触换热，滚筒床18在驱动机构的作用下沿设定方向低速旋转，转速控制在3rpm，粒化渣随滚筒床18的转动被筒内推进机构缓慢推进，温度降到180℃以下后排出滚筒床 18，依次经过溜槽及斗提机111送入渣仓112储存；渣仓112上安装有振动器113对渣仓112进行振动，防止粒化渣在渣仓112内堵塞渣仓出口、架桥、起拱；
滚筒床18的换热管道内的冷却水吸收热量后汽化，冷却水利用增压泵强制循环，经过第三汽水分离器19汽水分离后生成压强为约1.6MPa、温度为约201℃的饱和蒸汽，该饱和蒸汽进入过热蒸汽发生器126，利用天然气或钢铁冶炼过程中产生的混合煤气进行补热，补热后获得压强为约1.6MPa、温度为约350℃的过热蒸汽；
4)渣仓112内的粒化渣经过出渣阀114、输送机构116输送进入气流磨117，利用步骤2)和步骤3)获得的过热蒸汽冲击、研磨成超细微粉，超细微粉经过收粉装置118收集后作为高品质产品直接销售；
过热蒸汽压强降为常压，温度降至250℃以下，随后进入余热回收装置123，与余热回收装置123内通有冷却水的换热管道接触换热进一步回收余热，形成温度为约150℃的尾气；
所述余热回收装置123的换热管道内的冷却水吸收热量后汽化，之后经过第二汽水分离器汽水分离获得压强为约0.5MPa的饱和水蒸汽，返回粒化器15作为气雾流体用于粒化熔渣。
或者，渣仓112内粒化渣由卡车115运送至矿渣微粉生产线，直接研磨成比表面积为约420m2/kg的矿渣微粉。
生产过程中产生的废气一并送入尾气净化装置120，经过除尘、脱硫处理达到相关排放标准后由风机121抽出，经烟囱122排放。循环泵119将脱硫除尘液循环泵入尾气净化装置120内，当循环液浓度达到一定值(取决于实际处理场景)时，部分外排，从外部补充新鲜碱液，以维持正常、高效的脱硫、除尘效果。
本实施方式利用粒化器喷出的高速气雾流体冲击、破碎、粒化高炉熔渣，高速气雾流体的流量可控，其流量随在线称量装置所称量的高炉熔渣的多少而变化，高炉熔渣流量小，气雾流体流量适当减小，熔渣流量增大，气雾流体的流量随之增加。气雾流体的最大流量能够保证高炉熔渣最大量时高炉熔渣的安全粒化。
旋流器和滚筒床盘管内的冷却水吸收热量后形成1.2-1.6MPa的饱和蒸汽，之后被送至过热蒸汽发生器，利用天然气或钢铁冶炼过程中产生的混合煤气进行适当补热，饱和蒸汽被加热成1.2-1.6MPa、温度在250-350℃的过热蒸汽，形成的过热蒸汽直接送气流磨作为粒渣粉化的动力。过热蒸汽在气流磨内膨胀做功后品质下降，压强降为常压，温度降至150-250℃，这部分气体进入余热回收装置，经过管壳式间壁换热，制备出0.4-0.5MPa饱 和水蒸汽，形成的饱和水蒸汽可以直接送回粒化器，作为高炉熔渣粒化的气雾流体。气雾流体与高炉熔渣作用后经渣气分离后进入余热回收装置处理后可以重复利用。本实施方式可以实现高炉熔渣显热的梯度回收，并将回收的热量就近同级利用。
上述熔渣余热回收耦合利用的方法的装置，利用水淬和风碎相结合的气雾粒化方式，将高炉熔渣的显热逐级回收，并将回收的热量就近直接利用在高炉熔渣的处理过程中，不仅能实现高炉熔渣的安全、快速粒化，而且能提高回收后余热的利用率，避免常规方式将高炉熔渣显热回收后利用效率低下的问题。
在本实施方式中，水蒸气可以循环使用，避免了水资源的浪费，降低了高炉熔渣的粒化成本，处理过程对环境友好，实现高炉熔渣安全、快速粒化，获得高品质产品化的粒化渣，能够实现高炉熔渣的高价值资源化和高炉熔渣显热的高效回收利用。
根据本发明的又一实施方式提供一种带有高速蒸汽喷嘴的高炉熔渣粒化装置及工艺，兼具水淬和风淬粒化技术的优点，利用带水雾的高速蒸汽来冷却及粒化熔渣，既可适当减少新水消耗量以降低成本，还能兼顾熔渣冷却速率以利于固态渣的玻璃体形成，并且该装置可充分利用熔渣的余热，以减少能量的损耗；具有冷却速率较快，熔渣破碎效果好，耗能低等优点。
具体地，参见图2，其显示了实施根据本实施方式的熔渣粒化方法的装置。具体地，本实施方式提供了一种带有高速蒸汽喷嘴的高炉熔渣粒化装置，包括：熔渣粒化本体21，为一箱体结构，其上部一侧设供熔渣2100进入的渣流槽211，熔渣粒化本体21顶部设有蒸汽流出通道212；
蒸汽喷雾机构22，包括沿管道220依次设置的第一控制阀F21、水泵221、第二控制阀F22、压力表222、换热器223、温度计224和喷嘴225；该管道220的进口端接水源2200；喷嘴225设置于熔渣粒化本体21设有渣流槽211一侧的侧壁上，且，喷嘴225的轴向与渣流槽211的轴向成一角度，喷嘴225的出口方向正对从渣流槽211流出的熔渣；
换热器223上设余热回收管道23和换热流体流出管道24；其中，余热回收管道23上安装有阀门F23。
优选地，第一控制阀F21为电液闸阀。
优选地，喷嘴225的轴向与渣流槽211的轴向成30～60°夹角。
使用上述带有高速蒸汽喷嘴的熔渣粒化装置的熔渣粒化方法，按如下实施：通过水泵给进入管道的水加压，然后进入换热器内，来自余热资源回收管道的热源使换热器内的水温度升高，水处于高于大气压且高于常压下沸点温度的状态，经过喷嘴喷出后在常压下瞬 间气化形成含有蒸汽的高速射流(例如喷射速度为90～110m/s)冲击从渣流槽流出的熔渣，高速射流将熔渣冷却，并破碎成小颗粒落入熔渣粒化本体的底部；喷嘴喷出的混合射流冲击熔渣后全部变成蒸汽从上述装置上方流出作为余热资源待后续利用。
优选地，通过水泵给进入管道的水加压，管道内压强升至0.1～1MPa；来自余热回收管道的热能使换热器内的水温度升高至100～182℃。
与现有技术相比，采用根据本实施方式的熔渣粒化方法和装置的优点在于：
