CN222761237U - Variable-load air separation rectifying device - Google Patents

Variable-load air separation rectifying device Download PDF

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Publication number
CN222761237U
CN222761237U CN202421307247.3U CN202421307247U CN222761237U CN 222761237 U CN222761237 U CN 222761237U CN 202421307247 U CN202421307247 U CN 202421307247U CN 222761237 U CN222761237 U CN 222761237U
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China
Prior art keywords
tower
pipe
main
compressed air
oxygen
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CN202421307247.3U
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Chinese (zh)
Inventor
李震
孔令卓
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Kaifeng Kaixing Contract Energy Management Co ltd
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Kaifeng Kaixing Contract Energy Management Co ltd
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/32—Processes or apparatus using separation by rectification using a side column fed by a stream from the high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

本实用新型涉及一种变负荷空分精馏装置，包括主精馏塔和压缩空气输送总管，所述的主精馏塔包括上塔、主冷凝换热器和下塔，其压缩空气输送总管设置有第一压缩空气输送支管、透平膨胀机、机后换热器、第二压缩空气输送支管和第三压缩空气输送支管，第二压缩空气输送支管和上塔通过透平膨胀机的膨胀端相连通，第一压缩空气输送支管和下塔相连通，主冷凝换热器上连通有副精馏塔，副精馏塔包括填料塔和塔底蒸发器，塔底蒸发器和主冷凝换热器通过粗氧输送管相连通，第三压缩空气输送支管和塔底蒸发器相连通，下塔和填料塔通过污液氮输送管相连通。便于调整成品氧气产出量。本实用新型调节方便，具有广泛的市场前景。

The utility model relates to a variable load air separation distillation device, including a main distillation tower and a compressed air delivery main pipe, wherein the main distillation tower includes an upper tower, a main condensing heat exchanger and a lower tower, wherein the compressed air delivery main pipe is provided with a first compressed air delivery branch pipe, a turbine expander, a post-machine heat exchanger, a second compressed air delivery branch pipe and a third compressed air delivery branch pipe, wherein the second compressed air delivery branch pipe is connected to the upper tower through the expansion end of the turbine expander, the first compressed air delivery branch pipe is connected to the lower tower, the main condensing heat exchanger is connected to a secondary distillation tower, the secondary distillation tower includes a packing tower and a tower bottom evaporator, the tower bottom evaporator and the main condensing heat exchanger are connected through a crude oxygen delivery pipe, the third compressed air delivery branch pipe is connected to the tower bottom evaporator, and the lower tower and the packing tower are connected through a dirty liquid nitrogen delivery pipe. It is convenient to adjust the output of finished oxygen. The utility model is easy to adjust and has broad market prospects.

Description

Variable-load air separation rectifying device
Technical Field
The utility model relates to the field of variable-load air separation rectifying equipment, in particular to a variable-load air separation rectifying device.
Background
The cryogenic rectification method is also called as a cryogenic separation method, and the cryogenic air separation principle uses air as a raw material, and the air is liquefied into liquid air through compression, purification and heat exchange. The liquid air is mainly a mixture of liquid oxygen and liquid nitrogen, and nitrogen and oxygen are obtained by separating liquid oxygen and liquid nitrogen through rectification by utilizing the difference of boiling points of the liquid oxygen and the liquid nitrogen. Specifically, raw material air is filtered out dust and mechanical impurities through a self-cleaning filter, then enters a main air compressor, compressed gas is cooled by an air precooling device and then is sent to a purifying device to remove impurities such as water and carbon dioxide, so as to form adsorbed compressed air, and the adsorbed compressed air is sent to a rectifying tower for low-temperature rectification as raw material after heat exchange between a main heat exchanger and other gas mediums. The common nitrogen-oxygen separation rectifying tower sequentially comprises an upper tower, a main condensing heat exchanger and a lower tower from top to bottom, after raw materials are fed into the rectifying tower for rectification, finished product nitrogen and finished product oxygen are produced outwards from the upper tower, the main condensing heat exchanger produces finished product liquid oxygen and finished product liquid nitrogen, the upper tower utilizes the oxygen-enriched liquid space conveyed from the lower tower to the upper tower, and the oxygen-enriched liquid space entering the upper tower is utilized to perform full heat exchange with gas evaporated by the main condensing evaporator and liquid nitrogen flowing back to the upper tower, so that finished product nitrogen, finished product oxygen and finished product liquid oxygen are produced. However, for a simplified air separation device which simply realizes nitrogen-oxygen separation and does not further separate the rest low-content gas, the upper tower needs more theoretical plates to separate the finished product oxygen and the finished product liquid oxygen which meet the national standard. The increase of the theoretical plate number of the upper tower directly leads to the increase of the tower height of the upper tower, the process that the oxygen-enriched liquid air conveyed to the upper tower by the lower tower is difficult to realize when the pressure of the lower tower is only utilized to convey the oxygen-enriched liquid air to the upper tower, and a low-temperature booster pump is generally required to be additionally arranged on a conveying pipeline of the oxygen-enriched liquid air so as to provide auxiliary power for the oxygen-enriched liquid air conveyed to the upper tower, so that the process that the oxygen-enriched liquid air is conveyed to the upper tower from the lower tower can be completed.
