CN106885448A - Using the air-separating technology of high-pressure liquefaction natural gas cold energy - Google Patents
Using the air-separating technology of high-pressure liquefaction natural gas cold energy Download PDFInfo
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- CN106885448A CN106885448A CN201510940475.3A CN201510940475A CN106885448A CN 106885448 A CN106885448 A CN 106885448A CN 201510940475 A CN201510940475 A CN 201510940475A CN 106885448 A CN106885448 A CN 106885448A
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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
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
- F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—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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- 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
- F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
- 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
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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
- F25J3/04333—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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
- F25J3/04933—Partitioning walls or sheets
- F25J3/04939—Vertical, e.g. dividing wall 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
- F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
Abstract
The invention discloses a kind of air-separating technology of utilization high-pressure liquefaction natural gas cold energy, belong to technical field of air separation.In the technique, saturated air enters the lower tower of fractionation carries out rectifying, obtains gas nitrogen and oxygen-enriched liquid air；Oxygen-enriched liquid air enters the upper tower of fractionation carries out rectifying, part gas nitrogen is cooled down after main heat exchanger re-heat as cyclic nitrogen into liquefied natural gas heat exchanger, liquefaction heat exchange gas device is returned after cyclic nitrogen compressor compresses further to cool down, then the lower tower of fractionation is returned after main heat exchanger supercooling；Cold logistics in liquefied natural gas heat exchanger is high-pressure liquefaction natural gas；Tower is internally provided with vertical clapboard and horizontal baffle in fractionation, and one end of horizontal baffle is connected with the upper end of vertical clapboard, and the other end of horizontal baffle is connected with the side wall of the upper tower of fractionation；The withdrawn position of liquid argon product is located on the side wall that the upper tower of fractionation is connected with horizontal baffle, horizontal baffle lower section.The technique can directly obtain the liquid argon of purity 99.5% from the upper tower of fractionation, and energy consumption is low, stable operation, safety.
Description
Technical field
The present invention relates to technical field of air separation, more particularly to a kind of utilization high-pressure liquefaction natural gas cold energy
Air-separating technology.
Background technology
Air separates abbreviation space division, is the difference using the physical property of each component in air, cold using depth
The mistake that the methods such as jelly, absorption, UF membrane separate oxygen, nitrogen, argon etc. from air in liquid form
Journey.By the products such as the isolated liquid oxygen of air, liquid nitrogen and liquid argon be widely used in metallurgy, petrochemical industry,
The fields such as machinery, chemical fertilizer, glass, military project, food, medical treatment.Air is separated generally to be needed in 80~100K
Carried out in a low temperature of (- 193 DEG C~-173 DEG C), create and maintain low temperature to need to consume substantial amounts of energy.How
Reducing the energy consumption in air separation process turns into the problem of people's extensive concern.
Liquefied natural gas (Liquefied Natural Gas, LNG) is natural gas (Natural Gas, LNG)
Purified, liquefaction liquid mixture, its temperature is about -162 DEG C.Liquefied natural gas is contained huge
Cold energy, when liquefied natural gas under 0.1MPa pressure from -162 DEG C of re-heats to 5 DEG C when the cold energy that is discharged be about
230kW·h/t.And due to the temperature to be reached needed for air separation process than liquefied natural gas temperature also
It is low, therefore, the cold energy of liquefied natural gas is used for the optimum utilization that air separation is cold energy of liquefied natural gas
Mode.During actual fed, generally the pressure of liquefied natural gas is improved to pressure higher (for example
Conveyed again more than 1MPa).And when the pressure of liquefied natural gas is improved, one part cold energy is converted into
Pressure energy, so that its cold energy discharged in gasification is reduced, therefore, for high-pressure liquefaction natural gas
For, it is ensured that its cold energy can be fully used.
United States Patent (USP) US5220798A, United States Patent (USP) US5137558A, Chinese utility model patent
CN2499774Y, Chinese invention patent CN101033910, Chinese invention patent CN101532768 and
All disclosed using the air of high-pressure liquefaction natural gas cold energy in the documents such as Chinese invention patent CN101846436
Separating technology.In above-mentioned air-separating technology：In the isolated high-purity of the fractionating column of air gas separation unit
Liquid nitrogen, the liquid oxygen and crude argon of high-purity.A part of high-purity liquid nitrogen is extracted out as cyclic nitrogen compression,
Make liquefied natural gas gasifying, gasification release in liquefied natural gas heat exchanger with high-pressure liquefaction natural gas heat exchange
Cold energy pass to cyclic nitrogen, after cyclic nitrogen condensation liquefaction return fractionating column in provide air separate needed for it is cold
Amount.Wherein, it is to draw nitrogen from the upper top of tower of fractionation to make in air-separating technology disclosed in CN101033910
It is cyclic nitrogen, number of compression stages is more in the technique, stream sizes are more, energy consumption is higher；CN101532768 is disclosed
Air-separating technology using the compression of two sections of low-temperature circulating nitrogen, operating pressure is high, and heat exchanger channel number is more,
Flow is complicated；In air-separating technology disclosed in CN101846436 liquid nitrogen product from high-pressure liquefaction natural gas
Obtained at cyclic nitrogen after heat exchange, increased the risk that high-pressure liquefaction natural gas leakage is polluted to product.
