CN101915495B - Full liquid-air separation unit using liquefied natural gas cold energy and method thereof - Google Patents
Full liquid-air separation unit using liquefied natural gas cold energy and method thereof Download PDFInfo
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- CN101915495B CN101915495B CN2010102623634A CN201010262363A CN101915495B CN 101915495 B CN101915495 B CN 101915495B CN 2010102623634 A CN2010102623634 A CN 2010102623634A CN 201010262363 A CN201010262363 A CN 201010262363A CN 101915495 B CN101915495 B CN 101915495B
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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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams 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
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- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
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- F25J3/0426—The cryogenic component does not participate in the fractionation
- F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
- F25J3/04272—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons and comprising means for reducing the risk of pollution of hydrocarbons into the air fractionation
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- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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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
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- 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
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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
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- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
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- 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
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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04703—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser being arranged in more than one vessel
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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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
- F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
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- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
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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
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
Abstract
The invention relates to a full liquid-air separation unit using liquefied natural gas cold energy and a method thereof. The full liquid-air separation unit comprises a self-cleaning air filter AF, an air compressor TC1, an air cooler E5, a purification system, a main heat exchanger E2, a liquefier E7, a lower tower C1, an upper tower C2 communicated with the lower tower C1 through a pipe and a subcooler E3, a first condensation evaporator K1, a nitrogen circulating system and an argon fractionation system, wherein, the lower tower C1 is equipped with a liquid nitrogen fraction extraction opening and a barren liquor-air extraction opening; the subcooler E3 is equipped with a liquid nitrogen fraction channel and a barren liquor-air channel; the upper tower C2 is equipped with a liquid nitrogen fraction inlet and a barren liquor-air inlet; the liquid nitrogen fraction channel is respectively communicated with the upper tower C2 and the lower tower C1 through the subcooler E3; and the barren liquor-air channel is respectively communicated with the upper tower C2 and the lower tower C1 through the subcooler E3. The invention has high utilization ratio of refrigerating capacity, energy conservation, environmental protection, high operating efficiency and high safety factor.
Description
Technical field
The present invention relates to air-separating plant, be specifically related to a kind of full-liquid air separation device and method of utilizing cold energy of liquefied natural gas.
Background technology
Air separation equipment is exactly with air liquefaction, rectifying, finally is separated into the gas separation equipment of oxygen, nitrogen and other valuable gases, is called for short air separation plant.Air once was called as " permanent gas " to 19 end of the centurys, it is found that air also can liquefy under profound hypothermia, and because of oxygen, nitrogen boiling point difference, can isolate oxygen and nitrogen from liquefied air.The commercial oxygenerator of First was made in 1903, and it just is used for gas welding and the cutting of metal at first.At the end of the thirties, nitrogen fertilizer industry needs nitrogen, and oxygenerator develops into can produce oxygen and nitrogen simultaneously, renames as air separation equipment.
Natural gas is a kind of high-grade energy, has calorific value high, clean, the characteristics such as Air–pollution From Combustion is little, its Main Ingredients and Appearance is methane, for the ease of transporting its liquefaction condensing temperature generally at-150 ℃～-161 ℃), become liquefied natural gas LNG), be transported to behind the destination in order to utilize and to need its vaporization, can produce a large amount of colds during vaporization, 0.1Mpa under the cold energy that discharges during from-161 ℃ of re-heats to 27 ℃ of LNG be about 950KJ/kg, 8.0Mpa under the cold energy that discharges during from-161 ℃ of re-heats to 27 ℃ of NG be about 830KJ/kg, LNG contains huge high-quality cold energy, will be great waste if do not recycle.The mode of at present LNG cold energy use has cold energy generation, low-temperature grinding old tire, produces the full liquid space division device of liquid oxygen, liquid nitrogen, liquid argon.According to the low temperature cold principle utilized of low temperature as far as possible, full liquid space division device is LNG cold energy use the most rational the most effective a kind of mode of utilizing.