The product requirement of the low-temperature air separation unit in the current stage of steel production enterprises is that the low-temperature air separation unit is required to produce a large amount of finished nitrogen and a large amount of finished oxygen, and the finished liquid nitrogen and the finished liquid oxygen are produced as byproducts. Because the blast furnace is required for oxygen-enriched fuel gas, one great effect of finished oxygen is to be used as an oxygen source of the oxygen-enriched fuel gas, and because the blast furnace is intermittent in operation, the air separation low-temperature rectification device matched with steel production enterprises is required for variable load, so that sufficient oxygen can be continuously provided in the operation stage of the blast furnace, sufficient oxygen-enriched fuel gas can be provided, and the oxygen supply amount can be reduced in the stop operation stage of the blast furnace, so that the produced oxygen is prevented from being wasted. However, it is difficult to provide a higher rate of load change in order to meet the normal operation of the cryogenic rectification plant using only a cryogenic rectification plant comprising an upper column, a main condensing evaporator and a lower column. In the prior art, although the oxygen after vaporization can be combined to the finished product oxygen conveying pipe through vaporizing the finished product liquid oxygen so as to meet the requirement of enterprises on oxygen, the process of vaporizing the finished product oxygen is usually maintained at the outer side of the cold box, and the vaporization process also needs additional heat energy to be realized, and excessive consumption of energy exists, so that the main process of nitrogen-oxygen separation is not influenced, and the output of the finished product oxygen is convenient to adjust, which is a technical problem worthy of improvement, so that the steel production enterprises can use the process of supplying oxygen by using the low-temperature air separation device more conveniently as much as possible, and the market competitiveness of the low-temperature rectification device is convenient to improve.
Disclosure of Invention
Aiming at the defects of the prior art, the utility model provides a variable-load air separation rectifying device which is convenient for adjusting the output of finished oxygen and is used for overcoming the defects in the prior art.
The technical scheme includes that the variable-load air separation rectifying device comprises a main rectifying tower and a compressed air conveying main pipe, wherein the main rectifying tower sequentially comprises an upper tower, a main condensing heat exchanger and a lower tower from top to bottom, the compressed air conveying main pipe is sequentially provided with an inlet end of a first compressed air conveying branch pipe, a booster end of a turbine expander, a post-heat exchanger, an inlet end of a second compressed air conveying branch pipe and an inlet end of a third compressed air conveying branch pipe along the direction from an inlet end of the compressed air conveying main pipe to an outlet end of the compressed air conveying main pipe, an outlet end of the second compressed air conveying branch pipe is communicated with an inlet of the expansion end of the turbine expander, an outlet end of the expansion end of the turbine expander is communicated with the upper tower, an outlet end of the first compressed air conveying branch pipe is communicated with the lower tower, a cold source channel of the main condensing heat exchanger is communicated with an auxiliary rectifying tower, the auxiliary rectifying tower comprises a filler tower and a tower bottom evaporator arranged at the bottom end of the filler tower, the cold source channel of the tower bottom evaporator is communicated with a cold source channel of the main condensing heat exchanger through a crude oxygen conveying pipe, an outlet of the third compressed air conveying branch pipe is communicated with a liquid nitrogen sewage channel through the bottom of the evaporator.
Preferably, the first compressed air delivery branch pipe, the second compressed air delivery branch pipe and the third compressed air delivery branch pipe are respectively provided with a first regulating valve and a first gas flow sensor.
Preferably, a liquid nitrogen conveying main pipe is arranged on the outlet of the heat source channel of the main condensing heat exchanger, the liquid nitrogen conveying main pipe is sequentially provided with an inlet end of a first liquid nitrogen return pipe, an inlet end of a second liquid nitrogen return pipe and a second regulating valve along the direction from the main condensing heat exchanger to the main condensing heat exchanger, the first liquid nitrogen return pipe and the second liquid nitrogen return pipe are respectively provided with a third regulating valve, the top of the lower tower is communicated with the inlet of the heat source channel of the main condensing heat exchanger, the outlet end of the first liquid nitrogen return pipe is communicated with the top of the lower tower, the outlet end of the second liquid nitrogen return pipe is communicated with the top of the upper tower, the lower tower and the upper tower are provided with oxygen-enriched liquid air conveying pipes, and the oxygen-enriched liquid air conveying pipes are provided with fourth regulating valves.
Preferably, the inlet end of the dirty liquid nitrogen conveying pipe is positioned between the outlet end of the first compressed air conveying branch pipe and the outlet end of the first liquid nitrogen return pipe, a fifth regulating valve is arranged on the dirty liquid nitrogen conveying pipe, the inlet end of the liquefied air conveying pipe is arranged on the outlet of the heat source channel of the tower bottom evaporator, the inlet end of the dirty liquid nitrogen conveying pipe is communicated with the outlet end of the liquefied air conveying pipe and the lower tower between the outlet ends of the first compressed air conveying branch pipe, and a sixth regulating valve is arranged on the liquefied air conveying pipe.
