CN217952862U - Air separation rectifying device - Google Patents
Air separation rectifying device Download PDFInfo
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- CN217952862U CN217952862U CN202221848207.0U CN202221848207U CN217952862U CN 217952862 U CN217952862 U CN 217952862U CN 202221848207 U CN202221848207 U CN 202221848207U CN 217952862 U CN217952862 U CN 217952862U
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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
- F25J3/04248—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
Abstract
The utility model relates to an empty rectifier unit that divides, including the rectifying column, main heat exchanger, the air feed is responsible for and first booster unit, the rectifying column includes the tower, main condensation heat exchanger and lower tower, be equipped with first turboexpander on the first booster unit, be equipped with the circulating gas on the main heat exchanger and be responsible for, the air feed is responsible for and is linked together with lower tower, be equipped with the choke valve on the air feed is responsible for between lower tower and the main heat exchanger, the air feed in the main heat exchanger is responsible for and is linked together through first air feed branch pipe with first turboexpander, first turboexpander is linked together through second air feed branch pipe with lower tower, the air feed that the air feed was responsible for between inlet end and the first booster unit is responsible for and is linked together through the circulating gas with second air feed branch pipe, the circulating gas is responsible for and is equipped with first governing valve on the second air feed branch pipe between the lower tower. The utility model discloses be convenient for adjust the rectifying column's rectification operating mode, the utility model discloses adjust, convenient to use has extensive market prospect.
Description
Technical Field
The utility model relates to an empty rectification field that divides, concretely relates to empty rectification device that divides.
Background
Air separation, referred to as air separation, is a process of separating its components (oxygen, nitrogen and rare gases such as argon and helium) from air using the principle of cryogenic refrigeration, generally by first compressing the air and cooling it to a very low temperature or liquefying it by expansion, and then separating it in a rectification column. For example, when liquid air is boiling, nitrogen (boiling point-196 ℃ C.) which is relatively volatile vaporizes first, and oxygen (boiling point-183 ℃ C.) vaporizes later. The working principle of the air separation equipment is that according to the different boiling points of various gases in the air, the gases are pressurized, precooled and purified, and most of the cold energy provided by the turbine expansion agent is utilized to liquefy the gases and then rectify the liquids to obtain the required oxygen/nitrogen products. The air oxygen generation system comprises an air compressor system, a precooling system, a molecular sieve purification system, a pressurizing expansion agent system, a fractionating tower system, an oxygen/nitrogen compressor system and a pressure regulating station system.
The liquid target product and the gaseous target product can be conveyed outwards through the rectifying tower in the prior art, but the rectification working condition in the rectifying tower needs to be adjusted according to different proportions of the target product required in different time periods, and after a target process is formulated in the prior art, the corresponding rectification working condition is not easy to adjust so as to adjust the proportion of the target product, so that the process in the prior art is difficult to overcome under the background that the proportion supply of the target product needs to be changed and supplied, and equipment thereof has disadvantages.
Disclosure of Invention
The utility model provides a not enough to prior art, the utility model provides a can adjust the empty rectifier unit that divides of rectifying column's rectification operating mode simultaneously for overcome defect among the prior art.
The utility model discloses a technical scheme do: the utility model provides an empty rectifier unit that divides, includes the rectifying column, be used for gas exchange's main heat exchanger, the air feed person in charge of and the air feed person in charge of the first booster unit of installation on main heat exchanger, the rectifying column includes tower, main condensation heat exchanger and lower tower, first booster unit on be provided with first turboexpander, be provided with the circulating gas person in charge on the main heat exchanger, the exit end that the air feed is responsible for is linked together with lower tower, be provided with the choke valve on the air feed person in charge between lower tower and the main heat exchanger, the air feed person in charge in the main heat exchanger is linked together through first air feed branch pipe with the inlet end of first turboexpander, the end of giving vent to anger of first turboexpander is linked together through second air feed branch pipe with lower tower, the air feed person in charge between inlet end that the air feed is responsible for and the first booster unit is responsible for through the circulating gas with the second air feed branch pipe and is provided with first governing valve on the second air feed branch pipe between circulating gas person in charge and the lower tower.