Liquid oxygen, liquid nitrogen, the liquid argon product of full liquid space division device production are widely used in the fields such as metallurgy, petrochemical industry, machinery, chemical fertilizer, glass, military project, food, medical treatment, but traditional conventional empty minute energy consumption is large, produces 1Nm
3Fluid product needs the energy consumption of 1.05-1.25kwh, utilizes the air separation unit of LNG cold energy to produce 1Nm
3The fluid product Energy Intensity Reduction is more than 50%.
Summary of the invention
For the deficiencies in the prior art, the invention provides that a kind of cryogenic energy utilization rate is high, energy-conserving and environment-protective, high efficiency, the full-liquid air separation device that utilizes cold energy of liquefied natural gas and method that safety coefficient is high.
Technical scheme of the present invention is achieved in that a kind of full-liquid air separation device that utilizes the liquified natural gas cold energy, comprise: self-cleaning air filter AF, the air compressor TC1 that is connected with self-cleaning air filter AF, the aerial cooler E5 that is connected with air compressor TC1, the purification system that is connected with aerial cooler E5, the main heat exchanger E2 that is connected with purification system by the first raw air pipeline, the the second raw air pipeline that is connected with the first raw air pipeline, the lower tower C1 that is connected with the second raw air pipeline, also pass through the upper tower C2 that is connected behind the subcooler E3 with lower tower C1 by pipeline, be positioned at the first condenser/evaporator K1 of tower C2 bottom, the nitrogen circulating system that is connected with lower tower C1, and the argon gas fractionating system that is connected with upper tower C2, be provided with liquid nitrogen fraction on the described lower tower C1, the lean solution sky is taken out mouth, be provided with the empty passage of liquid nitrogen fraction passage and lean solution on the subcooler E3, be provided with liquid nitrogen fraction on the upper tower C2, the empty import of lean solution, the liquid nitrogen fraction passage is connected with upper tower C2 and lower tower C1 respectively by subcooler E3, and the empty passage of lean solution is connected with upper tower C2 and lower tower C1 respectively by subcooler E3.
Described nitrogen circulating system comprises high pressure heat exchanger E1, the delivering liquid natural gas is used for reclaiming the liquid natural feed channel of liquified natural gas cold to high pressure heat exchanger E1, the low pressure recycle nitrogen compressor TC2 that is connected by the first pipeline with lower tower C1, the Medium pressure cycle nitrogen compressor TC3 that is connected with low pressure recycle nitrogen compressor TC2, the the first gas-liquid separator SV1 that is connected by the 5th pipeline with low pressure recycle nitrogen compressor TC2 and Medium pressure cycle nitrogen compressor TC3, the the second gas-liquid separator SV2 that is connected with the first gas-liquid separator SV1 by the 6th pipeline, the liquefier E7 that is connected with the first gas-liquid separator SV1 by second pipe, wherein the first gas-liquid separator SV1 is connected with low pressure recycle nitrogen compressor TC2 by the 7th pipeline, be provided with the 8th pipeline that is connected with Medium pressure cycle nitrogen compressor TC3 on the 5th pipeline, liquefier E7 is connected with low pressure recycle nitrogen compressor TC2 by the 3rd pipeline and the 4th pipeline respectively again.
Described purification system is connected with main heat exchanger E2 by the first raw air pipeline, and the first raw air pipeline is connected with liquefier E7 after passing main heat exchanger E2, and liquefier E7 is connected with lower tower C1 by the liquid air pipeline.
The pressure of the natural gas in the described liquid natural feed channel 26 is 0.2Mpa-10.0Mpa.