喷嘴喷出的高速射流破碎高炉熔渣进行换热后全部生成水蒸气，水资源消耗比传统湿法工艺大幅度减少，减少了水污染，同时减少了有害气体的排放，且不需要对冷却后的高炉熔渣进行干燥处理；
熔渣显热经过与喷嘴喷出的射流进行换热，生成的高温水蒸气的热焓要高于传统风淬工艺生成的热空气的热焓，使熔渣显热的回收效率更高，进行余热回收更具有潜力；
相比于风淬工艺，根据本实施方式的装置以较少的能源消耗使管道内流体具有更大的压强，成本低，且噪音污染更小，由于换热介质是水，高温熔渣的冷却速率也比风淬的冷却速率要快，更加有利于玻璃体的形成，玻璃体质量越好、含量越高，高炉渣的回收利用率越高；
采用余热给管道加热的方式，形成蒸汽的能量全部来源于钢厂余热和废热，提高了能量的利用率；
由于管道内流动介质为水，液体相比于气体更容易获得高压，使其具有较大的打击动能。
根据本发明的一种实施方式提供一种气水混合的卧式熔渣粒化工艺及装置，利用气体喷嘴阵列组件喷出的高速气流冲击液态熔渣将其破碎，气液双流体喷嘴喷出的高密度雾滴颗粒对所粒化的渣粒迅速换热降温并辅助粒化，便于其快速成渣；以雾化的形式取代水淬直接喷水的形式，既可适当减少新水消耗量以降低成本，还能兼顾熔渣冷却速率以利于固态渣的玻璃体形成，并且该工艺可充分利用熔渣的余热，以减少能量的损耗；具有冷却速率较快，熔渣破碎效果好，耗能低等优点。
参见图3，其显示了实施根据本实施方式的熔渣粒化方法的装置。具体地，本实施方式提供了一种气水混合的卧式熔渣粒化工艺，其采用由气体喷嘴组成的空气喷嘴阵列组件提供的高速气流对下落的熔渣进行破碎，得到熔渣颗粒；同时，采用成排的气液双流体喷嘴对熔渣颗粒进行水雾喷吹，使熔渣颗粒快速降温，并给熔渣颗粒施加一个辅助推动力，使其更准确地落入后部的渣粒收集段。
优选地，上述高速气体喷嘴采用超音速喷嘴。
参见图3-图5，用于上述气水混合的卧式熔渣粒化工艺的装置，其包括：
熔渣粒化本体61，为箱体结构，其顶部设渣流入口611，其上方设渣溜槽612；
高速空气喷射机构62，包括：
压缩机621、储气罐622、连接储气罐622的输气管道620及连接输气管道620一端的空气喷嘴阵列组件623；与储气罐622的出口端相连的输气管道620上依次设置第一控制阀F61及流量计624；空气喷嘴阵列组件623包括多个气流喷嘴及相应的支流管道，支流管道与输气管道620相连；气流喷嘴设置于熔渣粒化本体61的一侧壁上部；所述高速气流喷嘴为超音速喷嘴；
储气罐622上设压力表625、进气管道626及进气阀6261；
空气喷嘴阵列组件623接入输气管道620；
喷雾机构63，包括：沿输水管道630依次设置的第二控制阀F62、水泵631、第三控制阀F63、压力表632、流量计633和多个气液双流体喷嘴634、634’；该输水管道630的进口端与水源6100相连；气液双流体喷嘴634、634’设置于熔渣粒化本体61的内上部及底部，且，气液双流体喷嘴634、634’通过连接管道635连接输气管道620及输水管道630。
参见图4，其中上述气液双流体喷嘴634、634’成阵列排布。
优选地，空气喷嘴阵列组件623的轴向与水平方向成0～20°夹角；优选地，空气喷嘴阵列组件623的宽度大于渣流入口611的宽度。
优选地，第二控制阀F62为电液闸阀。
优选地，熔渣粒化本体61为半封闭的，其后部设熔渣颗粒收集段。
参见图5，其所示为空气喷嘴阵列组件623的出口的一种结构形式，该空气喷嘴阵列组件623的出口包含有多个均匀分布的喷孔6231。
以渣流量5t/min为例，针对熔渣颗粒的飞行轨迹进行模拟计算。
如图6所示，采用不同喷嘴阵列组件在不同倾角(0度、10度、20度)下进行喷气时渣粒的飞行情况，渣粒的飞行角度会受到气流倾角的影响，但气流倾角不能一味的增大。如图7所示，发现在气流倾角超过20°后，一些渣粒会与熔渣粒化本体的上壁面相撞。
另外通过对熔渣粒化过程进行模拟计算，空气喷嘴阵列组件喷射的高速气流的速度优选为90～110m/s。若气流速度过小，熔渣不能被充分破碎，且熔渣会迅速下落附着在熔渣粒化本体的内壁上；若气流速度过大，则粒化效果和渣粒粒径也可能不会得到明显改善。
与现有技术相比，本实施方式的优点在于：
空气喷嘴阵列组件的气流喷嘴喷出的高速射流破碎高炉熔渣使水资源消耗比传统湿法工艺大幅度减少，减少了水污染，同时减少了有害气体的排放，气体管道不易磨损维护成本较少，且不需要花额外能源对冷却后的高炉熔渣进行干燥处理；
熔渣显热经过与雾化喷嘴喷出的大量雾滴进行换热，生成的高温水蒸气的热焓要高于传统风淬工艺生成的热空气的热焓，使熔渣显热的回收效率更高，进行余热回收更具有潜力；
相比于风淬工艺，根据本实施方式的装置由于换热介质主要是水破碎形成的雾滴颗粒，高温熔渣的冷却速率也比风淬的冷却速率要快，更加有利于玻璃体的形成，玻璃体质量越好、含量越高，高炉渣的回收利用率越高；
采用熔渣粒化本体内底部和上部安装多个成排的气液双流体雾化喷嘴的方式，形成均匀分布的雾滴颗粒与熔渣进行换热，与一般的水流冲击相比，均匀的雾滴颗粒与熔渣的换热更为充分，均匀的气流流场使粒化效果更加均匀，成渣效果更好；
雾化喷嘴所喷出的雾滴颗粒对熔渣的粒化及颗粒飞行具有一定的辅助作用，效果较纯气淬要好；
熔渣粒化本体为卧式半封闭装置，其后方设置有渣粒收集段，可以更方便地收集粒化的渣粒，防止熔渣不易收集而发生粘壁现象；
在近渣流入口位置、粒化装置中间位置、粒化装置底部分别设置喷嘴阵列，分段对渣流进行冲击、削薄、粒化，防止因渣流量过大而使粒化不充分的问题发生。
根据本发明的又一实施方式提供一种利用气体喷嘴阵列将高炉熔渣粒化的装置，利用高速气体喷嘴喷出的高速气流冲击液态熔渣将其破碎，并对所粒化的渣粒迅速降温，便于其快速成渣，可适当减少水消耗量以降低成本，还能兼顾熔渣冷却速率以利于固态渣的玻璃体形成，并且该装置可充分利用熔渣的余热，以减少能量的损耗，兼具水淬和风淬粒化技术的优点；冷却速率较快，熔渣破碎效果好，耗能低。