To sum up, realize it is of the invention during, inventor find prior art at least there is problems with：
The purity of argon obtained in fractionating column in the air-separating technology of existing utilization high-pressure liquefaction natural gas cold energy compared with
It is low further to be refined, it is necessary to be delivered to crude argon column so that air separation process energy consumption is higher.And,
Existing air-separating technology can not make full use of the cold energy of high-pressure liquefaction natural gas.
The content of the invention
In order to solve the above-mentioned technical problem, a kind of energy consumption of present invention offer is low, can make full use of the utilization of cold energy
The air-separating technology of high-pressure liquefaction natural gas cold energy.
Specifically, including following technical scheme：
A kind of air-separating technology of utilization high-pressure liquefaction natural gas cold energy, the pressure of the high-pressure liquefaction natural gas
Power is 1MPa~10MPa；The air-separating technology includes：Saturated air from main heat exchanger is by being fractionated
Lower tower bottom carries out rectifying into tower under the fractionation, obtains gas nitrogen and oxygen-enriched liquid air；The oxygen-enriched liquid air by
Tower top carries out rectifying into tower in the fractionation in fractionation, obtains liquid argon product and liquid oxygen product, the liquid
Argon product is extracted out from tower lateral line withdrawal function in the fractionation, the liquid oxygen product from tower bottom in the fractionation；One
Part gas nitrogen is extracted out by the lower top of tower of fractionation and obtains liquid nitrogen by the condenser condensation of boiling again of the upper tower bottom of fractionation,
As the liquid-phase reflux of tower under liquid nitrogen product and the upper tower of fractionation and fractionation after the liquid nitrogen extraction；Another part
Gas nitrogen is extracted out as cyclic nitrogen from top of tower under the fractionation, and the cyclic nitrogen is after the main heat exchanger re-heat
Into the cooling of liquefied natural gas heat exchanger, the liquefied natural gas heat exchange is returned to after cyclic nitrogen compressor compresses
Device is further cooled down, then through the main heat exchanger be subcooled after return to the fractionation under top of tower as liquid-phase reflux；
Cold logistics in the liquefied natural gas heat exchanger includes the high-pressure liquefaction natural gas；Wherein, the fractionation
Upper tower is internally provided with vertical clapboard and horizontal baffle, one end of the horizontal baffle and the vertical clapboard
Upper end connects, and the other end of the horizontal baffle is connected with the side wall of tower in the fractionation；The liquid argon product
Withdrawn position be located in the fractionation on the side wall that is connected with the horizontal baffle of tower and positioned at the level
The lower section of dividing plate.
Further, the oxygen-enriched liquid air is cold through liquid air liquid nitrogen subcooler after being extracted out by tower bottom under the fractionation
But entering back into tower in the fractionation afterwards carries out rectifying.
Further, the liquid nitrogen is divided into two parts after extracting out, and a part is returned by top of tower under the fractionation
Under the fractionation tower as tower under the fractionation liquid-phase reflux, another part is through the liquid air liquid nitrogen subcooler
Two parts are further divided into after cooling；A part is by top of tower in the fractionation into tower in the fractionation as described
The liquid-phase reflux of tower in fractionation, another part is delivered to liquid nitrogen storage tank as liquid nitrogen product.
Further, also obtain dirty nitrogen in the fractionation in tower distillation process, the dirty nitrogen with come from the liquid
The boil-off gas nitrogen of nitrogen storage tank enters the main heat exchanger after the liquid air liquid nitrogen subcooler re-heat together, as
Discharged after hot logistics heat exchange in the cold logistics of the main heat exchanger, with the main heat exchanger.
