CN115060041A - Liquid-air supercooling reflux expansion double-tower production nitrogen extraction system and method - Google Patents
Liquid-air supercooling reflux expansion double-tower production nitrogen extraction system and method Download PDFInfo
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- CN115060041A CN115060041A CN202210751096.XA CN202210751096A CN115060041A CN 115060041 A CN115060041 A CN 115060041A CN 202210751096 A CN202210751096 A CN 202210751096A CN 115060041 A CN115060041 A CN 115060041A
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 534
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 261
- 238000010992 reflux Methods 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 31
- 238000000605 extraction Methods 0.000 title claims abstract description 15
- 238000004519 manufacturing process Methods 0.000 title claims description 14
- 238000004781 supercooling Methods 0.000 title abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 96
- 238000000746 purification Methods 0.000 claims abstract description 9
- 230000008520 organization Effects 0.000 claims abstract description 5
- 238000001914 filtration Methods 0.000 claims abstract description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 59
- 239000001301 oxygen Substances 0.000 claims description 59
- 229910052760 oxygen Inorganic materials 0.000 claims description 59
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 11
- 238000001704 evaporation Methods 0.000 claims description 10
- 230000008020 evaporation Effects 0.000 claims description 10
- 238000005057 refrigeration Methods 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 7
- 230000008929 regeneration Effects 0.000 claims description 7
- 238000011069 regeneration method Methods 0.000 claims description 7
- 239000002808 molecular sieve Substances 0.000 claims description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 6
- 239000003463 adsorbent Substances 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 239000000945 filler Substances 0.000 claims description 3
- 238000003303 reheating Methods 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 238000007906 compression Methods 0.000 abstract description 3
- 230000006835 compression Effects 0.000 abstract description 3
- 230000008901 benefit Effects 0.000 abstract 2
- 239000002994 raw material Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 3
- 239000013526 supercooled liquid Substances 0.000 description 3
- 230000018109 developmental process Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000005514 two-phase flow Effects 0.000 description 1
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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
- F25J3/0228—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 characterised by the separated product stream
- F25J3/0257—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 characterised by the separated product stream separation of nitrogen
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- 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
- F25J3/04424—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 without thermally coupled high and low pressure columns, i.e. a so-called split columns
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- 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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
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- 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
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- 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.
- F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
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- 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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
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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
- 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
- F25J2205/32—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as direct contact cooling tower to produce a cooled gas stream, e.g. direct contact after cooler [DCAC]
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- 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
- F25J2205/34—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as evaporative cooling tower to produce chilled water, e.g. evaporative water chiller [EWC]
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/02—Internal refrigeration with liquid vaporising loop
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
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- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention provides a liquid-air supercooling reflux expansion double-tower extraction nitrogen-making system and a method, wherein the system comprises an air filtration compression system, an air precooling purification system, a rectification system, a heat exchange system and an expansion system, wherein the rectification system comprises a main nitrogen tower and an auxiliary nitrogen tower; the heat exchange system comprises a main heat exchanger, a main nitrogen tower condenser, an auxiliary nitrogen tower condenser and a subcooler; the expansion system includes an expander having a boost end and an expansion end; the equipment parts are connected through pipelines. The method adopts an organization form of double-tower rectification, landing arrangement and backflow expansion, utilizes a liquid nitrogen pump to pressurize auxiliary nitrogen tower liquid nitrogen and then provides partial reflux liquid for a main nitrogen tower, simultaneously sends partial main nitrogen tower bottom supercooling liquid air and main nitrogen tower condenser liquid air to the auxiliary nitrogen tower to participate in rectification, and provides a cold source for the auxiliary nitrogen tower condenser after the auxiliary nitrogen tower bottom liquid air is supercooled. The method can effectively improve the yield of the nitrogen and the liquid nitrogen, and has the advantages of remarkable economic benefit, simple system, high nitrogen extraction rate, and high operation reliability and safety.