A kind of full liquia air separation method that utilizes cold energy of liquefied natural gas, its method is as follows:
1) after raw air filters dust impurity through self-cleaning air filter AF, enter air compressor TC1 and be compressed to 0.52Mpa, cooled to 2 ℃-10 ℃ by refrigerant glycol water or fluorine Lyons, then enter purification system and remove the impurity such as airborne moisture content, carbon dioxide, raw air after the purification goes main heat exchanger E2 heat exchange, be cooled to-167 ℃ to-170 ℃, a part of raw air enters lower tower C1 through the second raw air pipeline; Another part raw air enters lower tower C1 through liquefier E7 liquefaction for liquid air and through the liquid air pipeline, carries out caloic exchange, condensation evaporation at lower tower C1, obtains successively nitrogen, liquid nitrogen, liquid nitrogen fraction, lean solution sky, oxygen-enriched liquid air;
2) oxygen-enriched liquid air described 1) is crossed the further rectifying of tower C2 in the cold deutomerite diffluence through subcooler E3, described 1) nitrogen that lower tower C1 top obtains in removes condenser/evaporator K1, be condensed into liquid nitrogen, part liquid nitrogen is as the phegma of lower tower, another part liquid nitrogen is crossed through subcooler E3 and is gone the further rectifying of upper tower C2, described 1 after cold) in the liquid nitrogen fraction that obtains of lower tower C1, lean solution sky cross through subcooler E3 by liquid nitrogen fraction passage, the empty passage of lean solution respectively and go upper tower C2 to participate in further rectifying after cold;
When gas nitrogen is condensed into liquid nitrogen in condenser/evaporator K1,1) liquid oxygen among the upper tower C2 is evaporated the rising gas as upper tower C2, and phegma liquid nitrogen, oxygen-enriched liquid air conduct heat between filler, mass transfer, oxygen, nitrogen separate, upper tower C2 bottom obtains highly purified liquid oxygen output ice chest I, it is that 8%-12% argon fraction is sent into argon producing system that upper tower C2 middle part obtains volume ratio, produces smart argon and exports ice chest I, and the nitrogen at upper tower C2 top is cooling box I after subcooler E3, main heat exchanger E2 re-heat;
3) with 1), 2) in the nitrogen that obtains of lower tower C1 top the 3rd pipeline of extracting a part of nitrogen that a part vaporizes out in the first pipeline and output liquefier E7 remove main heat exchanger E2 after merging, with cooling box I after the first raw air pipeline heat exchange intensification, then remove ice chest II, extract out in high pressure heat exchanger E1, be cooled to-120 ℃ to-126 ℃ by liquified natural gas after, send into low pressure recycle nitrogen compressor TC2; Another part nitrogen of vaporizing among the liquefier E7 by the 4th pipeline after high pressure heat exchanger E1 is warmed up to-120 ℃ to-126 ℃, send into low pressure recycle nitrogen compressor TC2, the isolated nitrogen of the first gas-liquid separator SV1 is also extracted out after high pressure heat exchanger E1 is warmed up to-120 ℃-126 ℃, send into low pressure recycle nitrogen compressor TC2, after returning high pressure heat exchanger E1 after the low pressure recycle nitrogen compressor TC2 supercharging again to be cooled to-120 ℃ to-126 ℃, extract out and remove Medium pressure cycle nitrogen compressor TC3, return heat exchanger E1 after the supercharging, reclaim the cold of liquefied natural gas, liquefaction is liquid nitrogen, extract out after the liquid nitrogen part throttling that is liquefied is warmed up to-120 ℃ to-126 ℃ by heat exchanger E1 and remove Medium pressure cycle nitrogen compressor TC3, the residue liquid nitrogen advances the first gas-liquid separator SV1, a liquid nitrogen part of separating is removed liquefier E7 liquefied air through second pipe, self is evaporated to nitrogen, another part liquid nitrogen removes the second gas-liquid separator SV2, liquid after the separation is sent as product, and gas is through heat exchanger E1 re-heat cooling box II;
4) the ducted liquified natural gas of liquified natural gas described 3) in high pressure heat exchanger E1 by re-heat, from the liquid natural feed channel at high pressure heat exchanger E1 middle part, extract a part of natural gas out and remove heat exchanger E4 cooling glycol water or freon, remainder is extracted out with after the merging of the natural gas after the heat exchanger E4 re-heat from high pressure heat exchanger E1 is terminal, finally obtain the sky hot gas more than 2 ℃, the refrigerant that is cooled goes the compressed air of intercooler of air compressor E6 and aftercooler E5 cooling-air compressor TC1 to arrive to 2 ℃-10 ℃, improve the efficient of air compressor TC1, reduce air compressor TC1 energy consumption.
