EP3400200A1 - Procédé et dispositif de granulation de nitrate d'ammonium poreux - Google Patents

Procédé et dispositif de granulation de nitrate d'ammonium poreux

Info

Publication number
EP3400200A1
EP3400200A1 EP17700153.4A EP17700153A EP3400200A1 EP 3400200 A1 EP3400200 A1 EP 3400200A1 EP 17700153 A EP17700153 A EP 17700153A EP 3400200 A1 EP3400200 A1 EP 3400200A1
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
prills
prilling
ammonium nitrate
prilling tower
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP17700153.4A
Other languages
German (de)
English (en)
Inventor
Axel Erben
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ThyssenKrupp AG
ThyssenKrupp Industrial Solutions AG
Original Assignee
ThyssenKrupp AG
ThyssenKrupp Industrial Solutions AG
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
Publication date
Application filed by ThyssenKrupp AG, ThyssenKrupp Industrial Solutions AG filed Critical ThyssenKrupp AG
Publication of EP3400200A1 publication Critical patent/EP3400200A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/18—Nitrates of ammonium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2/00—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic
    • B01J2/02—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic by dividing the liquid material into drops, e.g. by spraying, and solidifying the drops
    • B01J2/04—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic by dividing the liquid material into drops, e.g. by spraying, and solidifying the drops in a gaseous medium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2/00—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic
    • B01J2/16—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic by suspending the powder material in a gas, e.g. in fluidised beds or as a falling curtain
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05C—NITROGENOUS FERTILISERS
    • C05C1/00—Ammonium nitrate fertilisers
    • C05C1/02—Granulation; Pelletisation; Stabilisation; Colouring
    • C—CHEMISTRY; METALLURGY
    • C06—EXPLOSIVES; MATCHES
    • C06B—EXPLOSIVES OR THERMIC COMPOSITIONS; MANUFACTURE THEREOF; USE OF SINGLE SUBSTANCES AS EXPLOSIVES
    • C06B31/00—Compositions containing an inorganic nitrogen-oxygen salt
    • C06B31/28—Compositions containing an inorganic nitrogen-oxygen salt the salt being ammonium nitrate
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2004/00—Particle morphology
    • C01P2004/30—Particle morphology extending in three dimensions
    • C01P2004/32—Spheres