Preferably, the main heat exchanger is provided with a third air supply branch pipe, the air supply main pipe between the first booster set and the main heat exchanger is provided with a second booster set, the second booster set is provided with a second turboexpander, the air supply main pipe between the circulating air main pipe and the first booster set is communicated with the air inlet end of the second turboexpander through the third air supply branch pipe, the second turboexpander is communicated with the circulating air main pipe in the main heat exchanger, and the air supply main pipe between the circulating air main pipe and the third air supply branch pipe is provided with a third booster set.
Preferably, the main condensing heat exchanger on be provided with high-pressure liquid nitrogen conveyer pipe and finished product liquid oxygen conveyer pipe, be linked together through oxygen-enriched liquid air conveyer pipe between the bottom of lower tower and the last tower, be linked together through oxygen-enriched air conveyer pipe between the lower tower of oxygen-enriched liquid air conveyer pipe top and the last tower, be provided with finished product nitrogen gas conveyer pipe on the top of last tower, high-pressure liquid nitrogen conveyer pipe, oxygen-enriched liquid air conveyer pipe, be provided with first subcooler on oxygen-enriched air conveyer pipe and the finished product nitrogen gas conveyer pipe, be provided with the second subcooler on finished product nitrogen gas conveyer pipe between the exit end of finished product nitrogen gas conveyer pipe and the first subcooler and the finished product liquid oxygen conveyer pipe, be provided with the flash drum on the exit end of high-pressure liquid nitrogen conveyer pipe, be provided with finished product liquid nitrogen gas conveyer pipe on the flash drum bottom, finished product nitrogen gas conveyer pipe between first subcooler and the second subcooler and the top of flash drum are linked together through flash drum nitrogen gas conveyer pipe.
Preferably, the main circulating gas pipe between the main heat exchanger and the main gas supply pipe between the third booster set and the third gas supply branch pipe are respectively provided with a temperature sensor, and the second gas supply branch pipe between the main circulating gas pipe and the first turboexpander is provided with a pressure sensor.
Preferably, the second regulating valve and the first gas flow sensor are respectively arranged on the gas supply main pipe between the third gas supply branch pipe and the first booster set and the third gas supply branch pipe between the gas supply main pipe and the main heat exchanger.
Preferably, the main heat exchanger is provided with a finished product oxygen conveying pipe, the air inlet end of the finished product oxygen conveying pipe is communicated with the upper tower, and the finished product oxygen conveying pipe, the finished product nitrogen conveying pipe, the finished product liquid nitrogen conveying pipe and the finished product liquid oxygen conveying pipe are respectively provided with a first online chromatograph.
Preferably, a second online chromatograph is arranged on the oxygen-enriched liquid air conveying pipe between the first subcooler and the lower tower, and a third regulating valve and a second gas flow sensor are arranged on the oxygen-enriched air conveying pipe between the first subcooler and the lower tower.
The utility model has the advantages that: firstly, the utility model discloses an adjust the aperture of choke valve and the aperture of first governing valve can adjust the rectifying column's rectification operating mode, convenient to use.
Secondly, the utility model is provided with a first gas flow sensor on the installation gas supply main pipe, which is convenient for feeding back the flow parameter of the compressed air which is transmitted to the first booster set through the gas supply main pipe; the installation of the first gas flow sensor in the third gas supply branch facilitates feedback of a flow parameter of the compressed air delivered to the second turboexpander through the third gas supply branch.
Finally, the utility model discloses it does not be provided with first online chromatograph to equally divide on finished product oxygen conveyer pipe, finished product nitrogen gas conveyer pipe, finished product liquid nitrogen conveyer pipe and the finished product liquid oxygen conveyer pipe. The first on-line chromatograph facilitates feedback of the component parameters.
The utility model has the advantages of simple structure, convenient operation, design benefit has improved work efficiency greatly, has fine social and economic benefits, is the product of easily using widely.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
As shown in fig. 1, an air separation rectification apparatus includes a rectification column, a main heat exchanger 1 for gas exchange, a main gas supply pipe 2 installed on the main heat exchanger 1, a first booster set 3 installed on the main gas supply pipe 2, and a cold box 36, where the rectification column includes an upper column 4, a main condensation heat exchanger 5, and a lower column 6, a heat source channel of the main condensation heat exchanger 5 is communicated with the lower column 6, and a cold source channel of the main condensation heat exchanger 5 is communicated with the upper column 4, generally, a corresponding pressure sensor and a corresponding temperature sensor are installed in the lower column 6 in the prior art, and a liquid level sensor is also installed at the bottom of the lower column 6 to feed back a liquid level of an oxygen-enriched liquid atmosphere at the bottom of the lower column 6, which is not identified in the schematic diagram in order to avoid redundancy.
