CN115060041B - System and method for producing nitrogen by liquid-air supercooling, backflow and expansion double towers - Google Patents
System and method for producing nitrogen by liquid-air supercooling, backflow and expansion double towers Download PDFInfo
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- CN115060041B CN115060041B CN202210751096.XA CN202210751096A CN115060041B CN 115060041 B CN115060041 B CN 115060041B CN 202210751096 A CN202210751096 A CN 202210751096A CN 115060041 B CN115060041 B CN 115060041B
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 552
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 276
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 21
- 238000004781 supercooling Methods 0.000 title claims abstract description 19
- 239000007788 liquid Substances 0.000 claims abstract description 111
- 238000000034 method Methods 0.000 claims abstract description 32
- 238000010992 reflux Methods 0.000 claims abstract description 23
- 238000001914 filtration Methods 0.000 claims abstract description 7
- 230000008520 organization Effects 0.000 claims abstract description 3
- 238000000605 extraction Methods 0.000 claims abstract 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 54
- 239000001301 oxygen Substances 0.000 claims description 54
- 229910052760 oxygen Inorganic materials 0.000 claims description 54
- 238000001816 cooling Methods 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 238000000746 purification Methods 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 7
- 238000007906 compression Methods 0.000 claims description 6
- 230000006835 compression Effects 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 6
- 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
- 239000000945 filler Substances 0.000 claims description 3
- 238000005057 refrigeration Methods 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 239000013526 supercooled liquid Substances 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 description 5
- 238000003303 reheating Methods 0.000 description 4
- 239000006096 absorbing agent Substances 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010586 diagram Methods 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
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 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
Classifications
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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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- 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
- F25J3/04424—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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- 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
- F25J3/04151—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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- 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
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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.
- F25J3/04381—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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- 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
- 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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- 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
- F25J2205/34—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
Abstract
The invention provides a liquid-air supercooling, backflow and expansion double-tower nitrogen production system and method, wherein an air filtering and compressing system, an air precooling and purifying system, a rectifying system, a heat exchange system and an expansion system, wherein the rectifying 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 comprises an expander, wherein the expander is provided with a pressurizing end and an expansion end; the equipment parts are connected through pipelines. The method adopts the organization forms of double-tower rectification, floor arrangement and reflux expansion, liquid nitrogen pump is utilized to boost liquid nitrogen of the auxiliary nitrogen tower to provide partial reflux liquid for the main nitrogen tower, and simultaneously, the liquid air of the supercooled liquid at the bottom of the main nitrogen tower and the liquid air of the condenser of the main nitrogen tower are sent to the auxiliary nitrogen tower to participate in rectification, and a cold source is provided for the condenser of the auxiliary nitrogen tower after the liquid air at the bottom of the auxiliary nitrogen tower is supercooled. The method can effectively improve the yield of nitrogen and liquid nitrogen, has obvious 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-improving and nitrogen-producing system, in particular to a liquid-air supercooling and backflow expansion double-tower production-improving and nitrogen-producing system and a method thereof, and also relates to a liquid-air supercooling and backflow expansion double-tower production-improving and nitrogen-producing method, belonging to the technical field of air low-temperature separation and purification.
Background
With the rapid development of emerging industries such as semiconductors, electronic information, biological medicines, new materials and the like, particularly the development of power and energy storage battery enterprises, the market demand and scale for high-purity nitrogen are increasing, and at present, nitrogen is produced industrially in large scale, particularly for medium-and large-scale high-purity nitrogen production devices, the low-temperature rectification method is mostly adopted for nitrogen production.
The existing double-tower rectification nitrogen production method and device can be improved, for example, a double-tower stacking arrangement is provided by the patent application number of CN107345737A, 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 forward flow expansion energy is low, the potential of nitrogen product production exists by the patent application number of CN212006434U, and the liquid-air supercooling reflux expansion double-tower nitrogen production 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 nitrogen production system and method.