Described 3) lower tower C1 top is extracted a part of nitrogen out and remove main heat exchanger E2 after the first pipeline and the 3rd pipeline of exporting a part of nitrogen of vaporizing among the liquefier E7 is merged in, with cooling box I after the first raw air pipeline heat exchange intensification, then remove ice chest II, in high pressure heat exchanger E1, extracted out after-120 ℃-126 ℃ by the liquified natural gas tube-cooled, send into low pressure nitrogen press TC2; Another part nitrogen of vaporizing among the liquefier E7 by the 4th pipeline after high pressure heat exchanger E1 is warmed up to-120 ℃-126 ℃, send into low pressure nitrogen press TC2, the isolated nitrogen of the first gas-liquid separator SV1 is also extracted out after high pressure heat exchanger E1 is warmed up to-120 ℃-126 ℃ by the 7th pipeline, send into low pressure nitrogen press TC2, after low-temp low-pressure cyclic nitrogen press TC2 supercharging, return high pressure heat exchanger E1 cooling, extract out after again being cooled to-120 ℃-126 ℃ and remove Medium pressure cycle nitrogen compressor TC3, return heat exchanger E1 after the supercharging, reclaim the cold of liquified natural gas, liquefaction is liquid nitrogen, a liquid nitrogen part that is liquefied is extracted out through the 8th pipeline throttling is warmed up to-120 ℃-126 ℃ by heat exchanger E1 after and is removed Medium pressure cycle nitrogen compressor TC3, the residue liquid nitrogen advances the first gas-liquid separator SV1 by the 5th pipeline, a liquid nitrogen part of separating is removed liquefier E7 liquefied air through second pipe, self is evaporated to nitrogen, another part liquid nitrogen removes the second gas-liquid separator SV2 through the 6th pipeline, liquid is sent as product through the liquid nitrogen output channel, and gas passes through the 9th pipeline through heat exchanger E1 re-heat cooling box II.
The present invention has following good effect: the present invention takes out liquid nitrogen fraction, lean solution sky by lower tower, makes air separation unit not reduce recovery rate because of the liquefaction of part material air; In high pressure heat exchanger, liquefy the low temperature cold recovery of LNG by circulating nitrogen gas, glycol water (or freon) is with the high temperature cold recovery, the LNG cold energy utilizes stage by stage, but compares decrease power consumption and water consumption with traditional full liquid space division device; Liquid nitrogen passes to fractionating column system with air liquefaction with cold by liquefier, has stopped the leakage of methane to fractionating system, makes separator safe; LNG progressively heats up in high pressure heat exchanger and gasifies, the low temperature cold is transferred to nitrogen, but re-heat can not be used for its high temperature cold recovery by suitable refrigerant middle cooling and the final stage cooling of air compressor to normal temperature, improve the efficient of air compressor machine machine, energy-saving and cost-reducing.
Description of drawings
Fig. 1 is structural representation of the present invention.
The specific embodiment
As shown in Figure 1, a kind of full-liquid air separation device that utilizes the liquified natural gas cold energy, comprise: self-cleaning air filter AF, the air compressor TC1 that is connected with self-cleaning air filter AF, the aerial cooler E5 that is connected with air compressor TC1, the purification system that is connected with aerial cooler E5, the main heat exchanger E2 that is connected with purification system by the first raw air pipeline 1, the the second raw air pipeline 2 that is connected with the first raw air pipeline 1, the lower tower C1 that is connected with the second raw air pipeline 2, also pass through the upper tower C2 that is connected behind the subcooler E3 with lower tower C1 by pipeline, be positioned at the first condenser/evaporator K1 of tower C2 bottom, the nitrogen circulating system that is connected with lower tower C1, and the argon gas fractionating system that is connected with upper tower C2, be provided with liquid nitrogen fraction on the described lower tower C1, the lean solution sky is taken out mouth, be provided with the empty passage 7 of liquid nitrogen fraction passage 6 and lean solution on the subcooler E3, be provided with liquid nitrogen fraction on the upper tower C2, the empty import of lean solution, liquid nitrogen fraction passage 6 is connected with upper tower C2 and lower tower C1 respectively by pipeline, and the empty passage 7 of lean solution is connected with upper tower C2 and lower tower C1 respectively by pipeline.
