CN214333201U - Low-coupling multi-strand composite expansion air separation flow device - Google Patents
Low-coupling multi-strand composite expansion air separation flow device Download PDFInfo
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- CN214333201U CN214333201U CN202022445511.8U CN202022445511U CN214333201U CN 214333201 U CN214333201 U CN 214333201U CN 202022445511 U CN202022445511 U CN 202022445511U CN 214333201 U CN214333201 U CN 214333201U
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- 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
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- 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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
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- 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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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- 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
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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- 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
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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- 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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
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- 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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
- F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
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- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
A low-coupling multi-stream composite expansion air separation flow device comprises a raw material compression system, a precooling and purifying system and a low-temperature separation system, wherein the raw material compression system comprises an air compressor and a supercharger; the precooling and purifying system comprises an air cooling tower, a water chilling unit, a cooling water pump, a chilled water pump, a purifier and a purifier; the low-temperature separation system comprises a high-temperature booster expansion machine, a low-temperature booster expansion machine, a main heat exchanger, a subcooler, a lower tower, a main condensation evaporator, an upper tower, a crude argon condenser, a fine argon tower, a fine argon condenser and a fine argon evaporator. The utility model discloses when liquid output is less than the design value, when the operating mode changes, can realize through closing 1-2 shares of fluid. Therefore, the problem that the low-load operation of the unit cannot be achieved or the low-load operation efficiency is low is avoided, the problem of variable working conditions is solved, and the unit energy consumption of liquid production under the low-load working conditions is optimized.
Description
Technical Field
The utility model relates to an empty flow of dividing of compound inflation of many strand flows of low coupling mainly is applicable to production multiple pressure oxygen and pressure nitrogen gas product, can produce more liquid nitrogen, liquid oxygen, liquid argon liquid product simultaneously, belongs to cryogenic air separation technical field.
Background
The main products of the air separation device are oxygen and nitrogen, and the air separation device is widely applied to the fields of metallurgy, steel, energy chemical industry, electronic chemistry, machinery and the like. The steel industry is one of the national important raw material industries, an air separation device matched with the steel industry needs to meet the requirements of oxygen and nitrogen products required by steel mills, and can also produce liquid products for peripheral requirements, and the requirements of the market on liquid oxygen and liquid nitrogen are continuously increased along with the development of the manufacturing industry, particularly the development of coastal shipbuilding industry and electronic industry. Adopt built-in liquefaction of interior compression flow, produce a large amount of liquid in the time of pressure oxygen and pressure nitrogen gas product, can satisfy the demand of peripheral market to the liquid product like this, also can reduce the unit energy consumption of oxygen product, the liquid demand often relies on the development of market fluctuation and economic situation, can present periodic fluctuation usually, the fluctuation of liquid output is stable to whole air separation plant's operation, operating mode regulation and energy consumption optimization all have certain influence, the empty flow of dividing of research low energy consumption low coupling nature has important meaning, it can be adjusted according to the liquid market is undulant in a flexible way to realize air separation plant.
Disclosure of Invention
The utility model discloses in order to overcome prior art's not enough, and designed a simple structure, the utilization efficiency is high, the empty flow arrangement that divides of the compound inflation of low coupling multiple stream of with low costs, in order to realize the utility model discloses a low coupling multiple stream compound inflation empty flow arrangement that divides of purpose, the device includes feed gas compression system, precooling and purification system and low temperature separation system, feed gas compression system include air compressor and booster compressor; the pre-cooling and purifying system comprises an air cooling tower, a water chilling unit, a cooling water pump and a freezing water pump; first clarifier, second clarifier, the cryogenic separation system include high temperature pressure boost expander, low temperature pressure boost expander, main heat exchanger, subcooler, lower tower, main condensation evaporimeter, go up the tower, crude argon condenser, smart argon tower, smart argon condenser, smart argon evaporimeter.
Preferably, the method comprises the following steps: the air compressor is connected with a cooling tower and a water cooling tower, wherein the cooling tower and the water cooling tower are respectively connected with a water chilling unit through a cooling water pump, a chilled water pump, the cooling tower is respectively provided with a first purifier and a second purifier, the rear parts of the first purifier and the second purifier are connected with a lower tower in a heat exchanger through a pipeline, and the other pipeline is connected with a supercharger.