The aim of the invention can be achieved by adopting the following technical scheme:
a liquid-air supercooling reflux expansion double-tower nitrogen production 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 filtering 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 arranged with the tower. The oxygen-enriched liquid air pipeline at the bottom of the main nitrogen tower is sequentially connected with the main heat exchanger, the main nitrogen tower condenser and the auxiliary nitrogen tower, the liquid air pipeline of the main nitrogen tower condenser is connected with the auxiliary nitrogen tower, and the liquid air at the bottom of the auxiliary nitrogen tower is sequentially connected with the main heat exchanger and the auxiliary nitrogen tower condenser;
the 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 is divided into two parts after being supercooled by the main heat exchanger, and one part enters the main nitrogen tower condenser to be used as a cold source; the other part enters the lower part of the auxiliary nitrogen tower to participate in rectification after being throttled.
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 sent to a user.
Preferably, the valve control is used for blocking the connecting flow path of the double rectifying towers, and the single rectifying tower and the double rectifying towers are switched to operate.
A liquid-air supercooling reflux expansion double-tower nitrogen production method comprises the following steps:
s100: the purified air after filtration, compression and precooling purification is cooled by a main heat exchanger and enters the bottom of the main nitrogen tower for rectification;
s200: an oxygen-enriched liquid air is obtained at the bottom of the main nitrogen tower, the oxygen-enriched liquid air is divided into two parts after being supercooled by the main heat exchanger, and one part enters the lower part of the auxiliary nitrogen tower to participate in rectification after being throttled; part of the concentrated oxygen-enriched liquid enters the condenser of the main nitrogen tower to serve as a cold source, and part of the concentrated oxygen-enriched liquid enters the bottom of the auxiliary nitrogen tower to participate in rectification after the concentrated oxygen-enriched liquid enters the lower part of the auxiliary nitrogen tower to participate in rectification after being throttled;
s300: obtaining pressure nitrogen at the top of the main nitrogen tower, wherein the pressure nitrogen is divided into two parts, one part enters a main nitrogen tower condenser to serve as a heat source, the liquefied part flows back to the main nitrogen tower, and the other part is pressurized by a pressurizing end of an expander after being reheated by a main heat exchanger to be supplied to a user;
s400: the bottom of the auxiliary nitrogen tower is provided with an oxygen-enriched liquid air II, the oxygen-enriched liquid air II is supercooled by a main heat exchanger and enters the auxiliary nitrogen tower condenser to be used as a cold source for partial evaporation, the evaporated oxygen-enriched liquid air II is reheated by the main heat exchanger and then is expanded and cooled by an expander, the expanded oxygen-enriched liquid air II is reheated by the main heat exchanger to normal temperature and then is divided into two parts to be sent out of a cold box, one part of the water cooling tower is used for cooling circulating water, the other part of the water cooling tower is used as regenerated gas to be heated by an electric heater and then is used as regenerated gas to regenerate an adsorber molecular sieve;
s500: the top of the auxiliary nitrogen tower is provided with low-pressure nitrogen, the low-pressure nitrogen enters the condenser of the auxiliary nitrogen tower as a heat source, and is divided into three parts after being liquefied, and one part of the low-pressure nitrogen reflows to the auxiliary nitrogen tower; part of the liquid 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 supercooled by the cooler and then supplied to users.
Preferably, in step S200, the oxygen-enriched liquid is divided into two parts after being supercooled by the main heat exchanger, and one part directly enters the main nitrogen tower condenser 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.
Preferably, after the pressure nitrogen is reheated 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, in the step S300, the method further includes extracting pressurized liquid nitrogen generated by liquefaction in the main condensing evaporator of the main nitrogen tower as a liquid nitrogen product;
and/or, in the step S500, the method further includes extracting low-pressure liquid nitrogen generated by liquefaction in the auxiliary nitrogen tower condenser as a liquid nitrogen product.
Preferably, in step S400, the second oxygen-enriched liquid air 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 vaporized second oxygen-enriched liquid air is reheated by the main heat exchanger and then is expanded and cooled by the expander.