Described nitrogen circulating system comprises high pressure heat exchanger E1, the delivering liquid natural gas is used for reclaiming the liquid natural feed channel 26 of liquified natural gas cold to high pressure heat exchanger E1, the low pressure recycle nitrogen compressor TC2 that is connected by the first pipeline 13 with lower tower C1, the Medium pressure cycle nitrogen compressor TC3 that is connected with low pressure recycle nitrogen compressor TC2, the the first gas-liquid separator SV1 that is connected by the 5th pipeline 17 with low pressure recycle nitrogen compressor TC2 and Medium pressure cycle nitrogen compressor TC3, the the second gas-liquid separator SV2 that is connected with the first gas-liquid separator SV1 by the 6th pipeline 20, the liquefier E7 that is connected with the first gas-liquid separator SV1 by second pipe 19, wherein the first gas-liquid separator SV1 is connected with low pressure recycle nitrogen compressor TC2 by the 7th pipeline 18, be provided with the 8th pipeline 16 that is connected with Medium pressure cycle nitrogen compressor TC3 on the 5th pipeline 17, liquefier E7 is connected with low pressure recycle nitrogen compressor TC2 by the 3rd pipeline 14 and the 4th pipeline 15 respectively again.
Described purification system is connected with main heat exchanger E2 by the first raw air pipeline 1, and the first raw air pipeline 1 is connected with liquefier E7 after passing main heat exchanger E2, and liquefier E7 is connected with lower tower C1 by liquid air pipeline 3.
The pressure of the natural gas in the described liquid natural feed channel 26 is 0.2Mpa-10.0Mpa.
A kind of full liquia air separation method that utilizes cold energy of liquefied natural gas, its method is as follows:
1) after raw air filters dust impurity through self-cleaning air filter AF, enter air compressor TC1 and be compressed to 0.52Mpa, cooled to 2 ℃-10 ℃ by refrigerant glycol water (or fluorine Lyons), then enter purification system and remove the impurity such as airborne moisture content, carbon dioxide, raw air after the purification goes main heat exchanger E2 heat exchange, be cooled to-167 ℃ to-170 ℃, a part of raw air enters lower tower C1 through the second raw air pipeline 2; Another part raw air enters lower tower C1 through liquefier E7 liquefaction for liquid air and through liquid air pipeline 3, carries out caloic exchange, condensation evaporation at lower tower C1, obtains successively nitrogen, liquid nitrogen, liquid nitrogen fraction, lean solution sky, oxygen-enriched liquid air;
2) oxygen-enriched liquid air described 1) is crossed the further rectifying of tower C2 in the cold deutomerite diffluence through subcooler E3, described 1) nitrogen that lower tower C1 top obtains in removes condenser/evaporator K1, be condensed into liquid nitrogen, part liquid nitrogen is as the phegma of lower tower, another part liquid nitrogen is crossed through subcooler E3 and is gone the further rectifying of upper tower C2, described 1 after cold) in the liquid nitrogen fraction that obtains of lower tower C1, lean solution sky cross through subcooler E3 by liquid nitrogen fraction passage 6, the empty passage 7 of lean solution respectively and go upper tower C2 to participate in further rectifying after cold;
When gas nitrogen is condensed into liquid nitrogen in condenser/evaporator K1,1) liquid oxygen among the upper tower C2 is evaporated the rising gas as upper tower C2, and phegma liquid nitrogen, oxygen-enriched liquid air conduct heat between filler, mass transfer, oxygen, nitrogen separate, upper tower C2 bottom obtains highly purified liquid oxygen output ice chest I, it is that 8%-12% argon fraction is sent into argon producing system that upper tower C2 middle part obtains volume ratio, produces smart argon and exports ice chest I, and the nitrogen at upper tower C2 top is cooling box I after subcooler E3, main heat exchanger E2 re-heat;