Further, the quantity of the cyclic nitrogen compressor is at least 2；Taken out by top of tower under the fractionation
The cyclic nitrogen for going out enters the main heat exchanger, as the cold logistics of the main heat exchanger, with the main heat exchanger
In hot logistics heat exchange after enter the liquefied natural gas heat exchanger, with the high-pressure liquefaction natural gas heat exchange after
Compressed into First cyclic nitrogen compressor, the cyclic nitrogen of compression is again introduced into the liquefied natural gas heat exchange
Enter in next cyclic nitrogen compressor after device, with high-pressure liquefaction natural gas heat exchange and compress, repeat
Above-mentioned steps, after the cyclic nitrogen is changed into liquid returning to the main heat exchanger is subcooled；After supercooling
Cyclic nitrogen is divided into two parts, a part with from the fractionation under top of tower cyclic nitrogen together with enter the master
Heat exchanger, used as the cold logistics of the main heat exchanger, another part enters described by top of tower under the fractionation
The lower tower of fractionation.
Further, the air-separating technology also includes：Raw air compresses through air compressor, air
Air is purified after forecooler precooling and air cleaning unit purification, the purify air enters the master
The saturated air is obtained after heat exchanger cooling.
Further, refrigerant is entered after the high-pressure liquefaction natural gas exchange heat through the liquefied natural gas heat exchanger
Refrigerant in heat exchanger, with the refrigerant heat exchanger is exchanged heat；The refrigerant is pre- for cooling down the air
Raw air in cooler.
Further, the flow of the high-pressure liquefaction natural gas is 35~40t/h.
Further, the outlet pressure of the cyclic nitrogen compressor is more than 3.5MPa.
The beneficial effect of technical scheme provided in an embodiment of the present invention is：
In the air-separating technology of utilization high-pressure liquefaction natural gas cold energy provided in an embodiment of the present invention, according to every
The operation principle of wall tower, sets vertical clapboard and horizontal baffle inside tower in fractionation, makes in fractionation tower simultaneously
Two centrifugations of tower of fractionating column and crude argon column in existing air-separating technology are played, can directly from fractionation
Liquid argon product of the upper tower lateral line withdrawal function purity more than 99.5%.Due to eliminating crude argon column, therefore the present invention is real
The air-separating technology energy consumption for applying example offer is significantly reduced.Meanwhile, air provided in an embodiment of the present invention is separated
Heat exchanger channel number is few in technique, heat-exchange system efficiency high.To sum up, air provided in an embodiment of the present invention
Separating technology can make full use of the high-grade cryogenic cold energy of high-pressure liquefaction natural gas, and technological process it is simple,
System operation safety and stability, significantly reduces energy consumption and equipment investment and running cost.
Brief description of the drawings
Technical scheme in order to illustrate more clearly the embodiments of the present invention, institute in being described to embodiment below
The accompanying drawing for needing to use is briefly described, it should be apparent that, drawings in the following description are only the present invention
Some embodiments, for those of ordinary skill in the art, on the premise of not paying creative work,
Other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is the stream of the air-separating technology of utilization high-pressure liquefaction natural gas cold energy provided in an embodiment of the present invention
Cheng Tu；
Fig. 2 is the structural representation of main heat exchanger and liquefied natural gas heat exchanger.
Reference is represented respectively：
1st, air compressor；2nd, air precooler；3rd, air cleaning unit；4th, main heat exchanger；
5th, it is fractionated lower tower；6th, tower in fractionation；7th, vertical clapboard；8th, horizontal baffle；9th, liquid nitrogen storage tank；
10th, liquefied natural gas heat exchanger；11st, refrigerant heat exchanger；12nd, first circulation nitrogen compressor；
13rd, second circulation nitrogen compressor；14th, first throttle valve；15th, second throttle；
16th, the 3rd choke valve；17th, the 4th choke valve；18th, liquid air liquid nitrogen subcooler；
A, raw air；B, purify air；C, saturated air；D, cyclic nitrogen；E, oxygen-enriched liquid air；
F, liquid oxygen product；G, liquid argon product；H, dirty nitrogen；I, boil-off gas nitrogen；J, liquid nitrogen product；
K, waste nitrogen；M, high-pressure liquefaction natural gas；N, liquid circulation nitrogen；
The feeding air passage of A1-A2, main heat exchanger；The gaseous recycle nitrogen passage of B1-B2, main heat exchanger；
The dirty nitrogen passage of C1-C2, main heat exchanger；The liquid circulation nitrogen passage of D1-D2, main heat exchanger；
The liquefied natural gas passage of E1-E2, liquefied natural gas heat exchanger；
The second compressed nitrogen passage of F1-F2, liquefied natural gas heat exchanger；
The first compressed nitrogen passage of G1-G2, liquefied natural gas heat exchanger；
The gaseous recycle nitrogen passage of H1-H2, liquefied natural gas heat exchanger.
Specific embodiment
To make technical scheme and advantage clearer, below in conjunction with accompanying drawing to embodiment party of the present invention
Formula is described in further detail.