The main heat exchanger 1 is provided with a third air supply branch pipe 13, the air supply main pipe 2 between the first booster set 3 and the main heat exchanger 1 is provided with a second booster set 14, the second booster set 14 is provided with a second turbo expander 15, the air supply main pipe 2 between the circulating air main pipe 8 and the first booster set 3 is communicated with the air inlet end of the second turbo expander 15 through the third air supply branch pipe 13, the second turbo expander 15 is communicated with the circulating air main pipe 8 in the main heat exchanger 1, and the air supply main pipe 2 between the circulating air main pipe 8 and the third air supply branch pipe 13 is provided with a third booster set 16. The air feed between first booster unit 3 and the second booster unit 14 is responsible for on 2 and the air feed between second booster unit 14 and main heat exchanger 1 is responsible for on 2 and equally divide and do not is provided with the heat exchanger, the cold source of heat exchanger adopt the circulating water.
The gas supply main pipe 2 between the third gas supply branch pipe 13 and the first booster set 3 and the third gas supply branch pipe 13 between the gas supply main pipe 2 and the main heat exchanger 1 are respectively provided with a second regulating valve 29 and a first gas flow sensor 30. The installation of the first gas flow sensor 30 on the installation gas supply main pipe 2 facilitates the feedback of the flow parameter of the compressed air delivered to the first booster set 3 through the installation gas supply main pipe 2; the installation of the first gas flow sensor 30 in the third gas supply branch 13 facilitates feedback of the flow parameter of the compressed air delivered to the second turboexpander 15 through the third gas supply branch 13.
The main condensing heat exchanger 5 on be provided with high-pressure liquid nitrogen conveyer pipe 17 and finished product liquid oxygen conveyer pipe 18, be linked together through oxygen-enriched liquid air conveyer pipe 19 between the bottom of lower tower 6 and the last tower 4, be linked together through oxygen-enriched air conveyer pipe 20 between lower tower 6 of oxygen-enriched liquid air conveyer pipe 19 top and the last tower 4, be provided with finished product nitrogen conveyer pipe 21 on the top of going up tower 4, be provided with first subcooler 22 on high-pressure liquid nitrogen conveyer pipe 17, oxygen-enriched liquid air conveyer pipe 19, oxygen-enriched air conveyer pipe 20 and the finished product nitrogen conveyer pipe 21. Wherein the high-pressure liquid nitrogen delivery pipe 17, the oxygen-enriched liquid air delivery pipe 19 and the oxygen-enriched air delivery pipe 20 are all used as heat sources of a first subcooler 22, and the finished product nitrogen delivery pipe 21 is used as a cold source of the first subcooler 22; the second subcooler 23 is arranged on the finished product nitrogen conveying pipe 21 and the finished product liquid oxygen conveying pipe 18 between the outlet end of the finished product nitrogen conveying pipe 21 and the first subcooler 22, meanwhile, in order to reduce the temperature of the finished product nitrogen conveyed in the finished product nitrogen conveying pipe 21 after heat exchange through the first subcooler 22, the flash tank 24 is arranged at the outlet end of the high-pressure liquid nitrogen conveying pipe 17 of the product, a finished product liquid nitrogen conveying pipe 25 is arranged at the bottom end of the flash tank 24, and the finished product nitrogen conveying pipe 21 between the first subcooler 22 and the second subcooler 23 is communicated with the top end of the flash tank 24 through a flash evaporation nitrogen conveying pipe 26. After being cooled by the first subcooler 22, the high-pressure liquid nitrogen conveyed by the high-pressure liquid nitrogen conveying pipe 17 is conveyed to the flash tank 24, the pressure in the flash tank 24 is reduced, the temperature of the high-pressure liquid nitrogen is further reduced due to the pressure reduction after the high-pressure liquid nitrogen enters the flash tank 24, and the high-pressure liquid nitrogen is accompanied by partially vaporized low-temperature nitrogen, and then the low-temperature nitrogen is conveyed to the finished product nitrogen conveying pipe 21 between the first subcooler 22 and the second subcooler 23 through the flash nitrogen conveying pipe 26, so that the finished product nitrogen conveyed in the finished product nitrogen conveying pipe 21 is cooled again before entering the second subcooler 23.