Preferably, in step S500, the low-pressure liquid nitrogen is pressurized by a pump and then enters the upper part of the main nitrogen tower to be used as reflux liquid of the main nitrogen tower.
The beneficial technical effects of the invention are as follows:
according to the liquid-air supercooling and backflow expansion double-tower nitrogen production system and method provided by the invention, liquid air at the bottom of the main nitrogen tower is supercooled and then throttled to enter the auxiliary nitrogen tower to participate in rectification, so that the nitrogen yield can be improved.
The liquid air throttling of the main nitrogen tower condenser is utilized to enter the auxiliary nitrogen tower to participate in rectification, so that the nitrogen yield can be improved; the main nitrogen tower condenser has sufficient safety discharge and ensures the operation safety.
The liquid air at the bottom of the auxiliary nitrogen tower is used as the only cold source of the auxiliary condenser after being supercooled, thereby being convenient to control and simple to operate.
After reheating, the nitrogen product is pressurized through the pressurizing end of the expander, so that the nitrogen pressure is improved, a certain energy-saving effect is achieved, and the method is particularly suitable for production processes with high nitrogen pressure.
The invention can realize the switching operation of single tower and double tower, and the operation flexibility of the device is large.
Drawings
FIG. 1 is a schematic diagram of a process piping connection embodying the present invention;
in the figure: 100 air filters, 200 raw material air compressors, 300 chilled 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 booster turbo expanders.
Detailed Description
In order to make the technical solution of the present invention more clear and obvious to those skilled in the art, the present invention will be described in further detail with reference to examples and 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 nitrogen production system provided by the embodiment adopts a process structure of full low-pressure molecular sieve adsorption pre-purification, reflux expander refrigeration and double-filler nitrogen tower landing arrangement, and comprises an air filtering compression system, a pre-cooling purification system, a main heat exchanger, a supercooler, 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 arranged with the tower. The oxygen-enriched liquid air pipeline at the bottom of the main nitrogen tower is sequentially connected with the main heat exchanger, the main nitrogen tower condenser and the auxiliary nitrogen tower, the liquid air pipeline of the main nitrogen tower condenser is connected with the auxiliary nitrogen tower, and the liquid air at the bottom of the auxiliary nitrogen tower is sequentially connected with the main heat exchanger and the auxiliary nitrogen tower condenser;
the 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 this embodiment, the oxygen-enriched liquid is divided into two parts after being supercooled by the main heat exchanger, and one part enters the main nitrogen tower condenser as a cold source; the other part enters the lower part of the auxiliary nitrogen tower to participate in rectification after being throttled.
In the embodiment, 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 sent to a user.
In the embodiment, the valve control is used for blocking the connection flow path of the double rectifying towers, and the single rectifying tower and the double rectifying towers are switched to operate.
A liquid-air supercooling reflux expansion double-tower nitrogen production method comprises the following steps:
s100: the purified air after filtration, compression and precooling purification is cooled by a main heat exchanger and enters the bottom of the main nitrogen tower for rectification;
s200: an oxygen-enriched liquid air is obtained at the bottom of the main nitrogen tower, the oxygen-enriched liquid air is divided into two parts after being supercooled by the main heat exchanger, and one part enters the lower part of the auxiliary nitrogen tower to participate in rectification after being throttled; part of the concentrated oxygen-enriched liquid enters the condenser of the main nitrogen tower to serve as a cold source, and part of the concentrated oxygen-enriched liquid enters the bottom of the auxiliary nitrogen tower to participate in rectification after the concentrated oxygen-enriched liquid enters the lower part of the auxiliary nitrogen tower to participate in rectification after being throttled;
s300: obtaining pressure nitrogen at the top of the main nitrogen tower, wherein the pressure nitrogen is divided into two parts, one part enters a main nitrogen tower condenser to serve as a heat source, the liquefied part flows back to the main nitrogen tower, and the other part is pressurized by a pressurizing end of an expander after being reheated by a main heat exchanger to be supplied to a user;
s400: the bottom of the auxiliary nitrogen tower is provided with an oxygen-enriched liquid air II, the oxygen-enriched liquid air II is supercooled by a main heat exchanger and enters the auxiliary nitrogen tower condenser to be used as a cold source for partial evaporation, the evaporated oxygen-enriched liquid air II is reheated by the main heat exchanger and then is expanded and cooled by an expander, the expanded oxygen-enriched liquid air II is reheated by the main heat exchanger to normal temperature and then is divided into two parts to be sent out of a cold box, one part of the water cooling tower is used for cooling circulating water, the other part of the water cooling tower is used as regenerated gas to be heated by an electric heater and then is used as regenerated gas to regenerate an adsorber molecular sieve;
s500: the top of the auxiliary nitrogen tower is provided with low-pressure nitrogen, the low-pressure nitrogen enters the condenser of the auxiliary nitrogen tower as a heat source, and is divided into three parts after being liquefied, and one part of the low-pressure nitrogen reflows to the auxiliary nitrogen tower; part of the liquid 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 supercooled by the cooler and then supplied to users.