参见图8，根据本实施方式的利用气体喷嘴阵列将高炉熔渣粒化的装置，其包括：
熔渣粒化本体31，为箱体结构，其顶部设渣流入口311、蒸汽流出通道312，高炉熔渣3100通过渣溜槽313经渣流入口311进入熔渣粒化本体31内；
高速空气喷射机构32，包括：
压缩机321、储气罐322、连接储气罐322的输气管道323及连接输气管道323一端的喷嘴阵列324；与储气罐322的出口端相连的输气管道323上依次设置有第一控制阀F31及流量计325；
储气罐322上设有压力表326、进气管道327及进气阀F32；
喷嘴阵列324包括多个喷嘴3241及相应的支流管道3242，各支流管道3242分别与输气管道323相连；喷嘴3241设置于所述熔渣粒化本体31的一侧壁上。
优选地，喷嘴阵列324中的喷嘴3241为选自超音速喷嘴、雾化喷嘴或气液双流体喷嘴中的一种以上；喷嘴阵列324中的喷嘴3241的轴向与熔渣粒化本体31的侧壁相互垂直。
参见图9～图11，所述喷嘴阵列324中的喷嘴3241的排布方式为多行多列。
优选地，如图10和图11所示，喷嘴阵列324中的喷嘴3241的排布方式为多行多列，且相邻两行的喷嘴在竖直方向上错开。
优选地，如图11所示，喷嘴阵列324中的喷嘴3241的排布方式为多行多列，喷嘴数量沿竖直方向逐步减少或增加。
高速气体喷嘴喷出的高速射流(例如喷射速度为90～110m/s)破碎高炉熔渣使水资源消耗减少，减少了水污染，同时减少了有害气体的排放，因而气体管道不易磨损维护成本较少，且不需要花费额外能源对冷却后的高炉熔渣进行干燥处理。相比于风淬工艺，根据本实施方式的装置通过布置高速气体喷嘴以较少的能源消耗使管内气体在相同的压强下可以达到更高的速度，成本低，且噪音污染更小，高温熔渣的冷却速率也比传统风淬的冷却速率要快，更加有利于玻璃体的形成，玻璃体质量越好、含量越高，高炉渣的回收利用率越高。采用底部安装多个高速气体喷嘴的方式，形成均匀分布的高速气流与熔渣进行换热，喷嘴阵列的布置与熔渣的换热更为充分。阵列所形成的气体流域可以均匀而充分的覆盖渣流流动的范围，使得粒化效果更加均匀，成渣效果更好。
参见图12、图13，根据本实施方式的熔渣粒化装置还包括：喷嘴雾化机构33，其包括沿输水管道330依次设置的第二控制阀F32、水泵331、第三控制阀F33、压力表332、流量计333和多个雾化喷嘴334；输水管道330的进口端与水源3200相连；雾化喷嘴设置于熔渣粒化本体31的内底部，且至少排布为两排，水雾喷出方向正对自渣流入口311流入的熔渣。
参见图14，其为根据本发明的又一实施方式中熔渣粒化装置的结构示意图，其中，喷嘴阵列324中的喷嘴为气液双流体喷嘴；相应地，熔渣粒化装置还设有喷嘴供水机构36，其包括沿输水管道360依次设置的第四控制阀F34、水泵361、第五控制阀F35、压力表 362、流量计363；输水管道360的进口端与水源3200相连，出口端与气液双流体喷嘴的进口端相连。
参见图15，其为根据本发明的又一实施方式中熔渣粒化装置的结构示意图，其中，熔渣粒化装置还包括余热回收系统34，其包括：
换热箱体341，其一侧壁上部设有与所述熔渣粒化本体31的出料口相连的进料口3411；换热箱体341的顶部设有换热气流出口3412；换热箱体341内沿高度方向设有多个开孔床板342；换热箱体341的底部设有熔渣颗粒出口3413；
气体喷嘴阵列343，设置于换热箱体341的内底部、开孔床板342的下方，气体喷嘴阵列中的气体喷嘴与开孔床板342相对设置，喷出的气体可对沿开孔床板342下落的渣粒进行进一步冷却。
优选地，所述开孔床板342在换热箱体341内沿竖直方向呈Z字形布置，如图15所示，可延长渣粒下落的路径，有利于对渣粒的有效冷却。
熔渣粒化过程在熔渣粒化本体内进行，高速空气喷射机构、雾化喷嘴机构提供了对熔渣进行破碎粒化的主要动力和进行一次换热，余热回收系统将渣粒和气体分离并进行二次换热。
其工作过程如下：
高速空气喷射机构中的喷嘴阵列提供均匀高速气流将下落的高炉熔渣均匀破碎，得到了呈抛物线运动的高温熔渣颗粒；喷嘴雾化机构中的雾化喷嘴在熔渣粒化本体的底部对呈抛物线运动的熔渣颗粒进行水雾喷吹，一方面增加换热效率使熔渣颗粒快速降温，另一方面给熔渣施加一个推动力。在熔渣粒化本体的尾部设有渣粒收集段，其将渣粒和对熔渣降温形成的高温气流进入余热回收系统的换热箱体内进行气固分离，渣粒途经多个开孔床板与下方气体喷嘴阵列的气体喷嘴喷出的冷空气进行充分换热，换热空气从上方出口流出，冷渣从换热箱体的下方出口落下。
使用时，开启压缩机，压缩机给气体加压将气体送入储气罐，通过储气罐提供稳定压强的气体给(超音速气体)喷嘴阵列，喷嘴将高速气流射入熔渣粒化本体内对自渣流入口进入的熔渣进行破碎；同时，开启水泵，水泵给输水管道内的水加压，然后再经过雾化喷嘴喷出，喷出后雾滴颗粒冲击粒化后的熔渣颗粒，将熔渣颗粒快速降温并冷却成稳定小颗粒；喷嘴阵列中的喷嘴和喷嘴雾化机构中的雾化喷嘴喷出的混合射流冲击高温熔渣全部变成高温空气和水蒸汽的混合物从熔渣粒化本体的上方流出作为余热资源待后续回收利用。
参见图16，其为根据本发明的又一实施方式中熔渣粒化装置的结构示意图，其中，余热回收系统34采用旋风分离器35。
所述旋风分离器35包括分离器本体351，其上部一侧设与所述熔渣粒化本体31的出料口314连通的气固介质入口3511；分离器本体351的顶部设有空气出口3512，分离器本体351的底部设灰斗352。