Description
Technical Field
The invention relates to a double-tower production-extracting and nitrogen-producing system, in particular to a liquid-air supercooling reflux expansion double-tower production-extracting and nitrogen-producing system, and further relates to a double-tower production-extracting and nitrogen-producing method, in particular to a liquid-air supercooling reflux expansion double-tower production-extracting and nitrogen-producing system and a method, belonging to the technical field of low-temperature air separation and purification.
Background
With the rapid development of new industries such as semiconductors, electronic information, biological medicines, new materials and the like, particularly the development of power and energy storage battery enterprises, the demand and the scale of the market for high-purity nitrogen are getting stronger, and at present, the low-temperature rectification method is mostly adopted for producing nitrogen on an industrial scale, particularly for medium-large high-purity nitrogen production devices.
The existing double-tower rectification nitrogen-making method and device have the improvement aspect, for example, the patent application number of CN107345737A provides double-tower stacking arrangement, the problems of two-phase flow and arrangement limitation exist, the structure arrangement of the patent application number of CN113310282A is complex, the utilization rate of positive flow expansion energy is low, the patent application number of CN212006434U also has the potential of nitrogen product production improvement, and a liquid-air supercooling reflux expansion double-tower production-improving nitrogen-making system and method are designed to solve the problems.
Disclosure of Invention
The invention mainly aims to provide a liquid-air supercooling reflux expansion double-tower production nitrogen extraction system and a method.
The purpose of the invention can be achieved by adopting the following technical scheme:
a liquid-air supercooling reflux expansion double-tower production-extraction nitrogen-making system adopts a process organization of full-low-pressure molecular sieve adsorption pre-purification, reflux expander refrigeration and double-filler nitrogen tower landing arrangement, and comprises an air filtration compression system, a pre-cooling purification system, a main heat exchanger, a subcooler, a main nitrogen tower condenser, an auxiliary nitrogen tower condenser and a process liquid nitrogen pump;
the main nitrogen tower and the auxiliary nitrogen tower condenser are respectively and compositely installed with the tower device. An oxygen-enriched liquid-air pipeline at the bottom of the main nitrogen tower is sequentially connected with the main heat exchanger, a condenser of the main nitrogen tower and the auxiliary nitrogen tower, a liquid-air pipeline of the condenser of the main nitrogen tower is connected with the auxiliary nitrogen tower, and a liquid-air pipeline at the bottom of the auxiliary nitrogen tower is sequentially connected with the main heat exchanger and the condenser of the auxiliary nitrogen tower;
a nitrogen pipeline of the main nitrogen tower is sequentially connected with the main heat exchanger and the expander, and the oxygen-enriched air evaporated by the main condenser is connected with the auxiliary nitrogen tower;
the oxygen-enriched air of the condenser of the auxiliary nitrogen tower is sequentially connected with the main heat exchanger, the expander, the main heat exchanger and the purification system, and the reflux liquid nitrogen is respectively connected with the subcooler, the process liquid nitrogen pump and the main nitrogen tower.
Preferably, the oxygen-enriched liquid air 1 is subcooled by a main heat exchanger and then divided into two parts, and one part of the oxygen-enriched liquid air enters a condenser of the main nitrogen tower to serve as a cold source; the other part enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling.
Preferably, the pressure nitrogen at the upper part of the main nitrogen tower is reheated by the main heat exchanger, and then is further pressurized by the expander and then is sent to a user.
Preferably, the double rectifying towers are controlled and blocked by a valve to connect the flow paths, and the single rectifying tower and the double rectifying towers are switched to operate.