The main circulating gas pipe 8 between the main heat exchanger 1 and the main gas supply pipe 2 between the third booster set 16 and the third gas supply branch pipe 13 are respectively provided with a temperature sensor 27, and the second gas supply branch pipe 11 between the main circulating gas pipe 8 and the first turboexpander 7 is provided with a pressure sensor 28. A pressure sensor 28 is installed to facilitate feedback of pressure parameters of the compressed air fed to the lower tower 6.
Check valves 37 are respectively arranged on the circulating gas main pipe 8 between the second gas supply branch pipe 11 and the main heat exchanger 1, the finished product nitrogen conveying pipe 21 between the first subcooler 22 and the flash evaporation nitrogen conveying pipe 26, and the high-pressure liquid nitrogen conveying pipe 17 between the first subcooler 22 and the flash evaporation tank 24 and the flash evaporation nitrogen conveying pipe 26. The main heat exchanger 1 is provided with a finished product oxygen conveying pipe 31, the air inlet end of the finished product oxygen conveying pipe 31 is communicated with the upper tower 4, and the finished product oxygen conveying pipe 31, the finished product nitrogen conveying pipe 21, the finished product liquid nitrogen conveying pipe 25 and the finished product liquid oxygen conveying pipe 18 are respectively provided with a first online chromatograph 32. The first online chromatograph 32 is installed to facilitate feedback of the corresponding component parameters.
A second on-line chromatograph 33 is arranged on the oxygen-enriched liquid air conveying pipe 19 between the first subcooler 22 and the lower tower 6, and a third adjusting valve 34 and a second gas flow sensor 35 are arranged on the oxygen-enriched air conveying pipe 20 between the first subcooler 22 and the lower tower 6. A third regulating valve 34 and a second gas flow sensor 35 are installed to facilitate the feedback and regulation of the flow parameters of the oxygen-enriched air fed to the upper column 4 through the lower column 6.
The use method of the product is as follows: as shown in fig. 1, the compressed air adsorbed by the molecular sieve adsorption system enters the main air supply pipe 2 and is pressurized by the third booster set 16, and a part of the compressed air is delivered to the second turbo expander 15 through the third air supply branch pipe 13 to be expanded and cooled to be used as a cold source, and then is delivered to the main air supply pipe 2 between the third booster set 16 and the main air supply pipe 2 through the main circulating air pipe 8 after being delivered to the main heat exchanger 1, and is pressurized by the third booster set 16 again to form a cycle. The other part of the air is conveyed continuously through the air supply main pipe 2 and then sequentially pressurized by the first booster set 3 and the second booster set 14 to be used as a heat source to be sent into the main heat exchanger 1.
Wherein, after a part of the compressed air sent into the main heat exchanger 1 is sent into the first turbo expander 7 through the first air supply branch pipe 10 to be expanded and cooled, the compressed air sent through the second air supply branch pipe 11 after being expanded and cooled is divided into two parts, one part is sent into the lower tower 6, and the other part is sent to the air supply main pipe 2 between the third booster set 16 and the air supply main pipe 2 through the circulating air main pipe 8. One part of the compressed air sent into the main heat exchanger 1 is continuously conveyed through the air supply main pipe 2, and when the part of the compressed air completely passes through the main heat exchanger 1, liquid air is formed, throttled and cooled through the throttle valve 9, and then sent into the lower tower 6. The opening degree of the throttle valve 9 during this time can facilitate control of the proportion of the compressed air delivered through the main air supply duct 2 and the first branch air supply duct 10.