渣粒和高温气流进入旋风分离器35内进行气固分离。旋风分离器35可以分离出干净的高温气流，能使熔渣粒化过程中产生的余热得到充分回收供后续利用。
与现有技术相比，本实施方式的优点在于：
高速气体喷嘴喷出的高速射流破碎高炉熔渣使水资源消耗减少，减少了水污染，同时减少了有害气体的排放，气体管道不易磨损维护成本较少，且不需要花费额外能源对冷却后的高炉熔渣进行干燥处理；
相比于风淬工艺，该装置通过布置高速气体喷嘴以较少的能源消耗使管内气体在相同的压强下可以达到更高的速度，成本低，且噪音污染更小，高温熔渣的冷却速率也比传统风淬的冷却速率要快，更加有利于玻璃体的形成，玻璃体质量越好、含量越高，高炉渣的回收利用率越高；
采用底部安装多个高速气体喷嘴的方式，形成均匀分布的高速气流(例如喷射速度为90～110m/s)与熔渣进行换热，喷嘴阵列的布置与熔渣的换热更为充分。阵列所形成的气体流域可以均匀而充分的覆盖渣流流动的范围，使得粒化效果更加均匀，成渣效果更好；
采用熔渣粒化本体内底部安装多个雾化喷嘴的方式，形成均匀分布的雾滴颗粒与熔渣进行换热，与一般的水流冲击相比，雾滴颗粒与熔渣的换热更为充分；且雾滴颗粒的喷射给气淬后的熔渣颗粒提供一个推动力，使其避免过早落入装置底部发生粘结现象；
优选地，高速气体以(超音速)喷嘴阵列的形式进行排布，阵列所形成的气体流域可以均匀而充分的覆盖渣流流动的范围，使得粒化效果更加均匀，成渣效果更好；
本实施方式通过余热回收段设计多层布置，渣粒和高温气流进入换热箱体内进行二次余热气体回收、换热和气固分离，大大提高了余热回收效率，且在底部成阵列的气体喷嘴可以使熔渣颗粒迅速降温，并且分离出高温的气流，使熔渣余热得到充分回收。
根据本发明的又一实施方式提供一种可清理落渣的气雾熔渣粒化的装置，利用高速喷嘴阵列组件喷出的高速气流冲击液态熔渣将其破碎，雾化喷嘴喷出的高密度雾滴颗粒对所粒化的渣粒迅速降温，便于其快速成渣，以雾化的形式取代水淬直接喷水的形式，既可适当减少新水消耗量以降低成本，还能兼顾熔渣冷却速率以利于固态渣的玻璃体形成，并且 该装置可充分利用熔渣的余热，以减少能量的损耗；具有冷却速率较快，熔渣破碎效果好，耗能低等优点。
参见图17、图18，本实施方式中可清理落渣的气雾熔渣粒化的装置，其包括：
熔渣粒化本体41，为箱体结构，其顶部设有渣流入口411，其尾部设有渣粒收集段412；熔渣4100通过渣溜槽413自渣流入口411进入熔渣粒化本体41内；
气体喷嘴阵列42，设置于熔渣粒化本体41的一侧壁上；
雾化喷嘴阵列43，设置于熔渣粒化本体41的内底部，气雾喷出方向对应从渣流入口411流入的熔渣；
清理落渣喷嘴44，设置于熔渣粒化本体41内底部，清理落渣喷嘴的出口对着熔渣粒化本体41内底部及渣粒收集段412方向。
优选地，气体喷嘴阵列42的轴向与熔渣粒化本体41的侧壁相互垂直。
优选地，清理落渣喷嘴44为选自水雾化喷嘴、蒸汽雾化喷嘴、高速气流喷嘴或气液双流体喷嘴中的一种以上。
气体喷嘴阵列提供均匀高速气流(例如喷射速度为90～110m/s)，将下落的高炉熔渣均匀破碎，得到了呈抛物线运动的破碎熔渣颗粒；雾化喷嘴在熔渣粒化本体的内底部对着呈抛物线运动的熔渣颗粒进行水雾喷吹，一方面增加换热效率使破碎的熔渣颗粒快速降温，另一方面给熔渣施加一个推动力。熔渣粒化本体尾部的设置有渣粒收集段，并用清理落渣喷嘴(雾化喷嘴)对落到熔渣粒化本体的内底部的渣粒进行换热及吹扫，防止渣粒粘壁。
参见图19和图20，其本发明又一实施方式的熔渣粒化装置的结构示意图，其中上述装置还设有：
高速空气喷射机构420，包括：
压缩机421、储气罐422、连接储气罐422的输气管道423以及连接输气管道423一端的气体喷嘴阵列42；储气罐422的出口端的输气管道423上依次设置第一控制阀F41及流量计424；
所述储气罐422上设有压力表426、进气管道427及进气阀F42；
所述气体喷嘴阵列42包括喷嘴及相应的支流管道4231、4232，支流管道接入输气管道423；清理落渣喷嘴44通过连接管道441及一阀门连接至所述输气管道423；
喷嘴雾化机构430，包括沿输水管道431依次设置的第二控制阀F42、水泵432、第三控制阀F43、压力表433、流量计434；该输水管道431进口端接水源4200，其出口端连接所述雾化喷嘴阵列43。
参见图19，所述雾化喷嘴阵列43的喷嘴为气液双流体喷嘴，其进口端分别与输气管道423和输水管道431相连。
参见图20，发明另一实施方式的熔渣粒化装置的结构示意图，其中，熔渣粒化本体41的顶部设多个渣流入口411、411’。
参见图21，其示出图20中熔渣粒化本体41的俯视图中渣流入口的其中一种排布方式，在本实施方式中，熔渣粒化本体41的顶部设多个渣流入口411、411’、411”。
参见图22，其示出本实施方式中气体喷嘴阵列42中喷嘴的结构示意图，其中心位置排布有均匀的数量较多的气流喷射孔4201，孔的数量和排数可根据实际情况进行调整。
参见图23，其示出本实施方式中气体喷嘴阵列42的另一种结构设计，所述气体喷嘴阵列42的出口位置两侧分别设置有挡板428，挡板428的外侧分别安装液体/雾化喷嘴429，利用气体喷嘴阵列42的喷出的高速空气将液体/雾化喷嘴429喷出的水进行破碎雾化。
与现有技术相比，本实施方式的优点在于：
气体喷嘴阵列喷出的高速射流破碎熔渣使水资源消耗比传统湿法工艺大幅度减少，减少了水污染，同时减少了有害气体的排放，气体管道不易磨损维护成本较少，且不需要花费额外能源对冷却后的高炉熔渣进行干燥处理；
熔渣显热经过与雾化喷嘴阵列喷出的大量雾滴进行换热，生成的高温水蒸气的热焓要高于传统风淬工艺生成的热空气的热焓，使熔渣显热的回收效率更高，进行余热回收利用更具有潜力；