Preferably, the upper tower is provided with a main sewage nitrogen conveying pipe, the main liquid nitrogen conveying pipe, the air oxygen-enriched liquid conveying pipe and the main sewage nitrogen conveying pipe between the inlet end of the first liquid nitrogen return pipe and the second liquid nitrogen return pipe are provided with a subcooler, the top of the filling tower is provided with an inlet end of a branch sewage nitrogen conveying pipe, and the main sewage nitrogen conveying pipe between the subcooler and the upper tower is communicated with an outlet end of the branch sewage nitrogen conveying pipe.
Preferably, the bottom of the packing tower is provided with an oxygen conveying main pipe, the oxygen conveying main pipe is sequentially provided with an online chromatographic analyzer, an oxygen conveying branch pipe, a seventh regulating valve and a second gas flow sensor along the direction from the packing tower to the packing tower, the oxygen conveying branch pipe is provided with an eighth regulating valve and a third gas flow sensor, the bottom of a cold source channel of the tower bottom evaporator is provided with a liquid oxygen conveying pipe, and the liquid oxygen conveying pipe is provided with a ninth regulating valve.
Preferably, the liquid level sensors are respectively arranged on the cold source channel of the tower bottom evaporator, the cold source channel of the main condensing heat exchanger and the bottom of the lower tower, and the liquid flow sensors are arranged on the dirty liquid nitrogen conveying pipe.
The utility model has the advantages that firstly, although the auxiliary rectifying tower comprising the packing tower and the tower bottom evaporator is added, the flow rate of the third compressed air which is conveyed to the heat source channel of the tower bottom evaporator through the second heat source channel of the main heat exchanger by the third compressed air conveying branch pipe is convenient to adjust, so that the flow rate of oxygen conveyed by the oxygen conveying main pipe is convenient to adjust. The product has larger variable adjustment quantity in the produced oxygen flow, thereby meeting the change of oxygen demand quantity of steel production enterprises in different production periods, and furthermore, the product is externally conveyed through the cold source channel of the main condensation heat exchanger, is not liquid oxygen product but liquid oxygen containing partial nitrogen component, relatively speaking, the height of the upper tower is reduced, thereby being convenient for utilizing the pressure of the lower tower to convey oxygen-enriched liquid to the upper tower to participate in the rectification process of the upper tower.
And secondly, the oxygen transmission main pipe is sequentially provided with the online chromatographic analyzer, the oxygen transmission branch pipe, the seventh regulating valve and the second gas flow sensor along the direction from the direction close to the packing tower to the direction far away from the packing tower, the online chromatographic analyzer is convenient to feed back related component parameters, and the second gas flow sensor is convenient to feed back related flow parameters.
Finally, the first compressed air conveying branch pipe, the second compressed air conveying branch pipe and the third compressed air conveying branch pipe are respectively provided with a first regulating valve and a first gas flow sensor, so that the flow rates of compressed air conveyed by the first compressed air conveying branch pipe, the second compressed air conveying branch pipe and the third compressed air conveying branch pipe can be conveniently regulated respectively.
The utility model has the advantages of simple structure, convenient operation, ingenious design, great improvement of working efficiency, good social and economic benefits and easy popularization and use.
Drawings
Fig. 1 is a schematic structural view of the present utility model.
Fig. 2 is an enlarged partial schematic view of detail a of fig. 1.
Detailed Description
As shown in fig. 1 and 2, a variable load air separation rectifying device comprises a main rectifying tower and a compressed air conveying main pipe 1, the main rectifying tower sequentially comprises an upper tower 2, a main condensing heat exchanger 3 and a lower tower 4 from top to bottom, the compressed air conveying main pipe 1 is sequentially provided with an inlet end of a first compressed air conveying branch pipe 5, a supercharging end of a turbine expander 6, a post-machine heat exchanger 7, an inlet end of a second compressed air conveying branch pipe 8 and an inlet end of a third compressed air conveying branch pipe 9 along the direction from the inlet end of the compressed air conveying main pipe 1 to the outlet end of the compressed air conveying main pipe 1, an outlet end of the second compressed air conveying branch pipe 8 is communicated with an expansion end inlet of the turbine expander 6, an outlet end of the turbine expander 6 is communicated with the upper tower 2, an outlet end of the first compressed air conveying branch pipe 5 is communicated with the lower tower 4, the auxiliary rectifying tower is sequentially arranged on a cold source channel of the main condensing heat exchanger 3, the auxiliary rectifying tower comprises a filling tower 10 and a tower bottom evaporator 11 arranged on the bottom end of the filling tower 10, an evaporator 11 is communicated with a cold source channel of the bottom 11 of the filling tower 10, and a cold source channel of the bottom of the main condensing heat exchanger 3 is communicated with the cold source channel 11 through the cooling source channel of the filling tower 11, and the cold source channel of the cooling tower 11 is communicated with the cold source channel of the cold source channel 11. The first compressed air delivery branch pipe 5, the second compressed air delivery branch pipe 8 and the third compressed air delivery branch pipe 9 are respectively provided with a first regulating valve 14 and a first gas flow sensor 15.