The embodiment of the present invention provides a kind of air-separating technology of utilization high-pressure liquefaction natural gas cold energy, using pressure
Power carries out air separation for the cold energy of the high-pressure liquefaction natural gas of 1MPa~10MPa；Referring to Fig. 1, the air
Separating technology includes：
Saturated air c from main heat exchanger 4 enters the lower tower 5 of fractionation by the lower bottom of tower 5 of fractionation carries out rectifying,
Obtain gas nitrogen and oxygen-enriched liquid air e.Gained oxygen-enriched liquid air enters the upper tower 6 of fractionation by the upper top of tower 6 of fractionation carries out essence
Evaporate, obtain liquid argon product g and liquid oxygen product f, liquid argon product g is produced from the upper lateral line withdrawal function of tower 6 of fractionation, liquid oxygen
Product f is extracted out from the upper bottom of tower 6 of fractionation；A part in brought about the desired sensation nitrogen is extracted out through undue by the lower top of tower 5 of fractionation
The condenser condensation of boiling again for evaporating the bottom of tower 6 obtains liquid nitrogen, as liquid nitrogen product j and fractionation after liquid nitrogen extraction
The liquid-phase reflux of upper tower 6 and the lower tower 5 of fractionation；Another part gas nitrogen is extracted conduct out and is followed from the lower top of tower 5 of fractionation
Ring nitrogen d, cyclic nitrogen d are cooled down after the re-heat of main heat exchanger 4 into liquefied natural gas heat exchanger 10, through circulation
The further cooling of liquefaction heat exchange gas device 10 is returned after nitrogen compressor compresses, then after the supercooling of main heat exchanger 4
The lower top of tower 5 of fractionation is returned to as liquid-phase reflux；Cold logistics in liquefied natural gas heat exchanger 10 includes high pressure
Liquefied natural gas.
Wherein, tower 6 is internally provided with vertical clapboard 7 and horizontal baffle 8, one end of horizontal baffle 8 in fractionation
Upper end with vertical clapboard 7 is connected, and the other end of horizontal baffle 8 is connected with the side wall of the upper tower 6 of fractionation；Liquid
The withdrawn position of argon product g is located on the side wall that the upper tower 6 of fractionation is connected with horizontal baffle 8 and positioned at level
The lower section of dividing plate 8.
It is substantially a separation process for multicomponent mixture system that air is separated.Traditional multicomponent separation process
Multiple rectifying columns are generally needed, according to the relative volatility size of component, is separated from each rectifying column successively.
Each rectifying column is required for condenser and reboiler, and it is high that this results in traditional separating technology power consumption, long flow path,
Investment is big.And the design research and development of next door rectifying column solve above mentioned problem well.Separated with ternary mixture
As a example by, typical next door rectifying column is that two towers of conventional rectification sequence are integrated into a tower, and with one piece
Vertical dividing plate separates, and is divided into prefractionation section, public rectifying section, public stripping section and lateral line withdrawal function section four
Part, the reasonable diffluence of liquid phase and the reboiler backflow gas phase of being flowed back by overhead condenser, realizes that three components exist
Efficiently separating in one tower.The use of next door tower can improve process thermodynamics efficiency, and reducing energy consumption is simultaneously saved
Investment-saving.
According to the operation principle of above-mentioned next door tower, the upper tower 6 of fractionation is transformed in the embodiment of the present invention,
Vertical clapboard 7 and horizontal baffle 8 are set in fractionation in tower 6, and vertical clapboard 7 and the combination of horizontal baffle 8 are formed
Inverted "L" shaped, horizontal baffle 8 plays a part of to bind.Rectifying column is divided into prefractionator by vertical clapboard 7
And king-tower, feed side is prefractionator, and exit side is king-tower.Horizontal baffle 8 as binding, by fractionation
The liquid nitrogen reflux at the top of tower 6 separates with the argon gas that king-tower rises, so as to avoid backflow liquid nitrogen to liquid argon product
Pollution, improve liquid argon concentration.Tower 6 plays existing air-separating technology in improved fractionation simultaneously in
Two centrifugations of tower of fractionating column and crude argon column, can be directly from the upper tower lateral line withdrawal function purity of fractionation 99.5%
Liquid argon product above.Due to eliminating crude argon column, enable air-separating technology provided in an embodiment of the present invention
Consumption is significantly reduced.
The embodiment of the present invention is while tower 6 optimizes improvement on to fractionation, to cold in air-separating technology
Amount removal process has been also carried out Optimal improvements.In the embodiment of the present invention, raw air a through overcompression, precooling,
After the pre-treatments such as purification, saturation temperature is cooled to after cold logistics heat exchange into main heat exchanger 4, with main heat exchanger 4
Degree (- 173 DEG C or so), obtains saturated air c.Saturated air c enters the lower bottom of tower 5 of fractionation carries out rectifying.