A liquid-air supercooling reflux expansion double-tower extraction and nitrogen production method comprises the following steps:
s100: the purified air after being filtered, compressed, precooled and purified is cooled by a main heat exchanger and enters the bottom of a main nitrogen tower for rectification;
s200: obtaining oxygen-enriched liquid air 1 at the bottom of the main nitrogen tower, wherein the oxygen-enriched liquid air 1 is subcooled by a main heat exchanger and then is divided into two parts, and one part enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling; one part of the oxygen-enriched air enters a condenser of the main nitrogen tower to be used as a cold source, the other part of the evaporated oxygen-enriched air 1 enters the bottom of the auxiliary nitrogen tower to participate in rectification, and the concentrated oxygen-enriched liquid air 1 enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling;
s300: obtaining pressure nitrogen at the top of the main nitrogen tower, wherein the pressure nitrogen is divided into two parts, one part of the pressure nitrogen enters a condenser of the main nitrogen tower to be used as a heat source and flows back to the main nitrogen tower after being liquefied, and the other part of the pressure nitrogen is reheated by a main heat exchanger and then is pressurized by a pressurizing end of an expander for users;
s400: the bottom of the auxiliary nitrogen tower is provided with an oxygen-enriched liquid air 2, the oxygen-enriched liquid air 2 is subcooled by a main heat exchanger and then enters a condenser of the auxiliary nitrogen tower to be used as a cold source for partial evaporation, the oxygen-enriched air 2 generated by evaporation is reheated by the main heat exchanger and then enters an expander for expansion and refrigeration, the expanded oxygen-enriched air 2 is reheated by the main heat exchanger to the normal temperature and then is divided into two parts to be sent out of a cold box, one part of the air is cooled by a water cooling tower, the other part of the air is used as regeneration gas to be heated by an electric heater and then is used as regeneration gas to regenerate the molecular sieve of the adsorbent;
s500: obtaining low-pressure nitrogen gas at the top of the auxiliary nitrogen tower, wherein the low-pressure nitrogen gas completely enters the auxiliary nitrogen tower condenser to be used as a heat source, is liquefied and then is divided into three parts, and one part of the liquefied low-pressure nitrogen gas reflows to the auxiliary nitrogen tower; one part of the nitrogen enters the upper part of the main nitrogen tower after being pressurized by a liquid nitrogen pump and is used as reflux liquid; the other part is supplied to users after being supercooled by the cooler.
Preferably, in the step S200, the oxygen-enriched liquid air 1 is subcooled by a main heat exchanger and then divided into two parts, and one part directly enters the condenser of the main nitrogen tower to serve as a cold source; the other part enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling.
Preferably, after reheating by the main heat exchanger, the pressure nitrogen is further pressurized by the pressurizing end of the expander, so as to increase the pressure of the nitrogen.
Preferably, the step S300 further includes extracting pressure liquid nitrogen generated by liquefaction in the main condensation evaporator of the main nitrogen tower as a liquid nitrogen product;
and/or, in the step S500, extracting low-pressure liquid nitrogen generated by liquefaction in the auxiliary nitrogen tower condenser as a liquid nitrogen product.
Preferably, in the step S400, the oxygen-enriched liquid air 2 is subcooled by a main heat exchanger and then enters the auxiliary nitrogen tower condenser as a cold source part for evaporation, and the oxygen-enriched air 2 generated by evaporation is reheated by the main heat exchanger and then enters an expander for expansion refrigeration.
Preferably, in the step S500, the low-pressure liquid nitrogen enters the upper portion of the main nitrogen column after being pressurized by a pump, and is used as a main nitrogen column reflux liquid.
The invention has the beneficial technical effects that:
the liquid-air supercooling reflux expansion double-tower yield-increasing nitrogen-producing system and method provided by the invention utilize liquid-air supercooling at the bottom of the main nitrogen tower to throttle liquid and air to enter the auxiliary nitrogen tower for rectification, so that the nitrogen yield can be improved.
Liquid air throttling of a condenser of the main nitrogen tower is utilized to enter the auxiliary nitrogen tower to participate in rectification, so that the nitrogen yield can be improved; the safe discharge capacity of the condenser of the main nitrogen tower is sufficient, and the operation safety is ensured.