The oxygen-enriched liquid air at the bottom of the lower tower 6 is fed back to the component content through the second online chromatograph 33 by the oxygen-enriched air delivery pipe 20, then is used as a first heat source of the first subcooler 22 and a cold source of the first subcooler 22 for heat exchange, and then is delivered to the upper tower 4; when the component content fed back by the second online chromatograph 33 does not reach the preset parameter, the third adjusting valve 34 is opened, the oxygen-enriched air in the lower tower 6 passes through the oxygen-enriched air delivery pipe 20, the flow is fed back by the second gas flow sensor 35, the opening degree of the third adjusting valve 34 is adjusted again to be used as a second heat source of the first subcooler 22, the second heat source exchanges heat with the cold source of the first subcooler 22, then the second heat source and the cold source of the first subcooler 22 are delivered to the upper tower 4, the component content of the oxygen-enriched liquid air is adjusted by delivering the oxygen-enriched air to reduce the pressure of the lower tower 6, and when the component content fed back by the second online chromatograph 33 reaches the preset parameter, the third adjusting valve 34 is closed.
The finished product nitrogen conveyed by the upper tower 4 is conveyed through a finished product nitrogen conveying pipe 21, and is used as a cold source of the first subcooler 22 to exchange heat with a heat source of the first subcooler 22 during the conveying; liquid nitrogen in a heat source passage of the main condensation heat exchanger 5 is conveyed through a high-pressure liquid nitrogen conveying pipe 17, and is used as a third heat source of the first subcooler 22 to exchange heat with a cold source of the first subcooler 22 in the period, the liquid nitrogen is conveyed into the flash tank 24 through the first subcooler 22 to be flashed, and then the low-temperature nitrogen is conveyed into a finished product nitrogen conveying pipe 21 between the first subcooler 22 and the second subcooler 23 to be mixed with the finished product nitrogen heated by the first subcooler 22; the flash-evaporated low-temperature liquid nitrogen is delivered to a user through a finished product liquid nitrogen delivery pipe 25.
The temperature of the mixed finished product nitrogen is reduced, and then the mixed finished product nitrogen is used as a cold source of the second subcooler 23 to exchange heat with a heat source of the second subcooler 23, and then is subjected to heat exchange through the main heat exchanger 1 and is conveyed to a user.
The finished product liquid oxygen in the heat source channel of the main condensing heat exchanger 5 is used as the heat source of the second subcooler 23 through the finished product liquid oxygen conveying pipe 18 and is conveyed to the user after heat exchange with the cold source of the second subcooler 23.
The working condition index of the rectifying tower is adjusted through two aspects, namely, on one hand, liquid air conveyed to the upper tower 4 by the main air supply pipe 2 and pressurized low-temperature air conveyed to the upper tower 4 by the second air supply branch pipe 11 are adjusted, and meanwhile, the second adjusting valve 29 of the main air supply pipe 2, the second adjusting valve 29 of the third air supply branch pipe 13, the first adjusting valve 12 on the second air supply branch pipe 11 and the throttle valve 9 need to be adjusted comprehensively. On the other hand, when the technological index of the oxygen-enriched liquid air needs to be changed, the component parameters of the oxygen-enriched liquid air can be changed by changing the pressure of the oxygen-enriched air on the upper layer of the oxygen-enriched liquid air by adjusting the opening degree of the third adjusting valve 34.
The utility model discloses an empty rectifier unit that divides who satisfies in empty rectification field worker needs makes the utility model discloses extensive market prospect has.
Claims (7)
1. The utility model provides an empty rectifier unit that divides, includes rectifying column, the main heat exchanger (1) that is used for gas exchange, the gas supply of installing is responsible for (2) and the gas supply is responsible for first booster unit (3) of installing on (2) on main heat exchanger (1), and rectifying column includes tower (4), main condensation heat exchanger (5) and lower tower (6), its characterized in that: the first booster set (3) on be provided with first turboexpander (7), be provided with the circulation gas on main heat exchanger (1) and be responsible for (8), the exit end that the air feed was responsible for (2) is linked together with lower tower (6), be provided with choke valve (9) on the air feed that lower tower (6) and main heat exchanger (1) between was responsible for (2), the air feed in main heat exchanger (1) is responsible for (2) and is linked together through first air feed branch pipe (10) with the inlet end of first turboexpander (7), the end of giving vent to anger of first turboexpander (7) is linked together through second air feed branch pipe (11) with lower tower (6), the air feed that the air feed was responsible for (2) is responsible for (2) and air feed between first booster set (3) is responsible for (2) and is responsible for (8) through the circulation gas with second air feed branch pipe (11) and is linked together, be provided with first governing valve (12) on second air feed branch pipe (11) between circulation gas is responsible for (8) and lower tower (6).