Definitions

  • the invention relates to the production of porous ammonium nitrate, wherein an ammonium nitrate composition is prilled in an ammonium nitrate Prillierstrom to form an ammonium nitrate granules, which is collected in a fluidized bed and there at least partially cooled.
  • the method of prilling a composition in a prilling plant is a known technical method for producing granulated products from melts or from concentrated solutions.
  • Spray nozzles thereby divide the supplied melt or solution into drops which fall through a gaseous medium, usually air, and are thereby cooled so that they solidify into grains. If the material supplied is a solution, the solidification process is accompanied by partial evaporation.
  • the prilling technique finds great industrial application in the production of, for example, urea fertilizer, but also of other substances which are provided or are obtained in the form of melts or concentrated solutions.
  • an ammonium nitrate composition is prilled in a prilling tower in a countercurrent of cooled air.
  • prills i. homogeneous solid bodies still containing some water content (e.g., about 4% by weight).
  • water is then quickly removed.
  • the resulting pores or cracks in the prill are continuous, so that they can be filled with oil, for example.
  • prilling towers cool an approximately 96% and 145-150 ° C hot ammonium nitrate composition to below the transformation point of about 84 ° C from.
  • the porosity is produced in a downstream drying drum and achieved the required low final moisture of prized final product in a turn downstream second drying drum.
  • Prilling towers usually comprise a prilling channel, through which the composition to be prilled flows and which makes up the free drop height of the prilling tower.
  • priming towers usually comprise discharge stations, which are attached to the head of the prilling tower and transfer the composition to be prilled into the prilling tower.
  • Prilling ammonium nitrate compositions are common Prilling systems are required, which have Prillturme with a total height of 60-70 m and a free drop height of 40-50 m.
  • Porous prilled ammonium nitrate is commonly used as one of the ingredients of explosive compositions.
  • porous prilled ammonium nitrate is blended with fuel oil to produce the explosive composition known as ANFO.
  • US 2009/0301618 A1 relates to porous granules of explosive ammonium nitrate, which are prepared from an ammonium nitrate melt in two successive fluidized beds. Also BG 63 296 B1 and DE 15 92 359 A1 disclose processes for the production of granules of ammonium nitrate. US 4,190,622 A and US 3,539,326 A disclose processes for producing granular particles.
  • the known methods and apparatus for producing porous ammonium nitrate are not entirely satisfactory and there is a need for improved methods and apparatus.
  • the invention is thus based on the object to provide methods and apparatus for the production of porous ammonium nitrate, which have advantages over the prior art.
  • a first aspect of the invention relates to a process for the preparation of porous ammonium nitrate, the process comprising the following steps:
  • step (b) collecting the prills formed in step (a) in a first fluidized bed
  • the ammonium nitrate composition is introduced into the prilling tower, preferably into the head end of the prilling tower.
  • the ammonium nitrate composition is an ammonium nitrate melt, which may optionally be aqueous.
  • the ammonium nitrate composition comprises water.
  • the ammonium nitrate composition a water content in the range of 1 to 6 wt .-%, more preferably in the range of 2 to 5.5 wt .-%, in the range of 3 to 5 wt .-%, or in the range of 4 to 4.5 wt. %.
  • the composition may optionally contain other additives, in particular Prillierzu algorithms. Suitable prilling additives are known to a person skilled in the art.
  • the ammonium nitrate composition is sprayed through one or more prilling nozzles in a Prillkanal and then flows through the Prill tower from top to bottom.
  • the preparation of the ammonium nitrate composition and the method of spraying the ammonium nitrate composition are known to those skilled in the art.
  • the prilling tower is additionally traversed by air.
  • the air preferably comprises various gaseous constituents, in particular oxygen and nitrogen.
  • the term "air” preferably also encompasses aerosols, so that the air, in addition to gaseous components, can also comprise solid and / or liquid constituents, which preferably occur during the prilling of ammonium nitrate.
  • the air may include ammonium nitrate dust.
  • such gas mixtures and / or aerosols are generally referred to as "air”.
  • the air flows through the Prill tower from the foot to the head, so from bottom to top.
  • the ammonium nitrate composition is flowed through as it flows through the prilling tower of the air in countercurrent.
  • the ammonium nitrate prills are formed from the ammonium nitrate composition (in statu nascendi) and fall down in the prilling tower, where they are circulated by air in countercurrent from bottom to top.
  • the air flow is not sufficient to put the prills in a floating state, but there is a relative movement of the prills down, which is slowed down by the air in countercurrent.
  • the relative amount of air flowing around the ammonium nitrate composition is in the range of 1 to 20 kg of air per kg of the ammonium nitrate composition employed, more preferably in the range of 1.5 to 15 kg, in the range of 2 to 10 kg in the range from 2.5 to 8 kg, in the range of 3 to 7 kg or in the range of 4 to 5.5 kg.