In this embodiment, in step S200, the oxygen-enriched liquid is divided into two parts after being supercooled by the main heat exchanger, and one part directly enters the main nitrogen tower condenser 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, after the pressure nitrogen is reheated by the main heat exchanger, the pressure nitrogen is further increased by the pressure increasing end of the expander, so as to increase the pressure of the nitrogen.
In this embodiment, in step S300, the method further includes extracting pressurized 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, the method further includes extracting low-pressure liquid nitrogen generated by liquefaction in the auxiliary nitrogen tower condenser as a liquid nitrogen product.
In this embodiment, in step S400, the oxygen-enriched liquid air 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 evaporated oxygen-enriched liquid air is reheated by the main heat exchanger and then is expanded and cooled by the expander.
In this embodiment, in step S500, the low-pressure liquid nitrogen is pressurized by a pump and then enters the upper portion of the main nitrogen tower to be used as the reflux liquid of the main nitrogen tower.
For a further understanding of the present invention, its objects, features and advantages, reference should be made to the following examples, which are illustrated in the accompanying drawings in which:
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 absorber 700, the outlet of the absorber 700 is connected with the hot stream inlet of the main heat exchanger 1000, and the hot stream outlet of the main heat exchanger 1000 is connected with the bottom air inlet of the main nitrogen tower 1100.
The liquid space 1 at the bottom of the main nitrogen tower 1100 is connected with a hot flow inlet of the main heat exchanger 1000, and a hot flow outlet of the main heat exchanger 1000 is respectively connected with a main nitrogen tower condenser 1110 and an auxiliary nitrogen tower 1200; the outlet of the main nitrogen tower condenser 1110 is connected with the auxiliary nitrogen tower 1200; the main nitrogen tower 1100 nitrogen is connected with the cold flow inlet of the main heat exchanger 1000, the cold flow outlet of the main heat exchanger 1000 is connected with the inlet of the pressurizing end of the pressurizing turbine expander 1500, and the outlet nitrogen of the pressurizing end of the pressurizing turbine expander 1500 is used for users.
The bottom liquid air 2 of the auxiliary nitrogen tower 1200 is connected with the hot flow inlet of the main heat exchanger 1000, the hot flow outlet of the main heat exchanger 1000 is connected with the auxiliary nitrogen tower condenser 1210, the outlet of the oxygen-enriched liquid air II of the auxiliary nitrogen tower condenser 1210 is connected with the cold flow inlet of the main heat exchanger 1000, the cold flow outlet of the main heat exchanger 1000 is connected with the expansion end inlet of the booster turbine expander 1500, the outlet of the expansion end of the booster turbine expander 1500 is connected with the cold flow inlet of the main heat exchanger 1000, the cold flow outlet of the main heat exchanger 1000 is connected with the adsorber regeneration heater 800, and the regenerated gas of the adsorber 700 is exhausted. The auxiliary nitrogen tower 1200 is respectively connected with an inlet of a process liquid nitrogen pump 1400 and a hot stream of a subcooler 1300, an outlet of the process liquid nitrogen pump 1400 is connected with the main nitrogen tower 1100, the hot stream outlet of the subcooler 1300 is divided into two parts, one part is connected with the cold stream inlet of the subcooler 1300, the cold stream outlet of the subcooler 1300 is connected with an expansion end outlet of a booster turbo expander 1500, and the other part of liquid nitrogen is used for users.