Saturated air c under the fractionation in tower 5 be fractionated under under the tower top stream of tower 5 liquid-phase reflux is in multilayer column plate or fills out
Condensation evaporation in material repeatedly obtain purity reach 99.99% high-purity gas nitrogen and oxygen content 37% or so
Oxygen-enriched liquid air e.Wherein, oxygen-enriched liquid air e is gathered in the bottom of the lower tower 5 of fractionation, and gas nitrogen is then gathered in fractionation
The top of lower tower 5.The liquefaction that is condensed of brought about the desired sensation a nitrogen part obtains liquid nitrogen, and a part is used in this part liquid nitrogen
In the upper tower 6 of fractionation and the liquid-phase reflux of the lower tower 5 of fractionation, remaining is delivered to liquid nitrogen storage tank 9 as liquid nitrogen product j
Stored.Remaining gas nitrogen is then extracted out as cyclic nitrogen d by the lower top of tower 5 of fractionation, multiple through main heat exchanger 4
The technique streams such as heat, liquefied natural gas heat exchanger 10 are cooled down, the supercooling of cyclic nitrogen compressor compresses, main heat exchanger 4
The lower top of tower 5 of fractionation is returned to after journey, for the rectifying of the lower tower 5 of fractionation provides cold.Gained oxygen-enriched liquid air e is then
Entering the upper tower 6 of fractionation by the upper top of tower 6 of fractionation carries out rectifying, and extracting purity out by the upper bottom of tower 6 of fractionation reaches
99.88% high-purity liquid oxygen product f, the liquid argon product g of the lateral line withdrawal function purity 99.5% of tower 6 in fractionation.Liquid
The withdrawn position of argon product g is located on the side wall that the upper tower 6 of fractionation is connected with horizontal baffle 8 and positioned at level
The lower section of dividing plate 8.
Using above-mentioned air-separating technology, heat exchanger channel quantity can be reduced, improve the efficiency of heat-exchange system.
To sum up, air-separating technology provided in an embodiment of the present invention can make full use of high-pressure liquefaction natural gas
High-grade cryogenic cold energy, and technological process is simple, system operation safety and stability, significantly reduce energy consumption and
Equipment investment and running cost.
Further, in above-mentioned air-separating technology, the size of vertical clapboard 7 and horizontal baffle 8 with
And the position in tower 6 in fractionation does not have strict restriction, those skilled in the art can be according to actual conditions
It is determined that.For example, the height of vertical clapboard 7 can be 1/5,1/4,1/3,1/2 etc. of the upper tower height of tower 6 of fractionation,
The length of horizontal baffle 8 can be 1/5,1/4,1/3,1/2 etc. of the upper diameter of tower 6 of fractionation, horizontal baffle 8
The distance of the upper tower top of tower 6 of distance fractionation can be 1/5,1/4,1/3,1/2 etc. of the upper tower height of tower 6 of fractionation.
Further, in above-mentioned air-separating technology, oxygen-enriched liquid air e is extracted out by the lower bottom of tower 5 of fractionation
- 183 DEG C or so are cooled to by liquid air liquid nitrogen subcooler 18, then enter fractionation after the decompression of the 4th choke valve 17
The top of upper tower 6 is used as liquid phase feeding.
Further, in above-mentioned air-separating technology, obtained by fractionation lower tower 5 top gas nitrogen condensation
Liquid nitrogen is divided into two parts after being extracted out by the lower top of tower 5 of fractionation, a part returns to fractionation by the lower top of tower 5 of fractionation
Lower tower 5 is cooled to -183 DEG C as the liquid-phase reflux for being fractionated lower tower 5, another part through liquid air liquid nitrogen subcooler 18
Two parts are further divided into behind left and right；A part is entered by the upper top of tower 6 of fractionation after the decompression of second throttle 15 and divided
Liquid-phase reflux of the tower 6 as the upper tower 6 of fractionation is evaporated, another part is after the decompression of the 3rd choke valve 16 as liquid
Nitrogen product j is delivered to liquid nitrogen storage tank 9.