Preferably, the method comprises the following steps: the rear part of the supercharger is respectively connected with a heat exchanger, a low-temperature expander supercharging end and a high-temperature expander supercharging end through three pipelines, the low-temperature expander supercharging end is supercharged and cooled and then enters a heat exchanger, the cooled and then pumped out to the low-temperature expander for expansion and then enters a lower tower, the high-temperature expander supercharging end is supercharged and then enters the heat exchanger, one part of the high-temperature expander supercharging end is cooled to be liquid air and throttled and then sent to the lower tower, the other part of the high-temperature expander is cooled to a certain temperature through the heat exchanger and then pumped into the high-temperature expander for expansion, the expanded air enters the heat exchanger to be further cooled to be close to the dew point temperature and enters the lower tower for rectification, the high-temperature expander and the low-temperature expander are designed in parallel, the device is adjusted more flexibly, and 1 or 2 expanders can be closed when the liquid yield is low.
Preferably, the method comprises the following steps: the lower tower is connected with a liquid nitrogen pump and a subcooler, the upper tower is connected with the upper tower, the upper tower is connected with a crude argon tower, a crude argon condenser is arranged above the crude argon tower and is connected with a refined argon tower, a refined argon evaporator is arranged below the refined argon tower, the main condensation evaporator is connected with a liquid oxygen pump, and the liquid oxygen pump is connected with a heat exchanger.
The utility model discloses a pressure of gas product, the configuration of unit is closely relevant in liquid output and the empty device, be different from 1 strand in the empty flow of dividing of conventional, 2 strand flow expansion refrigeration and heat transfer, introduce the empty flow of dividing of the compound inflation of the many strand flows of low coupling, adopt height promptly, the compound stream of low temperature expander and two strands of high pressure expansions carries out parallel design, utilize and exceed 4 strand fluidic compound expansions, utilize the air to expand under the different temperatures and externally do work, provide cold volume for air separation and liquid production, make the heat transfer difference in temperature of heat exchanger more even, the total difference in temperature is littleer, thereby make energy loss reduce by a wide margin. When the liquid yield is lower than the designed value and the working condition is changed, the working condition can be changed by closing 1-2 flows. Therefore, the problem that the low-load operation of the unit cannot be achieved or the low-load operation efficiency is low is avoided, the problem of variable working conditions is solved, and the unit energy consumption of liquid production under the low-load working conditions is optimized.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings, and as shown in fig. 1, a low-coupling multi-flow composite expansion air separation process apparatus includes a raw material gas compression system, a pre-cooling and purifying system and a low-temperature separation system, where the raw material gas compression system includes an air compressor C01 and a supercharger C05; the precooling and purifying system comprises an air cooling tower E20, a water cooling tower E21, a water chilling unit R20, a cooling water pump P20, a chilled water pump P21, a purifier R01 and a purifier R02; the low-temperature separation system comprises a high-temperature booster expansion machine ETC1-ET01, a low-temperature booster expansion machine ETC2-ET02, a main heat exchanger E01, a subcooler E03, a lower tower T01, a main condensation evaporator E02, an upper tower T02, a crude argon tower T10, a crude argon condenser E10, a fine argon tower T11, a fine argon condenser E16 and a fine argon evaporator E15.
Preferably, the method comprises the following steps: the air compressor C01 is connected with a cooling tower E20 and a water cooling tower E21, wherein the cooling tower E20 and the water cooling tower E21 are respectively connected with a water chilling unit R20 through a cooling water pump P20 and a cooling water pump P21, the cooling tower E20 is respectively connected with a first purifier R01 and a second purifier R02 which are connected in parallel, the rear parts of the first purifier R01 and the second purifier R02 are connected with a heat exchanger E01 through a pipeline, and the other pipeline is connected with a supercharger C05.
Preferably, the method comprises the following steps: the rear part of the supercharger C05 is respectively connected with a heat exchanger E01, a low-temperature expander supercharging end ETC2 and a high-temperature expander supercharging end ETC1 through three pipelines, the low-temperature expander supercharging end ETC2 is supercharged and cooled and then enters a heat exchanger E01, the cooled and extracted heat is extracted to a low-temperature expander ET2 to be expanded and then enters a lower tower T01, the high-temperature expander supercharging end ETC1 is supercharged and then enters a heat exchanger E01, one part of the liquefied air is liquefied into liquid air and throttled and then sent to the lower tower T01, the other part of the liquefied air is cooled to a certain temperature through a heat exchanger E01 and then is extracted to a high-temperature expander ET1 to be expanded, the expanded air enters the heat exchanger to be further cooled to be close to a dew point temperature and then enters a lower tower T01 to be rectified, the high-temperature expander ET01 and the low-temperature expander ET02 are designed in parallel, the device is more flexible to adjust, and 1 or 2 expanders can be closed when the liquid yield is low.