相比于风淬工艺，本实施方式中换热介质由于采用水破碎形成的雾滴颗粒，熔渣的冷却速率也比风淬的冷却速率要快，更加有利于玻璃体的形成，玻璃体质量越好、含量越高，高炉渣的回收利用率越高；
采用底部安装多个雾化喷嘴的方式，形成均匀分布的雾滴颗粒与熔渣进行换热，与一般的水流冲击相比，雾滴颗粒与熔渣的换热更为充分。且雾滴颗粒的喷射给气淬后的熔渣颗粒提供一个推动力，使其避免过早落入装置底部发生粘结现象；
以气体喷嘴阵列的形式进行气体喷嘴排布，阵列所形成的气体流域可以均匀而充分的覆盖渣流流动的范围，使得粒化效果更加均匀，成渣效果更好；
在熔渣粒化本体的底部设置有用于清理落渣的雾化喷嘴，可以清扫落到粒化装置底部的熔渣，防止落渣粘壁；
熔渣粒化本体的顶部设置有多个熔渣入口，将熔渣分流成小流量渣流，使喷嘴的熔渣处理能力和熔渣的粒化效率大大提高。
根据本发明的又一实施方式提供一种利用雾化喷嘴将熔渣快速冷却的装置，利用高速气体喷嘴喷出的高速气流冲击液态熔渣将其破碎，雾化喷嘴喷出的高密度雾滴颗粒对所粒化的渣粒迅速降温，便于其快速成渣，以雾化的形式取代水淬直接喷水的形式，既可适当减少新水消耗量以降低成本，还能兼顾熔渣冷却速率以利于固态渣的玻璃体形成，并且该装置可充分利用熔渣的余热，以减少能量的损耗；具有冷却速率较快，熔渣破碎效果好，耗能低等优点。
参见图24、图25，根据本实施方式的利用雾化喷嘴将熔渣快速冷却的装置，其包括：
熔渣粒化本体71，为箱体结构，其顶部设有渣流入口711；
气体喷嘴阵列72，气体喷嘴设置于熔渣粒化本体71的一侧壁上，气体喷嘴阵列中气体喷嘴的轴向与熔渣粒化本体的侧壁相互垂直；
流场优化喷嘴阵列73，设置于熔渣粒化本体71的内上部，近渣流入口711处；
清渣喷嘴阵列74，设置于熔渣粒化本体71的内下部或底部；
雾化喷嘴阵列75，设置于熔渣粒化本体71内，在熔渣粒化本体71的内壁上环绕渣流7100的径向布置，雾化喷嘴阵列中雾化喷嘴的轴向与气体喷嘴的轴向相互垂直。
优选地，熔渣粒化本体71的尾部设有渣粒收集段76。
优选地，所述流场优化喷嘴阵列73的喷嘴为气体喷嘴或气液双流体喷嘴。
优选地，所述清渣喷嘴阵列74的喷嘴为气体喷嘴。
优选地，所述雾化喷嘴阵列75的喷嘴为水雾化喷嘴。
采用气体喷嘴阵列72提供的均匀高速气流(例如喷射速度为90～110m/s)将自渣容器77下落至熔渣粒化本体71内的熔渣均匀破碎，得到了呈抛物线运动的熔渣颗粒；流场优化喷嘴阵列73在熔渣粒化本体71的上部对着呈抛物线运动的熔渣颗粒进行进一步喷吹，一方面增大熔渣的飞行速度以增强换热，另一方面防止熔渣落壁粘结损坏装置设备；在熔渣粒化本体71的内壁外围设置了多层雾化喷嘴，雾化喷嘴均匀围绕熔渣粒化本体71的内壁排布，使熔渣颗粒迅速降温，由在熔渣粒化本体71尾部的渣粒收集段收集渣粒和换热产生的高温气体。
本实施方式与现有技术相比，其优点为：
高速气体喷嘴喷出的高速射流破碎高炉熔渣使水资源消耗比传统湿法工艺大幅度减少，减少了水污染，同时减少了有害气体的排放，气体管道不易磨损维护成本较少，且不需要花费额外能源对冷却后的高炉熔渣进行干燥处理；
熔渣显热经过与雾化喷嘴喷出的大量雾滴进行换热，生成的高温水蒸气的热焓要高于传统风淬工艺生成的热空气的热焓，使熔渣显热的回收效率更高，进行余热回收更具有潜力；
相比于风淬工艺，由于换热介质是水破碎形成的雾滴颗粒，高温熔渣的冷却速率也比风淬的冷却速率要快，更加有利于玻璃体的形成，玻璃体质量越好、含量越高，高炉渣的回收利用率越高；
采用熔渣粒化本体内壁均匀环绕安装多个雾化喷嘴的方式，形成均匀分布的雾滴颗粒与熔渣进行换热，与一般的水流冲击相比，雾滴颗粒与熔渣的换热更为充分；
利用优化喷嘴阵列优化的方式给初步破碎的熔渣颗粒再次提供一个推动力，使其避免过早落入装置底部发生粘结现象；
高速气体以喷嘴阵列的形式进行排布，阵列所形成的气体流域可以均匀而充分的覆盖渣流流动的范围，使得粒化效果更加均匀，成渣效果更好。
根据本发明的又一实施方式提供一种用于高炉熔渣粒化的水雾粒化装置，利用水喷嘴阵列组件喷出的高速水流(例如喷射速度为90～110m/s)和气液双流体喷嘴喷出的水雾(例如喷射速度为90～110m/s)冲击液态熔渣将其破碎，雾化喷嘴喷出的高密度雾滴颗粒对破碎的渣粒进行迅速换热降温并辅助粒化，便于其快速成渣。以雾化的形式取代水淬直接喷水的形式，既可适当减少新水消耗量以降低成本，还能兼顾熔渣冷却速率以利于固态渣的玻璃体形成，并且该装置可充分利用熔渣的余热，以减少能量的损耗；具有冷却速率较快，熔渣破碎效果好，耗能低等优点。
参见图26、图27，本实施方式提供一种用于高炉熔渣粒化的水雾粒化装置，其包括：
机架51，为框架结构；
水喷嘴阵列组件52，包括，
本体521，为箱体结构，设置于所述机架51中部；其内依次间隔设置有均流板522、导流板523；本体521的后端与水源相连；
水喷嘴阵列524，均布于所述本体521的前端面；
气液双流体喷嘴组件53，包括，
气液双流体喷嘴531，平行设置于所述水喷嘴阵列524的两侧，并固定于机架51上；
气体管道532、输水管道533，固定于机架51上，并与气液双流体喷嘴531相连。
优选地，所述气液双流体喷嘴53、53’平行设置于水喷嘴阵列524的两侧。
水喷嘴阵列组件52的本体521的后端通过法兰与水源相连，水进入本体521内后经过均流板522、导流板523，使水压分布均匀进入水喷嘴阵列524将水喷出；同时，气体和液体分别从气体管道532、输水管道533进入气液双流体喷嘴531进行雾化。
与现有技术相比，本实施方式的优点在于：
水喷嘴阵列组件喷出的高速射流破碎高炉熔渣使水资源消耗比传统湿法工艺大幅度减少，减少了水污染，同时减少了有害气体的排放；