Further, a liquid nitrogen delivery main pipe 16 is disposed at the outlet of the heat source channel of the main condensing heat exchanger 3, the liquid nitrogen delivery main pipe 16 is sequentially provided with an inlet end of a first liquid nitrogen return pipe 17, an inlet end of a second liquid nitrogen return pipe 18 and a second regulating valve 19 along the direction from the main condensing heat exchanger 3 to the main condensing heat exchanger 3, the first liquid nitrogen return pipe 17 and the second liquid nitrogen return pipe 18 are respectively provided with a third regulating valve 20, the top of the lower tower 4 is communicated with the inlet of the heat source channel of the main condensing heat exchanger 3, the outlet end of the first liquid nitrogen return pipe 17 is communicated with the top of the lower tower 4, the outlet end of the second liquid nitrogen return pipe 18 is communicated with the top of the upper tower 2, the lower tower 4 and the upper tower 2 are provided with an oxygen-enriched liquid air delivery pipe 21, and the oxygen-enriched liquid air delivery pipe 21 is provided with a fourth regulating valve 22. The inlet end of the dirty liquid nitrogen conveying pipe 13 is positioned between the outlet end of the first compressed air conveying branch pipe 5 and the outlet end of the first liquid nitrogen return pipe 17, a fifth regulating valve 23 is arranged on the dirty liquid nitrogen conveying pipe 13, the inlet end of a liquefied air conveying pipe 24 is arranged on the outlet of the heat source channel of the tower bottom evaporator 11, the inlet end of the dirty liquid nitrogen conveying pipe 13 is communicated with the outlet end of the liquefied air conveying pipe 24, and a sixth regulating valve 25 is arranged on the liquefied air conveying pipe 24. The upper tower 2 is provided with a main dirty nitrogen conveying pipe 26, a main liquid nitrogen conveying pipe 16 between the inlet end of the first liquid nitrogen return pipe 17 and the second liquid nitrogen return pipe 18, an oxygen-enriched liquid air conveying pipe 21 and the main dirty nitrogen conveying pipe 26 are provided with a subcooler 27, the top of the packed tower 10 is provided with an inlet end of a branch dirty nitrogen conveying pipe 28, and the subcooler 27 is communicated with the outlet ends of the main dirty nitrogen conveying pipe 26 and the branch dirty nitrogen conveying pipe 28 between the upper tower 2.
Still further, an oxygen delivery main pipe 29 is disposed at the bottom of the packed tower 10, the oxygen delivery main pipe 29 is sequentially provided with an online chromatograph 30, an oxygen delivery branch pipe 31, a seventh regulating valve 32 and a second gas flow sensor 33 along the direction from the packed tower 10 to the packed tower 10, an eighth regulating valve 34 and a third gas flow sensor 35 are disposed on the oxygen delivery branch pipe 31, a liquid oxygen delivery pipe 36 is disposed at the bottom of the cold source channel of the bottom evaporator 11, and a ninth regulating valve 37 is disposed on the liquid oxygen delivery pipe 36.
The liquid level sensor 38 is respectively arranged on the cold source channel of the tower bottom evaporator 11, the cold source channel of the main condensing heat exchanger 3 and the bottom of the lower tower 4, so that the feedback of liquid level parameters is facilitated, the liquid flow sensor 39 is arranged on the dirty liquid nitrogen conveying pipe 13, and the tenth regulating valve 42 is arranged on the crude oxygen conveying pipe 12. The first compressed air delivery branch pipe 5, the second compressed air delivery branch pipe 8, the third compressed air delivery branch pipe 9, the dirty nitrogen delivery main pipe 26 on the side of the subcooler 27 away from the upper tower 2 and the nitrogen delivery pipe 40 are provided with main heat exchangers 41.
The application method of the product is as follows, as shown in fig. 1 and 2, and comprises the following steps:
S1, the compressed air conveying main pipe 1 receives purified compressed air conveyed by an upstream purifying system and is divided into two parts, namely a first part of compressed air and a second part of compressed air, wherein the first part of compressed air is conveyed to a first heat source channel of a first compressed air conveying branch pipe 5 and then conveyed to a main heat exchanger 41, and is conveyed to a lower tower 4 to serve as one of rectification raw materials of the lower tower 4 after heat exchange of a cold source continuously conveyed to the main heat exchanger 41, the second part of compressed air continuously moves along the compressed air conveying main pipe 1, is firstly pressurized again through a pressurizing end of a turbine expander 6, then is subjected to countercurrent heat exchange through a heat source channel of a post heat exchanger 7 and a cold source medium continuously conveyed to a cold source channel of the post heat exchanger 7, is divided into two parts again, namely a third part of compressed air and a fourth part of compressed air, and the third part of compressed air is conveyed to a third compressed air conveying branch pipe 9, enters the second heat source channel of the main heat exchanger 41 and the cold source continuously conveyed to the main heat exchanger 41, is finally conveyed to a heat source channel of the bottom evaporator 11 and the bottom evaporator 11 after heat exchange of the cold source continuously conveyed to the bottom evaporator 11, and finally is conveyed to the bottom tower 4 to serve as one of the rectification raw materials of the lower tower 4 after heat exchange medium is conveyed to the liquid air conveying pipe 24. The fourth part of compressed air is delivered to the second compressed air delivery branch pipe 8, then delivered to the third heat source channel of the main heat exchanger 41 and continuously delivered to the cold source of the main heat exchanger 41 for heat exchange, finally discharged from the high temperature area of the main heat exchanger 41, delivered to the expansion end of the turbine expander 6 for expansion cooling, and delivered to the upper tower 2 to serve as one of the rectification raw materials of the upper tower 2.