3) with 1), 2) in the nitrogen that obtains of lower tower C1 top the 3rd pipeline 14 of extracting a part of nitrogen that a part vaporizes out in the first pipeline 13 and output liquefier E7 remove main heat exchanger E2 after merging, with the first raw air pipeline 1) the rear cooling box I of heat exchange intensification, then remove ice chest II, extract out after in high pressure heat exchanger E1, being cooled to-120 ℃-126 ℃ by liquid natural feed channel 26, send into low pressure nitrogen press TC2; Another part nitrogen of vaporizing among the liquefier E7 by the 4th pipeline 15 after high pressure heat exchanger E1 is warmed up to-120 ℃-126 ℃, send into low pressure nitrogen press TC2, the isolated nitrogen of the first gas-liquid separator SV1 is also extracted out after high pressure heat exchanger E1 is warmed up to-120 ℃-126 ℃ by the 7th pipeline 18, send into low pressure nitrogen press TC2, after low-temp low-pressure cyclic nitrogen press TC2 supercharging, return high pressure heat exchanger E1 cooling, extract out after again being cooled to-120 ℃-126 ℃ and remove Medium pressure cycle nitrogen compressor TC3, return heat exchanger E1 after the supercharging, reclaim the cold of liquified natural gas, liquefaction is liquid nitrogen, a liquid nitrogen part that is liquefied is extracted out through 16 throttlings of the 8th pipeline are warmed up to-120 ℃-126 ℃ by heat exchanger E1 after and is removed Medium pressure cycle nitrogen compressor TC3, the residue liquid nitrogen advances the first gas-liquid separator SV1 by the 5th pipeline 17, a liquid nitrogen part of separating is removed liquefier E7 liquefied air through second pipe 19, self is evaporated to nitrogen, another part liquid nitrogen removes the second gas-liquid separator SV2 through the 6th pipeline 20, liquid is sent as product through liquid nitrogen output channel 21, gas by the 9th pipeline 22 through heat exchanger E1 re-heat cooling box II.
4) liquified natural gas in the liquid natural feed channel 26 described 3) in high pressure heat exchanger E1 by re-heat, from the liquid natural feed channel 26 at high pressure heat exchanger E1 middle part, extract a part of natural gas via natural gas lateral 23 out and remove heat exchanger E4 cooling glycol water (or freon), remainder is extracted out with after the merging of the natural gas via after the heat exchanger E4 re-heat from high pressure heat exchanger E1 is terminal, after namely merging with natural gas lateral 23, finally obtain the sky hot gas more than 2 ℃, the refrigerant that is cooled goes the compressed air of air press intercooler E6 and aftercooler E5 cooling-air compressor TC1 to arrive to 2 ℃-10 ℃ by refrigerant conveyance conduit 25, improve the efficient of air compressor TC1, reduce air compressor TC1 energy consumption.
The present invention utilizes circulating nitrogen gas to recycle the LNG cold by heat exchanger, again air liquefaction is passed to space division system with cold, by suitable refrigerant cold is passed to air compression system.Utilize the cold energy of LNG to produce liquid oxygen, liquid nitrogen, liquid argon, and decrease power consumption more than 50%, water consume more than 90%.Transmit cold by raw air, avoid methane toward the leakage of piece-rate system, safe.Extract liquid nitrogen fraction, lean solution sky by lower tower, tower reflux ratio in the increase makes air separation unit not reduce recovery rate because of the liquefaction of raw air.