After liquid air at the bottom of the auxiliary nitrogen tower is subcooled, the liquid air is used as the only cold source of the auxiliary condenser, so that the control is convenient, and the operation is simple.
After reheating, the nitrogen product is pressurized by the pressurizing end of the expansion machine, the nitrogen pressure is increased, certain energy-saving effect is achieved, and the method is particularly suitable for the production process with high nitrogen pressure.
The invention can realize the switching operation of single tower and double towers, and the operation elasticity of the device is large.
Drawings
FIG. 1 is a schematic view of a process piping connection embodying the present invention;
in the figure: 100 air filters, 200 raw material air compressors, 300 refrigeration water pumps, 400 air cooling towers, 500 water cooling towers, 600 water chilling units, 700 adsorbers, 800 electric heaters, 1000 main heat exchangers, 1100 main nitrogen towers, 1110 main nitrogen tower condensers, 1200 auxiliary nitrogen towers, 1210 auxiliary nitrogen tower condensers, 1300 subcoolers, 1400 process liquid nitrogen pumps and 1500 supercharging turboexpanders.
Detailed Description
In order to make the technical solutions of the present invention more clear and definite, the present invention is further described in detail below with reference to the examples and the accompanying drawings, but the embodiments of the present invention are not limited thereto.
As shown in fig. 1, the liquid-air supercooling reflux expansion double-tower production nitrogen extraction system provided by this embodiment adopts a process organization of full low-pressure molecular sieve adsorption pre-purification, reflux expander refrigeration, and double-filler nitrogen tower landing arrangement, and includes an air filtration and compression system, a pre-cooling purification system, a main heat exchanger, a subcooler, a main nitrogen tower condenser, an auxiliary nitrogen tower condenser, and a process liquid nitrogen pump;
the condenser of the main nitrogen tower and the condenser of the auxiliary nitrogen tower are respectively and compositely installed with the tower device. An oxygen-enriched liquid-air pipeline at the bottom of the main nitrogen tower is sequentially connected with the main heat exchanger, a condenser of the main nitrogen tower and the auxiliary nitrogen tower, a liquid-air pipeline of the condenser of the main nitrogen tower is connected with the auxiliary nitrogen tower, and a liquid-air pipeline at the bottom of the auxiliary nitrogen tower is sequentially connected with the main heat exchanger and the condenser of the auxiliary nitrogen tower;
a nitrogen pipeline of the main nitrogen tower is sequentially connected with the main heat exchanger and the expander, and the oxygen-enriched air evaporated by the main condenser is connected with the auxiliary nitrogen tower;
the oxygen-enriched air of the condenser of the auxiliary nitrogen tower is sequentially connected with the main heat exchanger, the expander, the main heat exchanger and the purification system, and the reflux liquid nitrogen is respectively connected with the subcooler, the process liquid nitrogen pump and the main nitrogen tower.
In the embodiment, the oxygen-enriched liquid air 1 is subcooled by a main heat exchanger and then is divided into two parts, and one part of the oxygen-enriched liquid air enters a condenser of the main nitrogen tower to be used as a cold source; the other part enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling.
In this embodiment, the nitrogen gas at the upper part of the main nitrogen column is reheated by the main heat exchanger, and then further pressurized by the expander and sent to the user.
In this embodiment, the double rectification column connection flow path is blocked by valve control, and the single rectification column and the double rectification column are switched to operate.