Preferably, the method comprises the following steps: lower tower T01 connects liquid nitrogen pump P05 and subcooler E03, and this E03 connects upper tower T02, and upper tower T02 connects crude argon tower T10, crude argon tower T10 top is equipped with crude argon condenser E10, and this crude argon condenser E10 is connected with fine argon tower T11, fine argon tower T11 below is equipped with fine argon evaporator E15, main condensation evaporator E02 connects liquid oxygen pump P03, and liquid oxygen pump P03 is connected with heat exchanger E01.
A method for a low-coupling multi-strand composite expansion air separation process comprises the following steps:
step 1: the raw air is pressurized to a certain pressure by an air compressor C01, and then the temperature of the raw air is reduced to a certain temperature by an air cooling tower E20. The air cooling tower E20 is a two-stage structured packing tower, and the bottom of the tower is provided with a stainless steel packing with a certain height. Cooling water from a circulating water system and chilled water further cooled by a water cooling tower E21 and a water chilling unit R20 are directly contacted with air for fractional cooling. The cooled processing air enters a purifier R01 to absorb and remove residual moisture, carbon dioxide and hydrocarbon, wherein the dew point of the moisture in the air at the outlet of the purifier R01 is less than or equal to-70 ℃ and the carbon dioxide is less than 1 ppm.
Step 2: a portion of the dry, clean air is passed directly to exchanger E01 to cool to near the dew point and into lower column T01. The rest gas is compressed by an air booster C05 and then divided into three parts, wherein one part of air is directly sent into a heat exchanger E01 to provide gasification heat for liquid oxygen and liquid nitrogen, and the air is cooled into liquid air which is then sent into a lower tower T01. One of the two streams enters a low-temperature expansion machine pressurization end ETC2, is subjected to pressurization cooling and then enters a heat exchanger E01, is cooled to a certain temperature, is pumped out to a low-temperature expansion machine ET2 for expansion, and enters a lower tower T01 after expansion; and the last air is pressurized by a pressurizing end ETC1 of the high-temperature expansion machine and then enters a heat exchanger E01, one part of the air is liquefied into liquid air and throttled, the liquid air and throttled are sent to a lower tower T01, the other part of the air is cooled to a certain temperature by a heat exchanger E01 and then pumped into a high-temperature expansion machine ET1 for expansion, the expanded air enters the heat exchanger for further cooling to be close to the dew point temperature, and then enters a lower tower T01 for rectification. The high-temperature expander ET01 and the low-temperature expander ET02 are designed in parallel, the device is more flexibly adjusted, and 1 or 2 expanders can be closed when the liquid yield is low.
And step 3: liquid nitrogen with high purity is obtained from the top of the lower tower T01, part of the liquid is pumped to the required pressure through a liquid nitrogen pump P05 and sent to a heat exchanger E01 to exchange heat with high-pressure air, and the liquid nitrogen is gasified into a pressure nitrogen product and sent to a nitrogen product pipe network. And after the rest liquid nitrogen passes through a cooler E03, throttling the rest liquid nitrogen into an upper tower T02 to provide reflux liquid for the rectification of the upper tower, and pumping out part of the liquid nitrogen as a liquid product to be sent into a downstream storage and backup system. The oxygen-enriched liquid at the bottom of the lower tower T01 passes through a cooler E03 and is throttled to enter the upper tower T02 to participate in rectification. The main condensing evaporator E02 obtains liquid oxygen with higher purity, and a proper amount of liquid oxygen is pumped to the required pressure through the liquid oxygen pump P03 and sent into the heat exchanger E01 to exchange heat with high-pressure air, and is gasified into a pressure oxygen product which is sent into an oxygen product pipe network. Part of the liquid oxygen is subcooled by cooler E03 and sent to the downstream storage and backup system as liquid product. Oxygen-enriched gas is extracted from the middle part of the upper tower T02 and is used as raw material gas of the crude argon tower T10, and the oxygen-enriched liquid air and the ascending crude argon exchange heat in a crude argon condenser E10 to provide cold energy for the crude argon tower T10. The crude argon condenser E10 obtains crude argon liquid with oxygen purity of 2ppm, and the crude argon liquid is sent into a fine argon tower T11 for further rectification and nitrogen removal. The argon rectification evaporator E15 provides heat for rectification, the argon rectification condenser E16 provides cold for rectification, and a pure liquid argon product is obtained at the bottom of the argon rectification tower T11 and is sent to a downstream storage system.