S2, the first part of compressed air is conveyed to the lower tower 4 through a first compressed air conveying branch pipe 5 to form an ascending air flow of the lower tower 4, the ascending air flow of the lower tower 4 sequentially carries out countercurrent heat exchange with liquid air conveyed to the lower tower 4 through a liquefied air conveying pipe 24 and reflux condensate of the lower tower 4 during continuous ascending along the inner cavity of the lower tower 4, the liquid air conveyed to the lower tower 4 through the liquefied air conveying pipe 24 and the reflux condensate of the lower tower 4 are respectively in countercurrent heat exchange with the ascending air flow of the lower tower 4, nitrogen components in the liquid air conveyed to the lower tower 4 through the liquefied air conveying pipe 24 and nitrogen components in part of reflux condensate of the lower tower 4 are vaporized and combined in the ascending air flow, the oxygen component in the first part of compressed air entering the lower tower 4, the oxygen component in the liquid air conveyed to the lower tower 4 by the liquefied air conveying pipe 24 and the unvaporized part of reflux condensate of the lower tower 4 form a descending liquid flow of the lower tower 4 together, the oxygen component in the descending liquid flow of the lower tower 4 continuously rises in the descending process of the inner cavity of the lower tower 4, a first nitrogen enrichment zone is finally formed at the top of the lower tower 4, and an oxygen-enriched liquid air enrichment zone is formed at the bottom of the lower tower 4, so that the nitrogen in the first nitrogen enrichment zone enters the heat source channel of the main condensing heat exchanger 3 through the top of the lower tower 4 to serve as a heat source continuously conveyed to the main condensing heat exchanger 3, the oxygen-enriched liquid air in the oxygen-enriched liquid air enrichment zone is conveyed to the upper tower 2 through the first heat source channel of the subcooler 27 and the cold source continuously conveyed to the subcooler 27 to serve as one of rectifying raw materials of the upper tower 2 after heat exchange, the dirty liquid nitrogen containing a small amount of oxygen component between the outlet end of the first compressed air delivery branch pipe 5 and the outlet end of the first liquid nitrogen return pipe 17 is delivered to the packed column 10 through the dirty liquid nitrogen delivery pipe 13 as reflux condensate of the packed column 10.
S3, after expansion cooling by an expansion end of a turbine expander 6, the fourth part of compressed air fed into the upper tower 2 enters the upper tower 2 to form an ascending air flow of the upper tower 2, wherein the ascending air flow of the upper tower 2 forms a descending liquid flow of the upper tower 2 together with oxygen-enriched liquid air fed into the upper tower 2 through an oxygen-enriched liquid air conveying pipe 21 and reflux condensate fed into the upper tower 2 through a second liquid nitrogen reflux pipe 18 in sequence in a countercurrent heat exchange process respectively in a continuous ascending process in the upper tower 2, the oxygen component in the fourth part of compressed air fed into the upper tower 2, the oxygen component in the oxygen-enriched liquid air fed into the upper tower 2 through the oxygen-enriched liquid air conveying pipe 21 and the non-vaporized part of reflux condensate fed into the upper tower 2 through the second liquid nitrogen reflux pipe 18, the nitrogen component in the fourth part of the compressed air entering the upper column 2, the nitrogen component in the oxygen-enriched liquid air entering the upper column 2 through the oxygen-enriched liquid air conveying pipe 21 and the vaporized part in the reflux condensate conveyed to the upper column 2 through the second liquid nitrogen return pipe 18 form an ascending air flow of the upper column 2, the second nitrogen enrichment zone at the top row of the upper column 2 finally, wherein partial nitrogen containing impurities forms first polluted nitrogen which passes through the polluted nitrogen conveying main pipe 26 and is conveyed to the polluted nitrogen conveying main pipe 26, the rest forms finished nitrogen which is conveyed to the nitrogen conveying pipe 40, the first cold source channel which is conveyed to the main heat exchanger 41 through the nitrogen conveying pipe 40 and the heat source which is continuously conveyed to the main heat exchanger 41 are subjected to heat exchange, the descending air flow of the upper column 2 is continuously conveyed to the user through the outlet end of the nitrogen conveying pipe 40, the descending air flow is continuously conveyed to the cold source channel of the main condensation heat exchanger 3 and the heat source which is continuously conveyed to the main condensation heat exchanger 3 finally, the nitrogen component in the descending air flow is further vaporized after the heat exchange, the reformed gas is combined into the ascending gas flow of the upper tower 2, and finally liquid oxygen containing partial nitrogen components is formed in the cold source channel of the main condensing heat exchanger 3, and the liquid oxygen is conveyed to the cold source channel of the tower bottom evaporator 11 through the crude oxygen conveying pipe 12.