熔渣显热经过与雾化喷嘴喷出的大量雾滴进行换热，生成的高温水蒸气的热焓要高于传统风淬工艺生成的热空气的热焓，使熔渣显热的回收效率更高，进行余热回收更具有潜力；
相比于风淬工艺，该装置由于换热介质主要是水破碎形成的雾滴颗粒，高温熔渣的冷却速率也比风淬的冷却速率要快，更加有利于玻璃体的形成，玻璃体质量越好、含量越高，高炉渣的回收利用率越高；
采用上部和底部安装多个成排的雾化喷嘴的方式，形成均匀分布的雾滴颗粒与熔渣进行换热，与一般的水流冲击相比，雾滴颗粒与熔渣的换热更为充分；
阵列所形成的射流流域可以均匀而充分的覆盖渣流流动的范围，使得粒化效果更加均匀，成渣效果更好。
虽然通过参照本发明的某些优选实施方式，已经对本发明进行了图示和描述，但本领域的普通技术人员应该明白，以上内容是结合具体的实施方式对本发明所作的进一步详细说明，不能认定本发明的具体实施只局限于这些说明。本领域技术人员可以在形式上和细节上对其作各种改变，包括做出若干简单推演或替换，而不偏离本发明的精神和范围。

Claims (47)

  1. 熔渣粒化方法，包括破碎熔渣得到熔渣颗粒，然后对所述熔渣颗粒进行冷却，并收集由此获得的粒化渣。
  2. 如权利要求1所述的方法，其中，
    熔渣通过射流粒化获得表面固化的颗粒和蒸汽，随后所述表面固化的颗粒在旋流场中进行冷却，获得固态渣粒。
  3. 如权利要求1或2所述的方法，其中，所述方法包括如下步骤：
    1)熔渣进入导流罩内，被从粒化器喷出的气雾流体冲击、破碎、粒化成粒径在5mm以内的颗粒熔滴，所述颗粒熔滴随气雾流体沿着导流罩定向飞行，颗粒熔滴在形成和飞行过程中与气雾流体换热得到冷却固化，生成1000℃以下的粒化渣和300～600℃的气流，实现对所述熔渣的粒化和冷却固化；
    2)所述粒化渣和所述气流从导流罩内流出后直接进入旋流器内，在离心力和重力共同作用下实现渣、气分离，分离后的粒化渣温度下降到700～800℃，从所述旋流器的底部流出；
    分离后的气流流经旋流器和溢流管，经溢流管内的螺旋换热管的冷却水换热后温度降到150～300℃，从旋流器和溢流管排出后进入余热回收装置，与余热回收装置内通有冷却水的换热管道接触换热进一步回收余热，形成温度为130～150℃的尾气；
    所述余热回收装置的换热管道内的冷却水吸收热量后汽化，之后经过汽水分离获得压强在0.4～0.5MPa的饱和水蒸汽，返回所述粒化器作为流体用于粒化所述熔渣；
    螺旋换热管内的冷却水吸收热量汽化，随后经过汽水分离生成压强为1.2～1.6MPa、温度在188～201℃的饱和蒸汽，所述饱和蒸汽进入过热蒸汽发生器，补热后获得压强为1.2～1.6MPa、温度为250～350℃的过热蒸汽；
    3)自旋流器的底部流出的粒化渣进入滚筒床，在滚筒床内与通有冷却水的换热管道接触换热，温度降至150～300℃，随后排出进入渣仓储存；
    滚筒床的换热管道内的冷却水吸收热量后汽化，经过汽水分离生成压强为1.2～1.6MPa、温度在188～201℃饱和蒸汽，所述饱和蒸汽进入过热蒸汽发生器，补热后获得压强为1.2～1.6MPa、温度在250～350℃的过热蒸汽；
    4)渣仓内的粒化渣输送进入气流磨，利用步骤2)和步骤3)获得的过热蒸汽冲击、研磨成超细微粉；
    过热蒸汽压强降为常压，温度降至150～250℃，随后进入余热回收装置，与余热回收装置内通有冷却水的换热管道接触换热进一步回收余热，形成温度为130～150℃的尾气；
    所述余热回收装置的换热管道内的冷却水吸收热量后汽化，之后经过汽水分离获得压强为0.4～0.5MPa的饱和水蒸汽，返回所述粒化器作为流体用于粒化所述熔渣。
  4. 如权利要求2或3所述的方法，其中，所述尾气经净化装置除尘、脱硫后排放。
  5. 如权利要求2或3所述的方法，其中，在步骤(1)中，所述气雾流体为选自压强为0.5-0.8MPa的压缩空气、压强为0.4-0.5MPa的水雾、压强为0.4-0.8MPa的蒸汽，以及它们的混合物中的一种以上。
  6. 如权利要求2或3所述的方法，其中，在步骤(1)中，所述颗粒熔滴冷却固化后粒径为2mm以内的颗粒的凝固率在80％以上。
  7. 如权利要求2或3所述的方法，其中，在步骤(3)中，在所述过热蒸汽发生器中利用天然气或钢铁冶炼过程中产生的混合煤气对所述饱和蒸汽进行补热。
  8. 如权利要求2或3所述的方法，其中，在步骤(3)中，将进入渣仓的粒化渣运送至矿渣粉末生产线，直接研磨成比表面积为420～440m2/kg的矿渣微粉。
  9. 如权利要求2或3所述的方法，其中，在步骤(4)中，所述超细微粉的比表面积为450-750m2/kg。
  10. 如权利要求1所述的方法，所述粒化通过带有高速蒸汽喷嘴的熔渣粒化装置实施，其中，通过水泵给进入管道的水加压，然后进入换热器内，来自余热回收管道的热源使换热器内的水温度升高，水处于高于大气压且高于常压下沸点温度的高温高压状态，经过喷嘴喷出后在常压下瞬间气化，形成含有蒸汽的高速射流冲击从渣流槽流出的熔渣，高速射流将熔渣冷却，并破碎成小颗粒落入熔渣粒化本体的底部；喷嘴喷出的混合射流冲击熔渣后全部变成蒸汽从所述装置上方流出作为余热资源待后续利用。
  11. 如权利要求10所述的方法，其中，通过水泵给进入管道的水加压，管道内压强升至0.1～1MPa；来自余热回收管道的热能使换热器内的水温度升高至100～182℃。
  12. 如权利要求1所述的方法，所述粒化通过气水混合的卧式熔渣粒化工艺进行，其中，采用由气体喷嘴组成的空气喷嘴阵列组件提供的高速气流对下落的熔渣进行破碎，得到熔渣颗粒；同时，采用成排的气液双流体喷嘴对所述熔渣颗粒进行水雾喷吹，使所述熔渣颗粒快速降温，并给所述熔渣颗粒施加一个辅助推动力，使其更准确地落入后部的渣粒收集段。