A liquid-air supercooling reflux expansion double-tower extraction and nitrogen production method comprises the following steps:
s100: the purified air after being filtered, compressed, precooled and purified is cooled by a main heat exchanger and enters the bottom of a main nitrogen tower for rectification;
s200: obtaining oxygen-enriched liquid air 1 at the bottom of the main nitrogen tower, wherein the oxygen-enriched liquid air 1 is subcooled by a main heat exchanger and then is divided into two parts, and one part enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling; one part of the oxygen-enriched air enters a condenser of the main nitrogen tower to be used as a cold source, the other part of the evaporated oxygen-enriched air 1 enters the bottom of the auxiliary nitrogen tower to participate in rectification, and the concentrated oxygen-enriched liquid air 1 enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling;
s300: obtaining pressure nitrogen at the top of the main nitrogen tower, wherein the pressure nitrogen is divided into two parts, one part of the pressure nitrogen enters a condenser of the main nitrogen tower to be used as a heat source and flows back to the main nitrogen tower after being liquefied, and the other part of the pressure nitrogen is reheated by a main heat exchanger and then is pressurized by a pressurizing end of an expander for users;
s400: the bottom of the auxiliary nitrogen tower is provided with an oxygen-enriched liquid air 2, the oxygen-enriched liquid air 2 is subcooled by a main heat exchanger and then enters a condenser of the auxiliary nitrogen tower to be used as a cold source for partial evaporation, the oxygen-enriched air 2 generated by evaporation is reheated by the main heat exchanger and then enters an expander for expansion and refrigeration, the expanded oxygen-enriched air 2 is reheated by the main heat exchanger to the normal temperature and then is divided into two parts to be sent out of a cold box, one part of the air is cooled by a water cooling tower, the other part of the air is used as regeneration gas to be heated by an electric heater and then is used as regeneration gas to regenerate the molecular sieve of the adsorbent;
s500: obtaining low-pressure nitrogen gas at the top of the auxiliary nitrogen tower, wherein the low-pressure nitrogen gas completely enters the auxiliary nitrogen tower condenser to be used as a heat source, is liquefied and then is divided into three parts, and one part of the liquefied low-pressure nitrogen gas reflows to the auxiliary nitrogen tower; one part of the nitrogen enters the upper part of the main nitrogen tower after being pressurized by a liquid nitrogen pump and is used as reflux liquid; the other part is supplied to a user after being supercooled by the cooler.
In this embodiment, in the step S200, the oxygen-enriched liquid air 1 is subcooled by a main heat exchanger and then divided into two parts, and one part directly enters the condenser of the main nitrogen tower to serve as a cold source; the other part enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling.
In this embodiment, the pressure nitrogen is reheated by the main heat exchanger and then further pressurized by the pressurization end of the expander to increase the pressure of the nitrogen.
In this embodiment, the step S300 further includes extracting the pressure liquid nitrogen generated by liquefaction in the main condensation evaporator of the main nitrogen tower as a liquid nitrogen product;
and/or, in the step S500, extracting low-pressure liquid nitrogen generated by liquefaction in the auxiliary nitrogen tower condenser as a liquid nitrogen product.
In this embodiment, in the step S400, the oxygen-enriched liquid air 2 is subcooled by the main heat exchanger and then enters the auxiliary nitrogen tower condenser as a cold source to be partially evaporated, and the evaporated oxygen-enriched air 2 is reheated by the main heat exchanger and then enters the expander to be expanded and refrigerated.
In this embodiment, in the step S500, the low-pressure liquid nitrogen is pumped to the upper portion of the main nitrogen column to serve as a main nitrogen column reflux liquid.
For further understanding of the contents, features and effects of the present invention, the following embodiments are exemplified in conjunction with the accompanying drawings and the following detailed description:
the outlet of the air filter 100 is connected with the inlet of the raw material air compressor 200, the outlet of the raw material air compressor 200 is connected with the air inlet of the air cooling tower 400, the air outlet of the air cooling tower 400 is connected with the inlet of the adsorber 700, the outlet of the adsorber 700 is connected with the heat flow inlet of the main heat exchanger 1000, and the heat flow outlet of the main heat exchanger 1000 is connected with the bottom air inlet of the main nitrogen tower 1100.