  • step (b) of the process according to the invention the prills formed in step (a) are collected in a first fluidized bed.
  • the fluid bed is formed by the prills, which previously flowed through the prilling tower.
  • a fluidized bed is suitable for a variety of process engineering processes for the treatment of solids and liquids and its structure is known to a person skilled in the art.
  • the fluidized bed of the present invention is constituted by the collected prills, which are fluidized by an upward flow of a fluid. This creates a liquid-like state of the prills, also referred to as a "fluidized bed.” This provides optimal cooling and drying conditions.
  • the prills formed in step (a) of the process according to the invention are collected in a fluidized bed of fluidized prills.
  • the prills Upon reaching the first fluid bed, the prills are preferably flowed around by the fluid, preferably by air, from bottom to top, whereby the fluid causes the prills to transition to a fluid state, to be set in permanent motion, at least partially not to the bottom of the fluidized bed touch and thus become part of the fluidized bed.
  • the first fluidized bed is preferably connected directly to the prilling tower.
  • the prills preferably fall from top to bottom through the prilling tower essentially exclusively as a result of the gravitational force and leave the prilling tower at the bottom thereof, whereupon they preferably also fall on the first fluidized bed essentially exclusively due to the gravitational force and are caught thereby.
  • the first fluidized bed is arranged below the prilling tower.
  • the ammonium nitrate composition is cooled while passing through the prilling tower and flowing around the air in countercurrent.
  • the ammonium nitrate composition is preferably cooled in such a way that the prills formed in the prilling tower are dimensionally stable when collected in the fluidized bed.
  • the cooling of the ammonium nitrate composition in the prilling tower preferably takes place in such a way that the liquid phase of the prills when collected in a fluidized bed is at most 80% by weight, more preferably at most 75% by weight, at most 70% by weight, at most 65% by weight.
  • the difference between the temperature of the ammonium nitrate composition when introduced into the head end of the prilling tower and the temperature of the prills at the moment of collection in the fluidized bed is preferably at least 20 ° C, more preferably at least 25 ° C, at least 30 ° C, at least 35 ° C, at least 40 ° C, at least 45 ° C or at least
  • the temperature of the ammonium nitrate composition when introduced into the head end of the prilling tower is at least 120 ° C, more preferably at least 125 ° C, at least 130 ° C, at least 135 ° C, at least 140 ° C, at least 145 ° C, at least 150 ° C, at least 155 ° C or at least 160 ° C
  • the prills when collected in the first fluidized bed, have a temperature in the range of 90 to 120 ° C, more preferably in the range of 92 ° C to 15 ° C, in the range of 94 ° C to 110 ° C or in the range of 95 ° C to 105 ° C.
  • the prills leave the prilling tower preferably at the bottom, whereupon they preferably fall on the first fluidized bed and are collected by this.
  • the collection of the prills in the first fluidized bed is very gentle compared to conventional prilling methods.
  • the prills are exposed to a significantly reduced mechanical stress. This makes it possible, not even to a large extent solidified or dried, i. to work through through hardened prills.
  • the procedure according to the invention therefore requires only a comparatively lower cooling of the prills in the prilling tower than in the case of processes without a connected fluidized bed.
  • the difference between the temperature of the ammonium nitrate prills, which are collected after leaving the prilling tower in the first fluidized bed, and the temperature of the ammonium nitrate prills leaving a conventional prilling tower without a fluidized bed connected according to the invention preferably at least 5 ° C, more preferably at least 10 ° C, at least 15 ° C, at least 20 ° C, at least 25 ° C or at least 30 ° C.
  • the temperature of the prills when leaving the prilling tower is significantly influenced by the dwell time of the prills in the prilling tower and thus by the free fall height of the prilling tower.
  • the required free fall height of the prilling tower is at most 60 m, more preferably at most 55 m, at most 50 m, at most 45 m, at most 40 m, at most 35 m, not more than 30 m, not more than 25 m, not more than 20 m, not more than 15 m, not more than 10 m or not more than 5 m.
  • the prills are at least partially cooled on the first fluidized bed.
  • the prills are cooled on the first fluidized bed so that their temperature on leaving the first fluidized bed is at least 5 ° C lower, more preferably at least 10 ° C, at least 15 ° C, at least 20 ° C or at least 25 ° C, than at Reaching the first fluidized bed.
  • the prills leave the first fluidized bed and the temperature of the prills upon leaving the first fluidized bed is less than 84 ° C, more preferably less than 80 ° C.
  • the prills leave the first fluidized bed and are then passed to a second fluidized bed.
  • Suitable measures for passing the prills from the first fluidized bed to the second fluidised bed are known to a person skilled in the art.