Further, in above-mentioned air-separating technology, oxygen-enriched liquid air e distillation processes of tower 6 in fractionation
In, in addition to the liquid oxygen product f and liquid argon product g that obtain high-purity, also obtain the dirt of nitrogen content 80% or so
Nitrogen h；A certain amount of boil-off gas nitrogen j can be produced in liquid nitrogen storage tank 9 simultaneously, in dirty nitrogen h and boil-off gas nitrogen j
Contain certain cold energy, therefore dirty nitrogen h and boil-off gas nitrogen j are delivered to liquid air liquid nitrogen subcooler 18 together
After re-heat, a part of the main heat exchanger 4 as the cold logistics of main heat exchanger 4 is then entered back into, with main heat exchanger 4
In hot logistics heat exchange, then as waste nitrogen k discharge.Using such technique, not only make dirty nitrogen h and steaming
The cold energy contained in nitrogen j of getting angry is fully used, and the temperature of dirty nitrogen h and boil-off gas nitrogen j is recovered to normal
Temperature, directly discharge will not be impacted to environment.
Further, in above-mentioned air-separating technology, the quantity of cyclic nitrogen compressor is at least 2；
The cyclic nitrogen d extracted out by the lower top of tower 5 of fractionation enters main heat exchanger 4, as the cold logistics of main heat exchanger 4,
Enter liquefied natural gas heat exchanger 10, the high-pressure liquefaction with outer confession with after the hot logistics heat exchange in main heat exchanger 4
Enter in First cyclic nitrogen compressor after natural gas m heat exchange and compress, the cyclic nitrogen of compression is again introduced into liquefaction
Enter in next cyclic nitrogen compressor after heat exchange gas device 10, with high-pressure liquefaction natural gas heat exchange and compress,
Repeat above-mentioned steps, until return main heat exchanger 4 is subcooled after cyclic nitrogen d is changed into liquid；Cross
Liquid circulation nitrogen n after cold is divided into two parts after being depressurized through first throttle valve 14, a part with fractionation
The cyclic nitrogen at the top of tower 5 enters main heat exchanger 4 together, and used as the cold logistics of main heat exchanger 4, another part is returned
Go back to the lower top of tower 5 of fractionation and enter the lower tower 5 of fractionation.It will be appreciated by persons skilled in the art that often by one
The pressure of recycle compressor compression Posterior circle nitrogen d is accordingly improved, after afterbody cyclic nitrogen compressor compresses
The pressure of cyclic nitrogen d reaches more than 3.5MPa, i.e. the outlet pressure of afterbody cyclic nitrogen compressor reaches
More than 3.5MPa.
Further, in above-mentioned air-separating technology, set between tower 6 and the lower tower 5 of fractionation in fractionation
Have and boil condenser again；The bottom that condenser is located at the upper tower 6 of fractionation is boiled again.The part gas at the lower top of tower 5 of fractionation
Nitrogen is liquefied by the above-mentioned condenser that boils again, the liquid oxygen of the upper bottom of towe of tower 6 of condensation heat vaporization fractionation.Due to identical
The boiling point of nitrogen is less than oxygen under pressure, therefore the lower tower 5 of fractionation runs under an operating pressure higher,
Motive force is provided as condenser is boiled again.
Further, in above-mentioned air-separating technology, raw air a is cooled down into main heat exchanger 4
To before saturation, first compressed through air compressor 1, the precooling of air precooler 2 and air cleaning unit 3
Purification, so as to be purified air b, purify air b is entered back into after main heat exchanger 4 is cooled down and is obtained saturated air
c.Wherein, raw air a is compressed to 0.5MPa~0.7MPa or so, air precooler by air compressor 1
Raw air a is cooled to 25~35 DEG C by 2 in advance, and air cleaning unit 3 removes water, the dioxy in raw air a
Change carbon, hydrogen sulfide and hydrocarbons etc. to pipeline and the harmful impurity of equipment.The tool of air cleaning unit 3
The body type embodiment of the present invention is not particularly limited, this area conventional technical means.
Further, in above-mentioned air-separating technology, high-pressure liquefaction natural gas m is changed through liquefied natural gas
Hot device 10 still has a part of cold energy after exchanging heat, in order that its cold energy is fully used, can be conveyed
Refrigerant into refrigerant heat exchanger 11, with refrigerant heat exchanger 11 is exchanged heat, for refrigerant therein provides cold energy.
The raw air a that refrigerant can be used in cooling air forecooler 2.Refrigerant can be water, glycol water
Deng cooling medium.
Further, in above-mentioned air-separating technology, the flow of high-pressure liquefaction natural gas can be
35~40t/h, such as 36t/h, 37t/h, 38t/h, 39t/h etc..
In accordance with the above, the cold logistics in main heat exchanger 4 includes two parts：A part is by the upper tower 6 of fractionation
The boil-off gas nitrogen i evaporated in the dirty nitrogen h and liquid nitrogen storage tank 9 of top extraction, another part is by under fractionation
The cyclic nitrogen and part that the top of tower 5 is extracted out are subcooled the liquid circulation nitrogen for obtaining through main heat exchanger 4.Main heat exchange
Hot logistics in device 4 equally includes two parts：A part is purify air b, and another part is from liquefaction day
The liquid circulation nitrogen of right gas heat exchanger 10.