The working principle of the technical scheme is as follows:
s1, raw material air sequentially passes through an air filter 100, a raw material air 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 enters a main heat exchanger 1000 to exchange heat with the returned product nitrogen and oxygen-enriched air; after the air is 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 the liquid air 1 at the bottom of the main nitrogen tower 1100 through a main heat exchanger 1000 to obtain supercooled liquid air at-171.5 ℃ and 780kPa.A and 22800Nm3/h, wherein 5000 Nm3/h of oxygen-enriched liquid air 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 the oxygen-enriched liquid air obtained by the main nitrogen tower condenser 1110 are throttled and then all enter the auxiliary nitrogen tower 1200 to participate in rectification; 30500Nm3/h, -173 ℃, 785kPa. A nitrogen is obtained at the upper part of the main nitrogen tower 1100, and after reheating to 13 ℃ by the main heat exchanger 1000, the nitrogen is sent to the pressurizing end of the expander 1500 to be pressurized to 815kPa. A for users.
S3, supercooling the liquid air 2 at the bottom of the auxiliary nitrogen tower 1200 through the main heat exchanger 1000 to obtain supercooled liquid air at-177.2 ℃ and 440kPa A and 19300Nm3/h, taking the supercooled liquid air as a cold source of the auxiliary nitrogen tower condenser 1210, reheating the vaporized oxygen-enriched liquid air to-152 ℃ and 165kPa A and 19200Nm3/h through the main heat exchanger 1000, entering the expander 1500 to expand to 100kPa A, merging the expanded oxygen-enriched air with nitrogen reheated by the supercooler 1300, entering the main heat exchanger 1000, reheating to 13.1 ℃ and then cooling circulating water by the adsorber 700 and the water cooling tower 500. The low pressure liquid nitrogen at the upper part of the auxiliary nitrogen tower 1200 is-180.5 ℃, 447 kPa A and 9600Nm3/h, wherein 220Nm3/h liquid nitrogen is supercooled to-191 ℃ by the supercooler 1300 for users, and the rest liquid nitrogen enters the upper part of the main nitrogen tower 1100 as reflux liquid after being pressurized by the process liquid nitrogen pump 1400.
Although the present invention has been described in connection with the above embodiments, the present invention is not limited to the above embodiments, which are merely illustrative and not restrictive, and many forms may be made by those of ordinary skill in the art without departing from the spirit of the invention and the scope of the appended claims, which are within the scope of the invention.
Claims (6)
1. A liquid-air supercooling reflux expansion double-tower nitrogen production system is characterized in that: the method adopts a process organization of full low-pressure molecular sieve adsorption pre-purification, reflux expander refrigeration and double-filler nitrogen tower floor arrangement, and comprises an air filtering 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 arranged with the tower; the oxygen-enriched liquid air pipeline at the bottom of the main nitrogen tower is sequentially connected with the main heat exchanger, the main nitrogen tower condenser and the auxiliary nitrogen tower, the liquid air pipeline of the main nitrogen tower condenser is connected with the auxiliary nitrogen tower, and the liquid air at the bottom of the auxiliary nitrogen tower is sequentially connected with the main heat exchanger and the auxiliary nitrogen tower condenser;
the 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;
the oxygen-enriched liquid is divided into two parts after being supercooled by a main heat exchanger, and one part enters a main nitrogen tower condenser to be used as a cold source; the other part enters the lower part of the auxiliary nitrogen tower to participate in rectification after being throttled;
the nitrogen at the upper pressure of the main nitrogen tower is reheated by the main heat exchanger, and is further pressurized by the expander and then sent to a user.