  • the first fluidized bed may not be completely level to support horizontal flow.
  • first and second fluidized bed can possibly also be achieved analogously by a single fluidized bed, which may be correspondingly larger in size.
  • the prills are at least partially pre-dried on the second fluidized bed.
  • the prills are predried on the second fluidized bed in such a way that the need for a predrying drum is eliminated in the downstream production fabrication steps.
  • the water content of the prills when leaving the second fluidized bed is at most 5% by weight, more preferably at most 4% by weight, at most 3% by weight, at most 2% by weight, at most 1% by weight, at most 0. 9 wt .-% or at most 0.8 wt .-%, each with respect to the total weight of the prills.
  • a first air flow flows through the first fluidized bed and / or a second airflow flows through the second fluidized bed and / or a further airflow flows through the prilling tower.
  • the first air flow flows through the first fluidized bed and / or the second air flow flows through the second fluidized bed from bottom to top.
  • the first air stream preferably puts the prills in the first fluidized bed into a fluidized state and / or the second airflow places the prills in the second fluidized bed in a fluidized state.
  • the first air stream is passed through the first fluidized bed to cool the prills.
  • the second air stream for predrying the prills is passed through the second fluidized bed. For efficient prilling a total of preferably a larger amount of air is required than the amount of air flowing through the first fluidized bed and / or the second fluidized bed.
  • the further air flow is preferably introduced into the prilling tower and flows through it preferably from bottom to top.
  • the further air flow is introduced at the foot into the prilling tower.
  • the further air stream may be introduced at one or at different positions in the prilling tower, preferably the further air stream is introduced at a position in the prilling tower.
  • the further air stream may also be mixed with the air stream of the second fluidized bed and / or at least partially added to the first fluidized bed.
  • the further air stream comprises ambient air.
  • the further air stream comprises process air which is obtained elsewhere in the process for the production of porous ammonium nitrate and / or in another process.
  • the air flow at the head end is derived from the prilling tower.
  • at least 10% by volume of the air stream passing through the prilling tower is derived from the prilling tower and treated in a purification step, more preferably at least 20% by volume, at least 30% by volume, at least 40% by volume, at least 50% Vol .-%, at least 60 vol .-%, at least 70 vol .-%, at least 80 vol .-% or at least 90 vol .-%.
  • the cleaning step is preferably a wet scrubber.
  • At least 10% by volume of the air treated in the purification stage is returned to the foot of the prilling tower, more preferably at least 20% by volume, at least 30% by volume, at least 40% by volume, at least 50% by volume. %, at least 60 vol.%, at least 70 vol.%, at least 80 vol.% or at least 90 vol.%.
  • the air treated in the purification step is completely returned to the foot of the prilling tower.
  • the further air flow may comprise only ambient air or only process air or only the air returned to the foot of the prilling tower or all possible combinations thereof in all possible proportions.
  • the first and the second air stream may be independent of each other or be in operative connection with each other. So both the first and the second Air flow are provided independently of each other and flow through the first and the second fluidized bed independently.
  • the second air stream is the second fluidized bed and then at least partially the first fluidized bed.
  • At least 10% by volume of the first air stream after flowing through the first fluidized bed flows through the prilling tower, more preferably at least 20% by volume, at least 30% by volume, at least 40% by volume, at least 50% by volume, at least 60% by volume, at least 70% by volume, at least 80% by volume or at least 90% by volume.
  • the first air stream preferably flows through the prilling tower completely after flowing through the first fluidized bed.
  • At least 10% by volume of the second air stream flows through the second fluidized bed and then the first fluidized bed, more preferably at least 20% by volume, at least 30% by volume, at least 40% by volume, at least 50 vol.%, At least 60 vol.%, At least 70 vol.%, At least 80 vol.% Or at least 90 vol.%.
  • the second air stream flows completely through the first fluidized bed after flowing through the second fluidized bed.
  • a further aspect of the invention relates to a device for the production of porous ammonium nitrate comprising the following components which are in operative connection with one another:
  • the components of the device according to the invention are in operative connection with each other, i. are connected to each other by suitable piping etc. in a manner which ensures the general functioning of the device.
  • the necessary measures are known to a person skilled in the art.
  • the ammonium nitrate prilling plant comprises a prilling tower whose free fall height is preferably at most 40 m, more preferably at most 35 m, at most 30 m, at most 25 m, at most 20 m, at most 15 m, at most 10 m or at most 5 m.
  • the fluidized bed is preferably arranged at the foot of the prilling tower.