A liquid air 1 at the bottom of the main nitrogen tower 1100 is connected with a hot stream inlet of a main heat exchanger 1000, and a hot stream outlet of the main heat exchanger 1000 is respectively connected with a condenser 1110 of the main nitrogen tower and an auxiliary nitrogen tower 1200; the outlet of the main nitrogen tower condenser 1110 is connected with the auxiliary nitrogen tower 1200; the nitrogen of the main nitrogen tower 1100 is connected with a cold stream inlet of the main heat exchanger 1000, a cold stream outlet of the main heat exchanger 1000 is connected with an inlet of a pressurization end of the pressurization turbo expander 1500, and the nitrogen at the outlet of the pressurization end of the pressurization turbo expander 1500 is sent to a user.
The liquid air 2 at the bottom of the auxiliary nitrogen tower 1200 is connected with a hot stream inlet of the main heat exchanger 1000, a hot stream outlet of the main heat exchanger 1000 is connected with an auxiliary nitrogen tower condenser 1210, an outlet of the oxygen-enriched air 2 of the auxiliary nitrogen tower condenser 1210 is connected with a cold stream inlet of the main heat exchanger 1000, a cold stream outlet of the main heat exchanger 1000 is connected with an expansion end inlet of the booster turboexpander 1500, an outlet of the expansion end of the booster turboexpander 1500 is connected with a cold stream inlet of the main heat exchanger 1000, a cold stream outlet of the main heat exchanger 1000 is connected with the adsorber regeneration heater 800, and the gas is discharged after the adsorber 700 is regenerated. The liquid nitrogen of the auxiliary nitrogen tower 1200 is respectively connected with an inlet of a process liquid nitrogen pump 1400 and a hot flow strand of a subcooler 1300, an outlet of the process liquid nitrogen pump 1400 is connected with a main nitrogen tower 1100, a hot flow outlet of the subcooler 1300 is divided into two parts, one part is connected with a cold flow inlet of the subcooler 1300, a cold flow strand outlet of the subcooler 1300 is connected with an outlet of an expansion end 1500 of a turbo-expander, and the other part of the liquid nitrogen is sent to a user.
The working principle of the technical scheme is as follows:
s1, enabling the raw material air to sequentially pass through an air filter 100, a raw material compressor 200, an air cooling tower 400 and an adsorber 700 to obtain purified air with the pressure of 800kPa.A, the temperature of 15.5 ℃ and the flow rate of 50500Nm3/h, and then enabling the purified air to enter a main heat exchanger 1000 to exchange heat with the returned product nitrogen and oxygen-enriched air; after being cooled to the saturation temperature of-168.8 ℃, the air enters the bottom of the main nitrogen tower 1100 to participate in rectification.
S2, supercooling liquid air 1 at the bottom of a main nitrogen tower 1100 through a main heat exchanger 1000 to obtain supercooled liquid air at the temperature of-171.5 ℃, 780kPa.A and 22800Nm3/h, wherein oxygen-enriched liquid air 1 at 5000Nm3/h is throttled and then enters an auxiliary nitrogen tower 1200 to participate in rectification, the rest part is used as a cold source of a main nitrogen tower condenser 1110, and oxygen-enriched air 1 obtained by the main nitrogen tower condenser 1110 and the oxygen-enriched liquid air are throttled and then all enter the auxiliary nitrogen tower 1200 to participate in rectification; 30500Nm3/h, -173 ℃ and 785kPa.A nitrogen gas is obtained at the upper part of the main nitrogen tower 1100, and is reheated to 13 ℃ by a main heat exchanger 1000, and then enters the pressurizing end of an expander 1500 to be pressurized to 815kPa.A for users.