S4, after the nitrogen in the first nitrogen enrichment area enters a heat source channel of the main condensing heat exchanger 3 through the top of the lower tower 4 and is subjected to heat exchange with a cold source continuously conveyed to a cold source channel of the main condensing heat exchanger 3, the nitrogen conveyed to the heat source channel of the main condensing heat exchanger 3 is liquefied and conveyed outwards through a liquid nitrogen conveying main pipe 16 and divided into two parts, namely a first part of liquid nitrogen and a second part of liquid nitrogen, the first part of liquid nitrogen is conveyed back to the lower tower 4 through a first liquid nitrogen backflow pipe 17 to serve as reflux condensate of the lower tower 4, the second part of liquid nitrogen enters a second heat source channel of the subcooler 27 and is subjected to heat exchange with a cold source continuously conveyed to the subcooler 27 to form supercooled liquid nitrogen, the supercooled liquid nitrogen is divided into two parts again, namely a third part of liquid nitrogen and a fourth part of liquid nitrogen, the third part of liquid nitrogen is conveyed back to the upper tower 2 through a second liquid nitrogen backflow pipe 18 to serve as reflux condensate of the upper tower 2, and the fourth part of liquid nitrogen is conveyed outwards through the liquid nitrogen conveying main pipe 16 to serve as a finished liquid nitrogen storage device.
S5, after the liquid oxygen containing partial nitrogen component and the heat source continuously conveyed to the heat source channel of the tower bottom evaporator 11 are subjected to heat exchange through the crude oxygen conveying pipe 12, the nitrogen component in the liquid oxygen containing partial nitrogen component and the partial oxygen component form countercurrent heat exchange with the reflux condensate of the filler tower 10 conveyed through the dirty liquid nitrogen conveying pipe 13, wherein the nitrogen component in the reflux condensate of the filler tower 10 is gasified in the process, the nitrogen component in the ascending gas flow is combined into the ascending gas flow together with partial impurity gas, the oxygen component in the reflux condensate of the filler tower 10 keeps liquid to form a descending liquid flow of the filler tower 10, the nitrogen component is gradually reduced and the oxygen component is gradually increased in the descending liquid flow of the filler tower 10 in the continuous descending process along the filler tower 10, finally an oxygen enrichment zone is formed at the bottom of the filler tower 10, and the liquid oxygen in the liquid oxygen enrichment zone is conveyed to the outside as a liquid oxygen conveying device through the liquid oxygen conveying pipe 36. The oxygen in the oxygen enrichment area of the packed tower 10 is delivered to the oxygen delivery main 29 and divided into two parts, namely, a first part of oxygen and a second part of oxygen, wherein the first part of oxygen is delivered to the target user through the outlet end of the oxygen delivery main 29 to serve as finished oxygen, and the second part of oxygen is delivered to the outside through the oxygen delivery branch pipe 31 to serve as an oxygen source of oxygen-enriched fuel gas. As the upward flow of the packed tower 10 continues to be upward, a nitrogen enrichment zone containing impurities is formed at the top of the packed tower 10 and second polluted nitrogen is delivered to the polluted nitrogen delivery main pipe 26 through the polluted nitrogen delivery branch pipe 28, the second polluted nitrogen and the first polluted nitrogen are combined to form third polluted nitrogen, and heat exchange between the cold source channel passing through the subcooler 27 and the heat source continuously delivered to the subcooler 27 continues to be performed along the polluted nitrogen delivery main pipe 26, and after heat exchange between the second cold source channel passing through the main heat exchanger 41 and the heat source continuously delivered to the main heat exchanger 41, the second polluted nitrogen is delivered to a polluted nitrogen user.
By this embodiment, although the auxiliary rectifying tower comprising the packed tower 10 and the bottom evaporator 11 is added, the flow rate of the third compressed air which is delivered to the heat source channel of the bottom evaporator 11 through the second heat source channel of the main heat exchanger 41 by the third compressed air delivery branch pipe 9 is conveniently adjusted, so that the flow rate of oxygen which is delivered through the oxygen delivery main pipe 29 is conveniently adjusted. The product has larger variable adjustment quantity in the produced oxygen flow, thereby meeting the change of oxygen demand of steel production enterprises in different production periods, and furthermore, the product is externally conveyed through the cold source channel of the main condensation heat exchanger 3, is not liquid oxygen product but liquid oxygen containing partial nitrogen component, relatively speaking, the height of the upper tower 2 is reduced, thereby being convenient for utilizing the pressure of the lower tower 4 to convey oxygen-enriched liquid to the upper tower 2 to participate in the rectification process of the upper tower 2.
The above-described embodiments are merely preferred embodiments of the present utility model and are not intended to limit the scope of the present utility model, so that all equivalent changes or modifications of the structure, characteristics and principles described in the claims should be included in the scope of the present utility model.