  • the fluidized bed is arranged below the prilling tower, so that the prills formed in the prilling tower fall by gravity into the first fluidized bed, are collected by this and become part of this fluidized bed.
  • the fluidized bed can comprise one or more beds.
  • the difference between the base area of the first fluidized bed and the base area of the Prillkanals is preferably at most 10%, more preferably at most 9%, at most 8%, at most 7% at most 6%, at most 5%, at most 4%, at most 3%, at most 2 % or at most 1%.
  • the base of the first fluidized bed and the base of the Prillkanals are the same size.
  • the apparatus comprises a second fluidized bed disposed after the first fluidized bed and configured to predry the prills.
  • the second fluidized bed may comprise one or more beds.
  • the device comprises the additional components which are at least temporarily in operative connection with one another:
  • the moistening devices preferably moisten the first and / or the further air stream by adding liquid.
  • the moistening devices preferably moisten the first and / or the further air flow by adding water.
  • the moistening of the first and / or the further air flow can take place continuously or temporarily.
  • the moistening of the first and / or of the further air stream preferably takes place as a function of the water content of the prills in the first fluidized bed.
  • the further air flow is moistened such that the relative humidity, ie the percentage ratio between the vapor content of the further air flow and the maximum possible vapor content of the further air flow, is in the range of 70 to 100%, more preferably in the range of 75 to 90%.
  • the device comprises the additional components which are at least temporarily in operative connection with one another:
  • the cleaning step removes impurities from the air discharged via the discharge device and is preferably a wet scrubber.
  • at least part of the air treated in the purification stage is returned via the return device to the foot end of the prilling tower.
  • at least 10% by volume of the air treated in the purification step is returned to the foot of the prilling tower, more preferably at least 20 vol.%, at least 30 vol.%, at least 40 vol.%, at least 50 vol.%, at least 60 vol.%, at least 70 vol.%, at least 80 vol.% or at least 90% by volume.
  • the air treated in the purification step is completely returned to the foot of the prilling tower.
  • the air is cooled in the purification stage.
  • the purification step comprises a wash solution and the cooling of the air to a temperature close to the cooling limit temperature over the present wash solution.
  • the cooling of the air is preferably carried out to a temperature which deviates by at most 10 ° C. from the cooling limit temperature above the present washing solution, more preferably by at most 5 ° C. or by at most 1 ° C.
  • the cooling limit temperature refers to the lowest temperature which can be achieved by direct evaporative cooling.
  • the device according to the invention is preferably used according to the method according to the invention.
  • FIG. 1 schematically and by way of example illustrates the process according to the invention for the production of porous ammonium nitrate using an ammonium nitrate prilling plant, but is not to be construed as limiting.
  • the process shown in Figure 1 comprises the prilling of an ammonium nitrate solution through one or more Prilldüsen (1) in a Prillkanal (2) with directly connected first fluidized bed (3) or second fluidized bed (4).
  • the free fall height of the Prillkanals is preferably carried out so long that the prills on reaching the first fluidized bed (3) have a temperature preferably in the range of 90 to 120 ° C and thus achieve sufficient strength and dimensional stability.
  • an optional water spray can be provided in front of the first fluidized bed (3).
  • the prills are preferably cooled to below 84 ° C. in a first step and then predried in a second, optional step on the second fluidized bed (4).
  • Pre-drying eliminates the need for a predrying drum in the downstream product fabrication steps. Since a larger relative amount of air may be necessary for efficient prilling than for the first fluidized bed (3), a further air flow is preferably conducted into the prilling channel. This further air flow may be, for example, a part of the prilling air used, which is cleaned and cooled in a purification stage (5) and then returned to the prilling channel (1).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Fertilizers (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne la fabrication de nitrate d'ammonium poreux, une composition de nitrate d'ammonium étant granulée dans un dispositif de granulation de nitrate d'ammonium afin de former des granulés de nitrate d'ammonium qui sont recueillis dans un lit fluidisé et au moins partiellement refroidis dans celui-ci, un premier courant d'air parcourant le premier lit fluidisé et/ou un deuxième courant d'air parcourant le deuxième lit fluidisé et/ou un autre courant d'air parcourant la tour de granulation.
EP17700153.4A 2016-01-07 2017-01-04 Procédé et dispositif de granulation de nitrate d'ammonium poreux Withdrawn EP3400200A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102016200108.6A DE102016200108A1 (de) 2016-01-07 2016-01-07 Verfahren und Apparatur zur Prillierung von porösem Ammoniumnitrat
PCT/EP2017/050110 WO2017118646A1 (fr) 2016-01-07 2017-01-04 Procédé et dispositif de granulation de nitrate d'ammonium poreux