2. The liquid-air subcooling reflux expansion double-tower nitrogen production system as claimed in claim 1, wherein: the valve controls to cut off the connecting flow path of the double rectifying towers, and the single rectifying tower and the double rectifying towers are switched to operate.
3. The method for producing nitrogen by liquid-air supercooling, backflow and expansion double-tower extraction according to claim 2, which is characterized in that: the method comprises the following steps:
s100: the purified air after filtration, compression and precooling purification is cooled by a main heat exchanger and enters the bottom of the main nitrogen tower for rectification;
s200: an oxygen-enriched liquid air is obtained at the bottom of the main nitrogen tower, the oxygen-enriched liquid air is divided into two parts after being supercooled by the main heat exchanger, and one part enters the lower part of the auxiliary nitrogen tower to participate in rectification after being throttled; part of the concentrated oxygen-enriched liquid enters the condenser of the main nitrogen tower to serve as a cold source, and part of the concentrated oxygen-enriched liquid enters the bottom of the auxiliary nitrogen tower to participate in rectification after the concentrated oxygen-enriched liquid enters the lower part of the auxiliary nitrogen tower to participate in rectification after being throttled;
s300: obtaining pressure nitrogen at the top of the main nitrogen tower, wherein the pressure nitrogen is divided into two parts, one part enters a main nitrogen tower condenser to serve as a heat source, the liquefied part flows back to the main nitrogen tower, and the other part is pressurized by a pressurizing end of an expander after being reheated by a main heat exchanger to be supplied to a user;
s400: the bottom of the auxiliary nitrogen tower is provided with an oxygen-enriched liquid air II, the oxygen-enriched liquid air II is supercooled by a main heat exchanger and enters the auxiliary nitrogen tower condenser to be used as a cold source for partial evaporation, the evaporated oxygen-enriched liquid air II is reheated by the main heat exchanger and then is expanded and cooled by an expander, the expanded oxygen-enriched liquid air II is reheated by the main heat exchanger to normal temperature and then is divided into two parts to be sent out of a cold box, one part of the water cooling tower is used for cooling circulating water, the other part of the water cooling tower is used as regenerated gas to be heated by an electric heater and then is used as regenerated gas to regenerate an adsorber molecular sieve;
s500: the top of the auxiliary nitrogen tower is provided with low-pressure nitrogen, the low-pressure nitrogen enters the condenser of the auxiliary nitrogen tower as a heat source, and is divided into three parts after being liquefied, and one part of the low-pressure nitrogen reflows to the auxiliary nitrogen tower; part of the liquid nitrogen enters the upper part of the main nitrogen tower after being pressurized by a liquid nitrogen pump and is used as reflux liquid; another part is supercooled by a cooler for users;
in the step S200, the oxygen-enriched liquid is divided into two parts after being supercooled by the main heat exchanger, and one part directly enters the main nitrogen tower condenser 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;
after the pressure nitrogen is reheated by the main heat exchanger, the pressure nitrogen is further pressurized by the pressurizing end of the expander so as to improve the pressure of the nitrogen.
4. The method for producing nitrogen by liquid-air supercooling, backflow and expansion double-tower extraction according to claim 3, which is characterized in that: in the step S300, the method further includes extracting pressurized liquid nitrogen generated by liquefaction in the main condensing evaporator of the main nitrogen tower as a liquid nitrogen product;
and/or, in the step S500, the method further includes extracting low-pressure liquid nitrogen generated by liquefaction in the auxiliary nitrogen tower condenser as a liquid nitrogen product.
5. The method for producing nitrogen by liquid-air supercooling, backflow and expansion double-tower extraction, which is characterized in that: in the step S400, the second oxygen-enriched liquid air is supercooled 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 evaporated second oxygen-enriched liquid air is reheated by the main heat exchanger and then is expanded and cooled by the expander.
6. The method for producing nitrogen by liquid-air supercooling, backflow and expansion double-tower extraction, which is characterized by comprising the following steps of: in the step S500, the low-pressure liquid nitrogen is pressurized by a pump and then enters the upper part of the main nitrogen tower to be used as reflux liquid of the main nitrogen tower.
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