Claims (7)

1.一种变负荷空分精馏装置，包括主精馏塔和压缩空气输送总管（1），所述的主精馏塔从上至下依次包括上塔（2）、主冷凝换热器（3）和下塔（4），其特征在于：所述的压缩空气输送总管（1）沿着压缩空气输送总管（1）进口端至压缩空气输送总管（1）出口端方向依次设置有第一压缩空气输送支管（5）的进口端、透平膨胀机（6）的增压端、机后换热器（7）、第二压缩空气输送支管（8）的进口端和第三压缩空气输送支管（9）的进口端，第二压缩空气输送支管（8）的出口端和透平膨胀机（6）的膨胀端入口相连通，透平膨胀机（6）的膨胀端出口和上塔（2）相连通，第一压缩空气输送支管（5）的出口端和下塔（4）相连通，主冷凝换热器（3）的冷源通道上连通有副精馏塔，所述的副精馏塔包括填料塔（10）和填料塔（10）底端上设置的塔底蒸发器（11），塔底蒸发器（11）的冷源通道和主冷凝换热器（3）的冷源通道通过粗氧输送管（12）相连通，第三压缩空气输送支管（9）的出口端和塔底蒸发器（11）的热源通道相连通，下塔（4）和填料塔（10）通过污液氮输送管（13）相连通。1. A variable load air separation and distillation device, comprising a main distillation tower and a compressed air delivery main pipe (1), wherein the main distillation tower comprises an upper tower (2), a main condensing heat exchanger (3) and a lower tower (4) from top to bottom, characterized in that: the compressed air delivery main pipe (1) is provided with an inlet end of a first compressed air delivery branch pipe (5), a booster end of a turbine expander (6), a post-machine heat exchanger (7), an inlet end of a second compressed air delivery branch pipe (8) and an inlet end of a third compressed air delivery branch pipe (9), an outlet end of the second compressed air delivery branch pipe (8) and a booster end of a turbine expander (6), and a post-machine heat exchanger (7). The expansion end inlet is connected, the expansion end outlet of the turbine expander (6) is connected to the upper tower (2), the outlet end of the first compressed air delivery branch pipe (5) is connected to the lower tower (4), the cold source channel of the main condensing heat exchanger (3) is connected to the auxiliary distillation tower, the auxiliary distillation tower comprises a packing tower (10) and a tower bottom evaporator (11) arranged at the bottom end of the packing tower (10), the cold source channel of the tower bottom evaporator (11) and the cold source channel of the main condensing heat exchanger (3) are connected through a crude oxygen delivery pipe (12), the outlet end of the third compressed air delivery branch pipe (9) is connected to the heat source channel of the tower bottom evaporator (11), and the lower tower (4) and the packing tower (10) are connected through a dirty liquid nitrogen delivery pipe (13). 2.根据权利要求1所述的变负荷空分精馏装置，其特征在于：所述的第一压缩空气输送支管（5）、第二压缩空气输送支管（8）和第三压缩空气输送支管（9）上均分别设置有第一调节阀（14）和第一气体流量传感器（15）。2. The variable load air separation and distillation device according to claim 1 is characterized in that: the first compressed air delivery branch pipe (5), the second compressed air delivery branch pipe (8) and the third compressed air delivery branch pipe (9) are respectively provided with a first regulating valve (14) and a first gas flow sensor (15). 3.根据权利要求1所述的变负荷空分精馏装置，其特征在于：所述的主冷凝换热器（3）的热源通道出口上设置有液氮输送主管（16），液氮输送主管（16）沿着靠近主冷凝换热器（3）至远离主冷凝换热器（3）的方向上依次设置有第一液氮回流管（17）的进口端、第二液氮回流管（18）的进口端和第二调节阀（19），第一液氮回流管（17）和第二液氮回流管（18）上均分别设置有第三调节阀（20），下塔（4）的顶部和主冷凝换热器（3）的热源通道进口相连通，第一液氮回流管（17）的出口端和下塔（4）顶部相连通，第二液氮回流管（18）的出口端和上塔（2）顶部相连通，下塔（4）和上塔（2）上设置有富氧液空输送管（21），富氧液空输送管（21）上设置有第四调节阀（22）。3. The variable load air separation and distillation device according to claim 1, characterized in that: a liquid nitrogen delivery main pipe (16) is arranged at the outlet of the heat source channel of the main condensing heat exchanger (3), and the liquid nitrogen delivery main pipe (16) is provided with an inlet end of a first liquid nitrogen reflux pipe (17), an inlet end of a second liquid nitrogen reflux pipe (18) and a second regulating valve (19) in sequence along the direction from close to the main condensing heat exchanger (3) to far away from the main condensing heat exchanger (3), and the first liquid nitrogen reflux pipe (17) and the inlet end of the second liquid nitrogen reflux pipe (18) and the second regulating valve (19) are arranged. The two liquid nitrogen reflux pipes (18) are each provided with a third regulating valve (20); the top of the lower tower (4) is connected to the heat source channel inlet of the main condensing heat exchanger (3); the outlet end of the first liquid nitrogen reflux pipe (17) is connected to the top of the lower tower (4); the outlet end of the second liquid nitrogen reflux pipe (18) is connected to the top of the upper tower (2); oxygen-enriched liquid air delivery pipes (21) are provided on the lower tower (4) and the upper tower (2); and fourth regulating valves (22) are provided on the oxygen-enriched liquid air delivery pipes (21). 