Publications (1)

Publication Number Publication Date
EP3400200A1 true EP3400200A1 (fr) 2018-11-14

Family

ID=57758625

Family Applications (1)

Application Number Title Priority Date Filing Date
EP17700153.4A Withdrawn EP3400200A1 (fr) 2016-01-07 2017-01-04 Procédé et dispositif de granulation de nitrate d'ammonium poreux

Country Status (5)

Country Link
EP (1) EP3400200A1 (fr)
CN (1) CN108473330A (fr)
DE (1) DE102016200108A1 (fr)
RU (1) RU2700054C1 (fr)
WO (1) WO2017118646A1 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU2021314568A1 (en) * 2020-07-31 2023-02-09 Dyno Nobel Asia Pacific Pty Limited Phase-stabilized ammonium nitrate explosives
JPWO2024204514A1 (fr) * 2023-03-30 2024-10-03

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1109410A (en) * 1966-04-01 1968-04-10 Toyo Koatsu Ind Inc Production of granular fertilizer
FR1483944A (fr) * 1966-04-28 1967-06-09 Nitrates & Engrais Procédé perfectionné de fabrication du nitrate d'ammonium en granules
GB1493612A (en) * 1974-07-06 1977-11-30 Fisons Ltd Prilling
US4190622A (en) * 1978-05-04 1980-02-26 Standard Oil Company (Ohio) Process for prilling urea
JPS62282629A (ja) * 1986-05-30 1987-12-08 Okawara Mfg Co Ltd 連続式流動層造粒装置
WO2000074835A1 (fr) * 1999-06-08 2000-12-14 Niro A/S Procede de spray et equipement correspondant
BG63296B1 (bg) * 1999-07-01 2001-09-28 Христо МИТЕВСКИ Метод и инсталация за получаване на порьозна гранулирана амониева селитра
CN100364654C (zh) * 2002-11-26 2008-01-30 奥姆尼亚肥料有限公司 用于制备硝酸盐颗粒的设备
US7198653B2 (en) * 2003-07-31 2007-04-03 Delavau Llc Calcium carbonate granulation
UA98306C2 (uk) * 2006-08-02 2012-05-10 Омния Фертилайзер Лимитед Гранули нітрату амонію та спосіб їх одержання
RU2411184C1 (ru) * 2009-08-17 2011-02-10 Открытое акционерное общество "Научно-исследовательский и проектный институт азотной промышленности и продуктов органического синтеза" (ОАО "ГИАП") Способ производства гранулированного нитрата аммония
CN201592092U (zh) * 2010-01-19 2010-09-29 北京德厚朴化工技术有限公司 一种新型两段式流化床
CN202214298U (zh) * 2011-01-19 2012-05-09 湖北宜化化工股份有限公司 一种降低尿素颗粒温度的装置

Also Published As

Publication number Publication date
RU2700054C1 (ru) 2019-09-12
DE102016200108A1 (de) 2017-07-13
WO2017118646A1 (fr) 2017-07-13
CN108473330A (zh) 2018-08-31

Similar Documents

Publication Publication Date Title
DE2825039B2 (de) Verfahren zur Herstellung von Harnstoffkörnern
EP1663455B1 (fr) Procede d'elimination d'ammoniac et de poussieres contenus dans des gaz brules, produits lors de la production d'urée
DE2746975A1 (de) Verfahren zur trennung trockener teilchenfoermiger masse aus einem heissgas
DE69911265T2 (de) Verfahren und anlage zum sprühtrocknen
EP0820802A2 (fr) Laveur à plusieures étapes et procédé pour la purification totale de gaz
DE1186802B (de) Zerstaeubungstrocknungsverfahren mit Feingutrueckfuehrung
DE2420639A1 (de) Verfahren zur selektiven reinigung von heissgasen
WO2017118646A1 (fr) Procédé et dispositif de granulation de nitrate d'ammonium poreux
WO1986004519A1 (fr) Installation d'epuration et procede pour retirer des elements polluants de gaz chauds
WO2018137995A1 (fr) Procédé et système de récupération de chaleur lors de la granulation en lit fluidisé
DE19751851A1 (de) Aerosolminderung
DE102004026909A1 (de) Verfahren und Vorrichtung zur aerosolarmen Partialkondensation
EP0492135B1 (fr) Dispositif pour la purification d'air avec des filtres à bio et procédé pour une telle purification d'air
DE2510241A1 (de) Verfahren zur absorption von gasfoermigen bestandteilen aus gasen
DE2503637A1 (de) Verfahren und vorrichtung zur herstellung von prills
DE2157831C3 (de) Vorrichtung zum Entfernen von Schwefeloxiden aus Abgasen
EP3914373B1 (fr) Épurateur d'air vicié comprenant une aspiration d'air interne
EP0509258B1 (fr) Procédé pour la purification de fumées
DE3024292C2 (de) Verfahren und Vorrichtung zum Herstellen von Paraffin- oder Wachspulver für die Kerzenformung
DE4015831C2 (de) Vorrichtung zum Auswaschen von HCl aus einem Abgas
EP3615194A1 (fr) Procédé et dispositif de fabrication d'urée
DE3229494C2 (de) Verfahren zur Reinigung von SO↓2↓-haltigen Gasen
DE69535271T2 (de) Eine methode für die reinigung von luft und anderen gasen, die von pulvern, rauch, gasen, dämpfen und lösungen, auch aromaten, verunreinigt sind
DE19731505A1 (de) Reinigung der bei der Herstellung von Mineraldüngemitteln entstehenden Abgase
EP0639104B1 (fr) Procede et installation pour l'epuration de gaz d'evacuation, et combinaison de cette epuration de gaz avec une epuration d'eaux usees

Legal Events

Date Code Title Description
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: UNKNOWN

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE

PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20180807

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

DAV Request for validation of the european patent (deleted)
DAX Request for extension of the european patent (deleted)
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

17Q First examination report despatched

Effective date: 20190826

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20200722

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20201202