Cold logistics in liquefied natural gas heat exchanger 10 is outer confession high-pressure liquefaction natural gas m, and hot logistics includes two
Part：One branch is the cyclic nitrogen from main heat exchanger 4, and another part is to add through each cyclic nitrogen compressor
Cyclic nitrogen after pressure.
Air-separating technology provided in an embodiment of the present invention is made further in detail below by specific test data
Describe in detail bright.
The air-separating technology of example 1 below~3 can be realized by following air-seperation system, referring to Fig. 1
And Fig. 2 is combined, the air-seperation system includes：Air compression pre-cooling unit, air cleaning member, air essence
Evaporate unit and cold energy of liquefied natural gas recovery unit.Wherein,
Air compression pre-cooling unit includes air compressor 1 and air precooler 2；
Air cleaning member is including miscellaneous for removing air reclaimed water, carbon dioxide, hydrogen sulfide, hydrocarbons etc.
The air cleaning unit 3 of matter；
Air rectification cell includes the upper tower 6 of fractionation, is fractionated lower tower 5, the tower 5 under the upper tower 6 of fractionation and fractionation
Between boil condenser, liquid air liquid nitrogen subcooler 18 and liquid nitrogen storage tank 9 again；Wherein, in fractionation in tower 6
Portion is provided with vertical clapboard 7 and horizontal baffle 8, and one end of horizontal baffle 8 is connected with the upper end of vertical clapboard 7,
The other end of horizontal baffle 8 is connected with the side wall of the upper tower 6 of fractionation.
Cold energy of liquefied natural gas recovery unit includes that main heat exchanger 4, liquefied natural gas heat exchanger 10, first follow
Ring nitrogen compressor 12, second circulation nitrogen compressor 13 and refrigerant heat exchanger 11.Wherein, main heat exchanger 4
In be provided with feeding air passage A1-A2, dirty nitrogen channel C 1-C2, gaseous recycle nitrogen passage B1-B2 and
Liquid circulation nitrogen passage D1-D2.Be provided with liquefied natural gas heat exchanger 10 liquefied natural gas passage E1-E2,
Gaseous recycle nitrogen passage H1-H2, the first compressed nitrogen passage G1-G2 and the second compressed nitrogen passage F1-F2.
Air compressor 1, air precooler 2, air cleaning unit 3, the feeding air of main heat exchanger 4 lead to
Road A1-A2 and the air intlet positioned at the lower bottom of tower 5 of fractionation are sequentially connected.
Oxygen-enriched liquid air outlet, liquid air liquid nitrogen subcooler 18 positioned at the lower bottom of tower 5 of fractionation and in fractionation
The oxygen-enriched liquid air import on the top of tower 6 is sequentially connected.
Positioned at the liquid nitrogen exit at the lower top of tower 5 of fractionation, two liquid nitrogen branch roads are set, one be located under fractionation
The phegma entrance at the top of tower 5 is connected, and another by being further divided into two branch roads after liquid air liquid nitrogen subcooler 18.
One is connected with the phegma entrance positioned at the upper top of tower 6 of fractionation, and another is connected with liquid nitrogen storage tank 9.
Cyclic nitrogen outlet, the gaseous recycle nitrogen passage B1-B2 of main heat exchanger 4 positioned at the lower top of tower 5 of fractionation,
The gaseous recycle nitrogen passage H1-H2 of liquefied natural gas heat exchanger 10, first circulation nitrogen compressor 12, liquefaction day
First compressed nitrogen passage G1-G2 of right gas heat exchanger 10, second circulation nitrogen compressor 13, liquefied natural gas are changed
Second compressed nitrogen passage F1-F2 of hot device 10 and the liquid circulation nitrogen passage D1-D2 of main heat exchanger 4 are sequentially
It is connected；The liquid circulation nitrogen passage D1-D2 outlets of main heat exchanger 4 set two branch roads, one and and position
Cyclic nitrogen entrance in the lower top of tower 5 of fractionation is connected, another with the gaseous recycle nitrogen passage of main heat exchanger 4
It is connected.
Positioned at the nothing of the outlet of dirty nitrogen, liquid air liquid nitrogen subcooler 18 and main heat exchanger 4 at the upper top of tower 6 of fractionation
Nitrogen passage is sequentially connected.
The liquefied natural gas passage E1-E2 of liquefied natural gas heat exchanger 10 is connected with refrigerant heat exchanger 11.