  13. 如权利要求12所述的方法，其中，所述高速气流的速度为90～110m/s。
  14. 熔渣粒化装置，包括：
    粒化机构，用于粒化熔渣获得破碎的熔渣颗粒；
    冷却机构，用于冷却所述熔渣颗粒获得粒化渣。
  15. 如权利要求14所述的装置，包括：
    导流罩，其为一筒体结构；优选其横截面呈矩形，长宽比为2:1～5:1；更优选，所述导流罩的进口端安装有在线称量装置；
    粒化器，其出口端连接导流罩的进口端；
    旋流器，其侧壁设有物料进口，底部设有物料出口；所述物料进口与所述导流罩的出口端相连，
    溢流管，其下部竖直插置于旋流器内，溢流管内设置螺旋换热管；
    第一汽水分离器，其上设冷却水进口、冷却水出口、蒸汽进口及蒸汽出口；所述冷却水进口连接冷却水管路，所述冷却水出口通过管道及水泵连接所述溢流管内的螺旋换热管的进口端，所述蒸汽进口与所述溢流管内的螺旋换热管的出口端连接，
    余热回收装置，其壳体上设有进气口及出气口，内部设有换热管道，该进气口与所述溢流管的出口端相连；
    第二汽水分离器，其上设冷却水进口、冷却水出口、蒸汽进口及蒸汽出口；该冷却水进口连接冷却水管路，冷却水出口通过管道及水泵与所述余热回收装置内换热管道的进口端连接，蒸汽进口通过管道与所述余热回收装置的换热管道的出口端连接，蒸汽出口通过管道与所述粒化器的进口端连接；
    滚筒床，其为一筒体结构，内部设有换热管道，所述滚筒床的进口端与所述旋流器的物料出口相连，所述滚筒床的出口端与渣仓相连，所述滚筒床上设有一可带动其转动的驱动装置；
    第三汽水分离器，其上设冷却水进口、冷却水出口、蒸汽进口及蒸汽出口；该冷却水进口连接冷却水管路，冷却水出口通过管道及水泵与所述滚筒床的换热管道的进口端连接，蒸汽进口与所述滚筒床的换热管道的出口端连接；
    气流磨，其壳体上设有进料管、进气管和出气管，所述气流磨的进料管与渣仓相连，所述气流磨的出气管与所述余热回收装置的进气口相连；
    过热蒸汽发生器，其壳体上设有进气管道和出气管道，所述过热蒸汽发生器的进气管道与所述第一汽水分离器的蒸汽出口及所述第三汽水分离器的蒸汽出口相连，所述过热蒸汽发生器的出气管道与所述气流磨的进气管相连。
  16. 如权利要求15所述的装置，其中，所述渣仓上设有振动器。
  17. 如权利要求14所述的装置，其中，所述装置为采用高速蒸汽喷嘴的熔渣粒化装置，包括：
    熔渣粒化本体，为一箱体结构，其上部一侧设供熔渣进入的渣流槽，熔渣粒化本体顶部设有蒸汽流出通道；
    蒸汽喷雾机构，包括沿管道依次设置的第一控制阀、水泵、第二控制阀、压力表、换热器、温度计和喷嘴；所述管道的进口端接水源；所述喷嘴设置于所述熔渣粒化本体设有渣流槽一侧的侧壁，且所述喷嘴的轴向与渣流槽的轴向成一夹角，喷嘴的出口方向正对渣流槽流出的熔渣；
    所述换热器上设余热回收管道和换热流体流出管道；其中，所述余热回收管道上安装有阀门。
  18. 如权利要求17所述的装置，其中，所述喷嘴的轴向与所述渣流槽的轴向成30～60°夹角。
  19. 如权利要求17所述的装置，其中，所述第一控制阀为电液闸阀。
  20. 如权利要求14所述的装置，其中，所述装置为用于气水混合的卧式熔渣粒化工艺的装置，包括：
    熔渣粒化本体，为箱体结构，其顶部设渣流入口；
    高速空气喷射机构，包括：
    压缩机、储气罐、连接储气罐的输气管道及连接输气管道一端的空气喷嘴阵列组件；与储气罐的出口端相连的输气管道上依次设置第一控制阀及流量计；
    所述储气罐上设压力表、进气管道及进气阀；
    所述空气喷嘴阵列组件包括多个气流喷嘴及相应的支流管道，所述支流管道与所述输气管道相连；所述气流喷嘴设置于所述熔渣粒化本体的一侧壁上部；
    喷雾机构，包括：沿输水管道依次设置的第二控制阀、水泵、第三控制阀、压力表、流量计和多个气液双流体喷嘴；所述输水管道的进口端与水源相连；所述气液双流体喷嘴设置于所述熔渣粒化本体的内上部及底部，且，所述气液双流体喷嘴通过连接管道与所述输气管道及输水管道相连。
  21. 如权利要求20所述的装置，其中，所述空气喷嘴阵列组件的轴向与水平方向成0～20°夹角。
  22. 如权利要求20或21所述的装置，其中，所述空气喷嘴阵列组件的宽度大于所述渣流入口的宽度。
  23. 如权利要求20所述的装置，其中，所述第二控制阀为电液闸阀。
  24. 如权利要求20所述的装置，其中，所述熔渣粒化本体是半封闭的，其后部设有熔渣颗粒收集段。
  25. 如权利要求20所述的装置，其中，所述气流喷嘴为超音速喷嘴。
  26. 如权利要求14所述的装置，其中，所述装置为利用气体喷嘴阵列将熔渣粒化的装置，包括：
    熔渣粒化本体，为箱体结构，其顶部设渣流入口、蒸汽流出通道；
    高速空气喷射机构，包括：
    压缩机、储气罐、连接储气罐的输气管道及连接输气管道一端的喷嘴阵列；储气罐出口端的输气管道中依次设置第一控制阀及流量计；所述储气罐上设压力表、进气管道及进气阀；
    所述喷嘴阵列包括多个喷嘴及相应的支流管道，各支流管道分别与所述输气管道相连；所述喷嘴设置于所述熔渣粒化本体的一侧壁上。
  27. 如权利要求26所述的装置，其中，所述装置还包括：
    喷嘴雾化机构，包括沿输水管道依次设置的第二控制阀、水泵、第三控制阀、压力表、流量计和多个雾化喷嘴；所述输水管道进口端与水源相连；所述雾化喷嘴设置于所述熔渣粒化本体的内底部，且至少排布为两排，水雾喷出方向正对自所述渣流入口流入的熔渣。