S3, supercooling liquid air 2 at the bottom of an auxiliary nitrogen tower 1200 through a main heat exchanger 1000 to obtain supercooled liquid air at-177.2 ℃, 440kPa.A and 19300Nm3/h, wherein all the supercooled liquid air is used as a cold source of an auxiliary nitrogen tower condenser 1210, evaporated oxygen-enriched air 2 is reheated to-152 ℃, 165kPa.A and 19200Nm3/h through the main heat exchanger 1000, enters an expander 1500 to be expanded to 100kPa.A, the expanded oxygen-enriched air and nitrogen reheated by a subcooler 1300 are converged to enter the main heat exchanger 1000, and the reheated oxygen-enriched air and the nitrogen reheated by the subcooler 1300 are cooled to 13.1 ℃ to be supplied to an adsorber 700 and a water cooling tower 500 to cool circulating water. The low-pressure liquid nitrogen at the upper part of the auxiliary nitrogen tower 1200 is cooled to minus 180.5 ℃, 448kPa.A and 9600Nm3/h, wherein the liquid nitrogen at 220Nm3/h is cooled to minus 191 ℃ by a cooler 1300 for a user, and the rest of the liquid nitrogen enters the upper part of the main nitrogen tower 1100 as reflux after being pressurized by a liquid nitrogen pump 1400.
Although the present invention has been described with reference to the accompanying drawings, the present invention is not limited to the above embodiments, which are only illustrative and not restrictive, and those skilled in the art can make various modifications without departing from the spirit and scope of the present invention as defined in the appended claims.
Claims (10)
1. The utility model provides a liquid empty subcooling flows back expansion double tower and draws product nitrogen system which characterized in that: the process organization comprises an air filtering and compressing system, a precooling and purifying system, a main heat exchanger, a subcooler, a main nitrogen tower condenser, an auxiliary nitrogen tower condenser and a process liquid nitrogen pump, wherein the process organization comprises full low-pressure molecular sieve adsorption and prepurification, reflux expander refrigeration and double-filler nitrogen tower landing arrangement;
the main nitrogen tower and the auxiliary nitrogen tower condenser are respectively and compositely installed with the tower device. An oxygen-enriched liquid-air pipeline at the bottom of the main nitrogen tower is sequentially connected with the main heat exchanger, a condenser of the main nitrogen tower and the auxiliary nitrogen tower, a liquid-air pipeline of the condenser of the main nitrogen tower is connected with the auxiliary nitrogen tower, and a liquid-air pipeline at the bottom of the auxiliary nitrogen tower is sequentially connected with the main heat exchanger and the condenser of the auxiliary nitrogen tower;
a nitrogen pipeline of the main nitrogen tower is sequentially connected with the main heat exchanger and the expander, and the oxygen-enriched air evaporated by the main condenser is connected with the auxiliary nitrogen tower;
the oxygen-enriched air of the condenser of the auxiliary nitrogen tower is sequentially connected with the main heat exchanger, the expander, the main heat exchanger and the purification system, and the reflux liquid nitrogen is respectively connected with the subcooler, the process liquid nitrogen pump and the main nitrogen tower.
2. The liquid air subcooling reflux expansion double-tower production-by-extraction nitrogen-making system as described in claim 1, wherein: the oxygen-enriched liquid air 1 is subcooled by a main heat exchanger and then divided into two parts, and one part of the oxygen-enriched liquid air enters a condenser of the main nitrogen tower to be used as a cold source; the other part enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling.
3. The liquid air subcooling reflux expansion double-tower production-by-extraction nitrogen-making system as described in claim 2, wherein: the pressure nitrogen at the upper part of the main nitrogen tower is reheated by the main heat exchanger and is further pressurized by the expander and then is sent to a user.
4. The liquid air subcooling reflux expansion double-tower production-by-extraction nitrogen-making system as described in claim 3, wherein: the double rectifying towers are controlled by a valve to separate the connecting flow path, and the single rectifying tower and the double rectifying towers are switched to operate.