Claims (4)
1. A low coupling multi-stream composite expansion air separation flow device comprises a raw material gas compression system, a precooling and purifying system and a low-temperature separation system, and is characterized in that the raw material gas compression system comprises an air compressor and a supercharger; the precooling and purifying system comprises an air cooling tower, a water chilling unit, a cooling water pump, a chilled water pump, a first purifier and a second purifier; the low-temperature separation system comprises a high-temperature booster expansion machine, a low-temperature booster expansion machine, a main heat exchanger, a subcooler, a lower tower, a main condensation evaporator, an upper tower, a crude argon condenser, a fine argon tower, a fine argon condenser and a fine argon evaporator.
2. The low-coupling multi-stream composite expansion air separation flow process device according to claim 1, characterized in that the air compressor is connected with a cooling tower and a water cooling tower which are connected in parallel, wherein the cooling tower and the water cooling tower are respectively connected with a water chilling unit through a cooling water pump and a chilled water pump, the cooling tower is respectively connected with a first purifier and a second purifier which are connected in parallel, the rear parts of the first purifier and the second purifier are directly connected with a heat exchanger through a pipeline, and the other pipeline is connected with a supercharger.
3. The low-coupling multi-stream composite expansion air separation process device according to claim 2, characterized in that the rear of the supercharger is connected with a heat exchanger, a low-temperature expander supercharging end and a high-temperature expander supercharging end through three pipelines, respectively, the low-temperature expander supercharging end is supercharged and cooled and then enters a heat exchanger, the cooled and then pumped out to the low-temperature expander for expansion, the expanded and then enters a lower tower, the high-temperature expander supercharging end is supercharged and then enters the heat exchanger, one part of the air is cooled to liquid air and throttled and then sent to the lower tower, the other part of the air is cooled to a certain temperature through the heat exchanger and then pumped into the high-temperature expander for expansion, the expanded air enters the heat exchanger for further cooling to a temperature close to a dew point, the air enters the lower tower for rectification, the high-temperature expander and the low-temperature expander are designed in parallel, and when the liquid yield is low, 1 or 2 expanders can be closed.
4. The low-coupling multi-strand composite expansion air separation process device according to claim 3, wherein the lower tower is connected with a liquid nitrogen pump and a subcooler, the subcooler is connected with the upper tower, the upper tower is connected with a crude argon tower, a crude argon condenser is arranged above the crude argon tower and is connected with a fine argon tower, a fine argon evaporator is arranged below the fine argon tower, the main condensation evaporator is connected with a liquid oxygen pump, and the liquid oxygen pump is connected with a heat exchanger.
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| CN202022445511.8U CN214333201U (en) | 2020-10-29 | 2020-10-29 | Low-coupling multi-strand composite expansion air separation flow device |
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| CN202022445511.8U CN214333201U (en) | 2020-10-29 | 2020-10-29 | Low-coupling multi-strand composite expansion air separation flow device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112229142A (en) * | 2020-10-29 | 2021-01-15 | 浙江智海化工设备工程有限公司 | Low-coupling multi-strand composite expansion air separation flow device and method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112229142A (en) * | 2020-10-29 | 2021-01-15 | 浙江智海化工设备工程有限公司 | Low-coupling multi-strand composite expansion air separation flow device and method |
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Address after: No. 280 Xingye Road, Leidian Town, Deqing County, Huzhou City, Zhejiang Province, 313219 Patentee after: Yingde Gas Engineering (Zhejiang) Co.,Ltd. Address before: 313219 Jingyi Road, Deqing Linhang Industrial Zone, LEIDIAN Town, Deqing County, Huzhou City, Zhejiang Province Patentee before: ZHEJIANG ZHIHAI CHEMICAL EQUIPMENT ENGINEERING Co.,Ltd. |
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