The present invention is not limited to the above-mentioned specific embodiment; the above-mentioned specific embodiment only is schematic; be not restrictive; those of ordinary skill in the art is under enlightenment of the present invention; do not breaking away from the scope situation that aim of the present invention and claim protect; can also make a lot of forms, these all belong within protection scope of the present invention.
Claims (2)
1. a full liquia air separation method that utilizes cold energy of liquefied natural gas is characterized in that, its method is as follows:
1) after raw air filters dust impurity through self-cleaning air filter AF, enter air compressor TC1 and be compressed to 0.52Mpa, cooled to 2 ℃-10 ℃ by refrigerant glycol water or fluorine Lyons, then enter purification system and remove airborne moisture content, carbon dioxide impurities, raw air after the purification goes main heat exchanger E2 heat exchange, be cooled to-167 ℃ to-170 ℃, a part of raw air enters lower tower C1 through the second raw air pipeline (2); Another part raw air enters lower tower C1 through liquefier E7 liquefaction for liquid air and through liquid air pipeline (3), carries out caloic exchange, condensation evaporation at lower tower C1, obtains successively nitrogen, liquid nitrogen, liquid nitrogen fraction, lean solution sky, oxygen-enriched liquid air;
2) oxygen-enriched liquid air described 1) is crossed the further rectifying of tower C2 in the cold deutomerite diffluence through subcooler E3, described 1) nitrogen that lower tower C1 top obtains in removes condenser/evaporator K1, be condensed into liquid nitrogen, part liquid nitrogen is as the phegma of lower tower, another part liquid nitrogen is crossed through subcooler E3 and is gone the further rectifying of upper tower C2, described 1 after cold) in the liquid nitrogen fraction that obtains of lower tower C1, lean solution sky cross through subcooler E3 by liquid nitrogen fraction passage (6), lean solution sky passage (7) respectively and go upper tower C2 to participate in further rectifying after cold;
When nitrogen is condensed into liquid nitrogen in condenser/evaporator K1,1) liquid oxygen among the upper tower C2 is evaporated the rising gas as upper tower C2, and phegma, oxygen-enriched liquid air conduct heat between filler, mass transfer, oxygen, nitrogen separate, upper tower C2 bottom obtains highly purified liquid oxygen output ice chest I, it is that 8%-12% argon fraction is sent into argon producing system that upper tower C2 middle part obtains volume ratio, produces smart argon and exports ice chest I, and the nitrogen at upper tower C2 top is cooling box I after subcooler E3, main heat exchanger E2 re-heat;
3) with 1), 2) in the nitrogen that obtains of lower tower C1 top the 3rd pipeline (14) of extracting a part of nitrogen that a part vaporizes out in the first pipeline (13) and output liquefier E7 remove main heat exchanger E2 after merging, with cooling box I after the first raw air pipeline (1) heat exchange intensification, then remove ice chest II, extract out after in high pressure heat exchanger E1, being cooled to-120 ℃ to-126 ℃ by liquified natural gas (26), send into low pressure recycle nitrogen compressor TC2; Another part nitrogen of vaporizing among the liquefier E7 by the 4th pipeline (15) after high pressure heat exchanger E1 is warmed up to-120 ℃ to-126 ℃, send into low pressure recycle nitrogen compressor TC2, the isolated nitrogen of the first gas-liquid separator SV1 is also extracted out after high pressure heat exchanger E1 is warmed up to-120 ℃-126 ℃, send into low pressure recycle nitrogen compressor TC2, after returning high pressure heat exchanger E1 after the low pressure recycle nitrogen compressor TC2 supercharging again to be cooled to-120 ℃ to-126 ℃, extract out and remove Medium pressure cycle nitrogen compressor TC3, return heat exchanger E1 after the supercharging, reclaim the cold of liquefied natural gas, liquefaction is liquid nitrogen, extract out after the liquid nitrogen part throttling that is liquefied is warmed up to-120 ℃ to-126 ℃ by heat exchanger E1 and remove Medium pressure cycle nitrogen compressor TC3, the residue liquid nitrogen advances the first gas-liquid separator SV1, a liquid nitrogen part of separating is removed liquefier E7 liquefied air through second pipe (19), self is evaporated to nitrogen, another part liquid nitrogen removes the second gas-liquid separator SV2, liquid after the separation is sent as product, and gas is through heat exchanger E1 re-heat cooling box II;
4) liquified natural gas in the liquid natural feed channel (26) described 3) in high pressure heat exchanger E1 by re-heat, from the liquid natural feed channel (26) at high pressure heat exchanger E1 middle part, extract a part of natural gas out and remove heat exchanger E4 cooling glycol water or freon, remainder is extracted out with after the merging of the natural gas after the heat exchanger E4 re-heat from high pressure heat exchanger E1 is terminal, finally obtain the natural gas more than 2 ℃, the refrigerant that is cooled removes intercooler of air compressor E6 and aftercooler E5, the compressed air of cooling-air compressor TC1 arrives to 2 ℃-10 ℃, improve the efficient of air compressor TC1, reduce air compressor TC1 energy consumption.