  28. 如权利要求26或27所述的装置，其中，所述装置还包括余热回收系统，所述余热回收系统包括：
    换热箱体，其一侧壁上部设有与所述熔渣粒化本体的出料口相连的进料口；所述换热箱体的顶部设有换热气流出口；换热箱体内沿高度方向设有多个开孔床板；所述换热箱体的底部设有熔渣颗粒出口；
    气体喷嘴阵列，设置于所述换热箱体的内底部、开孔床板的下方，所述气体喷嘴阵列中的气体喷嘴与所述开孔床板相对设置；或者，
    所述余热回收系统采用旋风分离器。
  29. 如权利要求28所述的装置，其中，所述开孔床板在换热箱体内沿竖直方向呈Z字形布置。
  30. 如权利要求29所述的装置，其中，所述旋风分离器包括分离器本体，所述分离器本体的上部一侧设有与所述熔渣粒化本体的出料口连通的气固介质入口；所述分离器本体的顶部设有空气出口，所述分离器本体的底部设有灰斗。
  31. 如权利要求26所述的装置，其中，所述喷嘴阵列中的喷嘴为选自超音速喷嘴、雾化喷嘴或气液双流体喷嘴中的一种以上；优选地，所述喷嘴阵列中喷嘴的轴向与熔渣粒化本体的侧壁互相垂直。
  32. 如权利要求26或31所述的装置，其中，所述喷嘴阵列中喷嘴的排布方式为多行多列，或呈弧形排列；优选地，相邻两行的喷嘴在竖直方向上错开；更优选地，喷嘴数量沿竖直方向逐步减少或增加。
  33. 如权利要求26所述的装置，其中，所述喷嘴阵列中的喷嘴为气液双流体喷嘴；相应地，所述装置还设有喷嘴供水机构，所述喷嘴供水机构包括沿输水管道依次设置的第四控制阀、水泵、第五控制阀、压力表、流量计；所述输水管道的进口端与水源相连，出口端与气液双流体喷嘴的进口端相连。
  34. 如权利要求14所述的装置，其中，所述装置为可清理落渣的气雾熔渣粒化的装置，包括：
    熔渣粒化本体，为箱体结构，其顶部设有渣流入口，其尾部设有渣粒收集段；
    气体喷嘴阵列，设置于所述熔渣粒化本体的一侧壁上；
    雾化喷嘴阵列，设置于所述熔渣粒化本体的内底部，气雾喷出方向对应从所述渣流入口流入的熔渣；
    清理落渣喷嘴，设置于所述熔渣粒化本体的内底部，所述清理落渣喷嘴的出口对着所述熔渣粒化本体的内底部及所述渣粒收集段方向。
  35. 如权利要求34所述的装置，其中，所述气体喷嘴阵列的轴向与所述熔渣粒化本体的侧壁相互垂直。
  36. 如权利要求34或35所述的装置，其中，所述气体喷嘴阵列的出口两侧分别设有挡板，所述挡板的外侧分别安装有液体/雾化喷嘴。
  37. 如权利要求34所述的装置，其中，所述清理落渣喷嘴为选自水雾化喷嘴、蒸汽雾化喷嘴、高速气流喷嘴或气液双流体喷嘴中的一种以上。
  38. 如权利要求34所述的装置，其中，所述装置还设有：
    高速空气喷射机构，其包括，压缩机、储气罐、连接储气罐的输气管道及连接输气管道一端的气体喷嘴阵列；储气罐的出口端的输气管道上依次设置第一控制阀及流量计；所述储气罐上设有压力表、进气管道及进气阀；所述喷嘴阵列包括若干喷嘴及相应的支流管道，支流管道接入输气管道；所述清理落渣喷嘴通过连接管道及一阀门连接至所述输气管道；
    喷嘴雾化机构，包括沿输水管道依次设置的第二控制阀、水泵、第三控制阀、压力表、流量计；所述输水管道的进口端与水源相连，其出口端连接至所述雾化喷嘴阵列。
  39. 如权利要求34或38所述的装置，其中，所述雾化喷嘴阵列中的喷嘴为气液双流体喷嘴，其进口端分别连接输气管道和输水管道。
  40. 如权利要求34或35或38所述的装置，其中，所述熔渣粒化本体的顶部设有至少两个渣流入口。
  41. 如权利要求14所述的装置，其中，所述装置为利用雾化喷嘴将熔渣快速冷却的装置，包括：
    熔渣粒化本体，为箱体结构，其顶部设有渣流入口；
    气体喷嘴阵列，设置于所述熔渣粒化本体的一侧壁上，所述气体喷嘴阵列中气体喷嘴的轴向与所述熔渣粒化本体的侧壁相互垂直；
    流场优化喷嘴阵列，设置于所述熔渣粒化本体的内上部，近所述渣流入口处；
    清渣喷嘴阵列，设置于所述熔渣粒化本体的内下部或底部；
    雾化喷嘴阵列，设置于所述熔渣粒化本体内，在所述熔渣粒化本体的内壁上环绕渣流的径向布置，所述雾化喷嘴阵列中雾化喷嘴的轴向与所述气体喷嘴的轴向相互垂直。
  42. 如权利要求41所述的装置，其中，所述熔渣粒化本体的尾部设有渣粒收集段。
  43. 如权利要求41所述的装置，其中，所述流场优化喷嘴阵列的喷嘴为气体喷嘴或气液双流体喷嘴。
  44. 如权利要求41所述的装置，其中，所述清渣喷嘴阵列的喷嘴为气体喷嘴。
  45. 如权利要求41所述的装置，其中，所述雾化喷嘴阵列的喷嘴为水雾化喷嘴。
  46. 如权利要求14所述的装置，其中，所述装置为用于熔渣粒化的水雾粒化装置，包括：
    机架，为框架结构；
    水喷嘴阵列组件，包括，
    本体，为箱体结构，设置于所述机架中部；其内依次间隔设置有均流板、导流板；所述本体的后端与水源相连；
    水喷嘴阵列，均布于所述本体的前端面；
    气液双流体喷嘴组件，包括，
    气液双流体喷嘴，平行设置于所述水喷嘴阵列的两侧，并固定于所述机架上；
    气体管道、输水管道，固定于机架上，并与所述气液双流体喷嘴相连。
  47. 如权利要求46所述的装置，其中，所述气液双流体喷嘴平行设置于所述水喷嘴阵列的两侧。
PCT/CN2023/138507 2022-12-13 2023-12-13 熔渣粒化方法及装置 Ceased WO2024125562A1 (zh)

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