5. The liquid air subcooling reflux expansion double-tower nitrogen-production extraction method is characterized in that: the method comprises the following steps:
s100: the purified air after being filtered, compressed, precooled and purified is cooled by a main heat exchanger and enters the bottom of a main nitrogen tower for rectification;
s200: obtaining oxygen-enriched liquid air 1 at the bottom of the main nitrogen tower, wherein the oxygen-enriched liquid air 1 is subcooled by a main heat exchanger and then is divided into two parts, and one part enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling; one part of the oxygen-enriched air enters a condenser of the main nitrogen tower to be used as a cold source, the other part of the evaporated oxygen-enriched air 1 enters the bottom of the auxiliary nitrogen tower to participate in rectification, and the concentrated oxygen-enriched liquid air 1 enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling;
s300: obtaining pressure nitrogen at the top of the main nitrogen tower, wherein the pressure nitrogen is divided into two parts, one part of the pressure nitrogen enters a condenser of the main nitrogen tower to be used as a heat source and flows back to the main nitrogen tower after being liquefied, and the other part of the pressure nitrogen is reheated by a main heat exchanger and then is pressurized by a pressurizing end of an expander for a user;
s400: the bottom of the auxiliary nitrogen tower is provided with an oxygen-enriched liquid air 2, the oxygen-enriched liquid air 2 is subcooled by a main heat exchanger and then enters a condenser of the auxiliary nitrogen tower to be used as a cold source for partial evaporation, the oxygen-enriched air 2 generated by evaporation is reheated by the main heat exchanger and then enters an expander for expansion and refrigeration, the expanded oxygen-enriched air 2 is reheated by the main heat exchanger to the normal temperature and then is divided into two parts to be sent out of a cold box, one part of the air is cooled by a water cooling tower, the other part of the air is used as regeneration gas to be heated by an electric heater and then is used as regeneration gas to regenerate the molecular sieve of the adsorbent;
s500: obtaining low-pressure nitrogen gas at the top of the auxiliary nitrogen tower, wherein the low-pressure nitrogen gas completely enters the auxiliary nitrogen tower condenser to be used as a heat source, the low-pressure nitrogen gas is liquefied and then divided into three parts, and one part of the low-pressure nitrogen gas refluxes to the auxiliary nitrogen tower; one part of the nitrogen enters the upper part of the main nitrogen tower after being pressurized by a liquid nitrogen pump and is used as reflux liquid; the other part is supplied to users after being supercooled by the cooler.
6. The liquid air subcooling reflux expansion double-tower nitrogen-extracting production method as claimed in claim 5, characterized in that: in the step S200, the oxygen-enriched liquid air 1 is subcooled by a main heat exchanger and then divided into two parts, and one part directly enters a condenser of the main nitrogen tower to be used as a cold source; the other part enters the lower part of the auxiliary nitrogen tower to participate in rectification after throttling.
7. The liquid air subcooling reflux expansion double-tower nitrogen-production extraction method is characterized in that: and after reheating through the main heat exchanger, the pressure nitrogen is further pressurized through a pressurizing end of the expansion machine so as to improve the pressure of the nitrogen.
8. The liquid air subcooling reflux expansion double-tower nitrogen-producing extraction method is characterized in that: in the step S300, the method further includes extracting pressure liquid nitrogen generated by liquefaction in the main condensation evaporator of the main nitrogen tower as a liquid nitrogen product;
and/or, in the step S500, extracting low-pressure liquid nitrogen generated by liquefaction in the auxiliary nitrogen tower condenser as a liquid nitrogen product.
9. The liquid air subcooling reflux expansion double-column production nitrogen-making method according to claim 8, characterized in that: in the step S400, the oxygen-enriched liquid air 2 is subcooled by the main heat exchanger and then enters the auxiliary nitrogen tower condenser to be used as a cold source for partial evaporation, and the oxygen-enriched air 2 generated by evaporation is reheated by the main heat exchanger and then enters the expander for expansion refrigeration.
10. The liquid air subcooling reflux expansion double-column production nitrogen-making method according to claim 9, characterized in that: in the step S500, the low-pressure liquid nitrogen is pumped into the upper portion of the main nitrogen tower to be used as a main nitrogen tower reflux liquid.
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