2. The air separation rectification plant according to claim 1, characterized in that: the main heat exchanger (1) is provided with a third air supply branch pipe (13), an air supply main pipe (2) between the first booster set (3) and the main heat exchanger (1) is provided with a second booster set (14), the second booster set (14) is provided with a second turbine expansion machine (15), the air supply main pipe (2) between the circulating air main pipe (8) and the first booster set (3) is communicated with the air inlet end of the second turbine expansion machine (15) through the third air supply branch pipe (13), the second turbine expansion machine (15) is communicated with the circulating air main pipe (8) in the main heat exchanger (1), and the air supply main pipe (2) between the circulating air main pipe (8) and the third air supply branch pipe (13) is provided with a third booster set (16).
3. The air separation rectification plant according to claim 1, characterized in that: the main condensing heat exchanger (5) is provided with a high-pressure liquid nitrogen conveying pipe (17) and a finished product liquid oxygen conveying pipe (18), the bottom end of a lower tower (6) is communicated with an upper tower (4) through an oxygen-enriched liquid air conveying pipe (19), the lower tower (6) above the oxygen-enriched liquid air conveying pipe (19) is communicated with the upper tower (4) through an oxygen-enriched air conveying pipe (20), the top end of the upper tower (4) is provided with a finished product nitrogen conveying pipe (21), the high-pressure liquid nitrogen conveying pipe (17), the oxygen-enriched liquid air conveying pipe (19), the oxygen-enriched air conveying pipe (20) and the finished product nitrogen conveying pipe (21) are provided with a first subcooler (22), the outlet end of the finished product nitrogen conveying pipe (21) and the finished product nitrogen conveying pipe (21) between the first subcooler (22) and the finished product liquid oxygen conveying pipe (18) are provided with a second subcooler (23), the outlet end of the high-pressure liquid nitrogen conveying pipe (17) is provided with a flash evaporation tank (24), the bottom end of the flash evaporation tank (24) is provided with a finished product liquid nitrogen conveying pipe (25), and the flash evaporation tank (21) between the first subcooler (22) and the second subcooler (23) are communicated with the top end of the flash evaporation tank (26).
4. The air separation rectification plant according to claim 2, characterized in that: the main heat exchanger (1) and the gas supply are in charge of the circulating gas between (2) and are responsible for (8) and the gas supply between third booster set (16) and third gas supply branch pipe (13) is in charge of (2) and is equallyd divide and be provided with temperature sensor (27) respectively, the circulating gas is in charge of (8) and is provided with pressure sensor (28) on second gas supply branch pipe (11) between first turbo expander (7).
5. The air separation rectification plant according to claim 2, characterized in that: and a second regulating valve (29) and a first gas flow sensor (30) are respectively arranged on the gas supply main pipe (2) between the third gas supply branch pipe (13) and the first booster set (3) and the third gas supply branch pipe (13) between the gas supply main pipe (2) and the main heat exchanger (1).
6. The air separation rectification plant according to claim 3, characterized in that: the main heat exchanger (1) is provided with a finished product oxygen conveying pipe (31), the air inlet end of the finished product oxygen conveying pipe (31) is communicated with the upper tower (4), and the finished product oxygen conveying pipe (31), the finished product nitrogen conveying pipe (21), the finished product liquid nitrogen conveying pipe (25) and the finished product liquid oxygen conveying pipe (18) are respectively provided with a first online chromatograph (32).
7. The air separation rectification plant according to claim 3, characterized in that: and a second online chromatograph (33) is arranged on the oxygen-enriched liquid air conveying pipe (19) between the first subcooler (22) and the lower tower (6), and a third regulating valve (34) and a second gas flow sensor (35) are arranged on the oxygen-enriched air conveying pipe (20) between the first subcooler (22) and the lower tower (6).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221848207.0U CN217952862U (en) | 2022-07-18 | 2022-07-18 | Air separation rectifying device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221848207.0U CN217952862U (en) | 2022-07-18 | 2022-07-18 | Air separation rectifying device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN217952862U true CN217952862U (en) | 2022-12-02 |
Family
ID=84221499
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202221848207.0U Active CN217952862U (en) | 2022-07-18 | 2022-07-18 | Air separation rectifying device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN217952862U (en) |
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2022
- 2022-07-18 CN CN202221848207.0U patent/CN217952862U/en active Active
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