2. the full liquia air separation method that utilizes cold energy of liquefied natural gas according to claim 1, it is characterized in that: lower tower C1 top is extracted a part of nitrogen out and remove main heat exchanger E2 after the first pipeline (13) and the 3rd pipeline (14) of exporting a part of nitrogen of vaporizing among the liquefier E7 is merged described 3), with cooling box I after the first raw air pipeline (1) heat exchange intensification, then remove ice chest II, extract out after in high pressure heat exchanger E1, being cooled to-120 ℃-126 ℃ by liquid natural feed channel (26), send into low pressure nitrogen press TC2; Another part nitrogen of vaporizing among the liquefier E7 by the 4th pipeline (15) after high pressure heat exchanger E1 is warmed up to-120 ℃-126 ℃, send into low pressure nitrogen press TC2, the isolated nitrogen of the first gas-liquid separator SV1 is also extracted out after high pressure heat exchanger E1 is warmed up to-120 ℃-126 ℃ by the 7th pipeline (18), send into low pressure nitrogen press TC2, after low-temp low-pressure cyclic nitrogen press TC2 supercharging, return high pressure heat exchanger E1 cooling, extract out after again being cooled to-120 ℃-126 ℃ and remove Medium pressure cycle nitrogen compressor TC3, return heat exchanger E1 after the supercharging, reclaim the cold of liquified natural gas, liquefaction is liquid nitrogen, a liquid nitrogen part that is liquefied is extracted out through the 8th pipeline (16) throttling is warmed up to-120 ℃-126 ℃ by heat exchanger E1 after and is removed Medium pressure cycle nitrogen compressor TC3, the residue liquid nitrogen advances the first gas-liquid separator SV1 by the 5th pipeline (17), a liquid nitrogen part of separating is removed liquefier E7 liquefied air through second pipe (19), self is evaporated to nitrogen, another part liquid nitrogen removes the second gas-liquid separator SV2 through the 6th pipeline (20), liquid is sent as product through liquid nitrogen output channel (21), and gas passes through the 9th pipeline (22) through heat exchanger E1 re-heat cooling box II.
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| CN105865147B (en) * | 2016-05-27 | 2018-05-11 | 开封空分集团有限公司 | The system and method for high purity carbon monoxide and hydrogen rich gas coproduction liquid methane |
| CN110701870B (en) * | 2019-05-29 | 2022-07-12 | 苏州市兴鲁空分设备科技发展有限公司 | Air separation device and method utilizing LNG cold energy |
| CN113587551B (en) * | 2021-07-14 | 2022-11-18 | 四川空分设备(集团)有限责任公司 | Air separation system and method for producing liquid oxygen, liquid nitrogen and liquid argon by using LNG cold energy |
| CN113587552B (en) * | 2021-07-14 | 2022-11-18 | 四川空分设备(集团)有限责任公司 | Air separation system and air separation method utilizing LNG cold energy |
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