4.根据权利要求3所述的变负荷空分精馏装置，其特征在于：所述的污液氮输送管（13）的进口端位于第一压缩空气输送支管（5）的出口端和第一液氮回流管（17）的出口端之间，污液氮输送管（13）上设置有第五调节阀（23），塔底蒸发器（11）的热源通道出口上设置有液化空气输送管（24）的进口端，污液氮输送管（13）的进口端与第一压缩空气输送支管（5）的出口端之间的下塔（4）和液化空气输送管（24）的出口端相连通，液化空气输送管（24）上设置有第六调节阀（25）。4. The variable load air separation and distillation device according to claim 3, characterized in that: the inlet end of the dirty liquid nitrogen delivery pipe (13) is located between the outlet end of the first compressed air delivery branch pipe (5) and the outlet end of the first liquid nitrogen reflux pipe (17), a fifth regulating valve (23) is provided on the dirty liquid nitrogen delivery pipe (13), the inlet end of the liquefied air delivery pipe (24) is provided at the outlet of the heat source channel of the tower bottom evaporator (11), the lower tower (4) and the outlet end of the liquefied air delivery pipe (24) are connected between the inlet end of the dirty liquid nitrogen delivery pipe (13) and the outlet end of the first compressed air delivery branch pipe (5), and a sixth regulating valve (25) is provided on the liquefied air delivery pipe (24). 5.根据权利要求3所述的变负荷空分精馏装置，其特征在于：所述的上塔（2）上设置有污氮气输送主管（26），第一液氮回流管（17）的进口端和第二液氮回流管（18）之间的液氮输送主管（16）、富氧液空输送管（21）和污氮气输送主管（26）上设置有过冷器（27），填料塔（10）的塔顶上设置有污氮气输送支管（28）的进口端，过冷器（27）与上塔（2）之间的污氮气输送主管（26）和污氮气输送支管（28）的出口端相连通。5. The variable load air fractionation and distillation device according to claim 3, characterized in that: a dirty nitrogen gas delivery main pipe (26) is provided on the upper tower (2), a subcooler (27) is provided on the inlet end of the first liquid nitrogen reflux pipe (17), the liquid nitrogen delivery main pipe (16) between the second liquid nitrogen reflux pipe (18), the oxygen-enriched liquid air delivery pipe (21) and the dirty nitrogen gas delivery main pipe (26), the inlet end of the dirty nitrogen gas delivery branch pipe (28) is provided on the top of the packed tower (10), and the outlet end of the subcooler (27) and the dirty nitrogen gas delivery main pipe (26) and the dirty nitrogen gas delivery branch pipe (28) between the upper tower (2) are connected. 6.根据权利要求1所述的变负荷空分精馏装置，其特征在于：所述的填料塔（10）的底部上设置有氧气输送主管（29），氧气输送主管（29）沿着靠近填料塔（10）至远离填料塔（10）的方向依次设置有在线色谱分析仪（30）、氧气输送支管（31）、第七调节阀（32）和第二气体流量传感器（33），氧气输送支管（31）上设置有第八调节阀（34）和第三气体流量传感器（35），塔底蒸发器（11）冷源通道的底部设置有液氧输送管（36），液氧输送管（36）上设置有第九调节阀（37）。6. The variable load air separation and distillation device according to claim 1, characterized in that: an oxygen delivery main pipe (29) is arranged at the bottom of the packed tower (10), and an online chromatograph (30), an oxygen delivery branch pipe (31), a seventh regulating valve (32) and a second gas flow sensor (33) are arranged in sequence on the oxygen delivery main pipe (29) along the direction from close to the packed tower (10) to far away from the packed tower (10), an eighth regulating valve (34) and a third gas flow sensor (35) are arranged on the oxygen delivery branch pipe (31), and a liquid oxygen delivery pipe (36) is arranged at the bottom of the cold source channel of the tower bottom evaporator (11), and a ninth regulating valve (37) is arranged on the liquid oxygen delivery pipe (36). 7.根据权利要求1所述的变负荷空分精馏装置，其特征在于：所述的塔底蒸发器（11）的冷源通道、主冷凝换热器（3）的冷源通道和下塔（4）的底部上均分别设置有液位传感器（38），所述的污液氮输送管（13）上设置有液体流量传感器（39）。7. The variable load air separation distillation device according to claim 1, characterized in that: the cold source channel of the bottom evaporator (11), the cold source channel of the main condensing heat exchanger (3) and the bottom of the lower tower (4) are respectively provided with liquid level sensors (38), and the dirty liquid nitrogen delivery pipe (13) is provided with a liquid flow sensor (39).
CN202421307247.3U 2024-06-11 2024-06-11 Variable-load air separation rectifying device Active CN222761237U (en)

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