The liquid oxygen outlet of tower 6 is located at the bottom of the upper tower 6 of fractionation in fractionation, the liquid argon outlet position of tower 6 in fractionation
In on the side wall that the upper tower 6 of fractionation is connected with horizontal baffle 8 and positioned at the lower section of horizontal baffle 8.
First throttle valve 14 is provided near the liquid circulation nitrogen channel outlet of main heat exchanger 4；Liquid air liquid nitrogen mistake
Second throttle 15 is provided with the pipeline that cooler 18 is connected with the phegma import of the upper tower 6 of fractionation, with liquid nitrogen
The 3rd choke valve 16 is provided with the connected pipeline of storage tank 9, the oxygen-enriched liquid air import with the upper tower 6 of fractionation is connected
Pipeline on be provided with the 4th choke valve 17.
Embodiment 1
The present embodiment provides a kind of air-separating technology of utilization high-pressure liquefaction natural gas cold energy, in the present embodiment
The pressure of liquefied natural gas used is 1MPa, and the air-separating technology of the present embodiment is specific as follows：
The raw air a of 30t/h normal temperature and pressures is compressed to 0.6MPa by air compressor 1, in air precooling
30 DEG C are cooled in device 2, water, carbon dioxide, hydrogen sulfide, hydrocarbon are removed subsequently into air cleaning unit 3
The impurity such as class material, are purified air b.Purify air b in main heat exchanger 4 with cyclic nitrogen and from point
The boil-off gas nitrogen i heat exchange for evaporating the dirty nitrogen h at the top of tower 6 and being evaporated from liquid nitrogen storage tank 9, is cooled to
Into tower rectifying under the lower bottom of tower 5 participates in is fractionated after -173.1 DEG C, tower 5 is interior and phegma is in column plate under fractionation
Or continuous caloic exchange and condensation evaporation are carried out in filler, the bottom of tower 5 obtains 20t/h oxygen content under fractionation
It is the oxygen-enriched liquid air e of 37.8% (wt), the tower top of tower 5 obtains purity up to the height of 99.99% (wt) under fractionation
Purity gas nitrogen, condensation portion condensation of a part of gas nitrogen by boiling condenser again obtains liquid nitrogen, gained liquid nitrogen one
Used as the lower top liquid-phase reflux of tower 5 of fractionation, remaining is extracted out by the lower top of tower 5 of fractionation for part；Remaining 14.5t/h
Gas nitrogen is sent to the cooling of main heat exchanger 4 and is entered nitrogen cycle as cyclic nitrogen by the lower top of tower 5 extraction of fractionation.
The cyclic nitrogen d for extracting out at the lower top of tower 5 is fractionated through the re-heat of main heat exchanger 4 to -22 DEG C, subsequently into liquefaction
Heat exchange gas device 10 is cooled to -130 DEG C, then is compressed to 1.5MPa by first circulation nitrogen compressor 12,
It is then returned to liquefied natural gas heat exchanger 10 and is cooled to -130 DEG C again, then by second circulation nitrogen compressor 13
3.5MPa is compressed to, return liquefaction heat exchange gas device 10 is cooled to -150 DEG C of whole liquefaction and obtains liquid circulation
Nitrogen n, liquid circulation nitrogen n return to main heat exchanger 4 and cross and be cooled to -172 DEG C, by after the decompression of first throttle valve 14
It is divided into two strands, one cyclic nitrogen d extracted out with the lower tower 5 of fractionation mixes return main heat exchanger 4 and completes nitrogen cycle,
Another strand of cold returned needed for the lower top of the tower 5 offer air of fractionation is separated；The top of tower 6 is extracted out in fractionation
15.5t/h nitrogen contents are the dirty nitrogen h of 80.61% (wt), are changed through liquid air liquid nitrogen subcooler 18 and liquefied natural gas
The re-heat of hot device 10 to 10 DEG C as waste nitrogen k discharge.The China and foreign countries of liquefied natural gas heat exchanger 10 for flow be 37.4t/h,
Pressure is 1MPa, the high-pressure liquefaction natural gas m that temperature is -150 DEG C, by liquefied natural gas heat exchanger 10
After extremely -125.5 DEG C of re-heat, the cold needed for refrigerant heat exchanger 11 provides refrigerant is sent to.
The liquid nitrogen that the lower top of tower 5 of fractionation is extracted out, crosses through liquid air liquid nitrogen subcooler 18 and is cooled to -183 DEG C, then takes out
Go out 0.56t/h by entering the upper top of tower 6 of fractionation after the decompression of second throttle 15 as liquid nitrogen reflux, remaining warp
3rd choke valve 16 enters liquid nitrogen storage tank 9 after being decompressed to 120kPa as liquid nitrogen product j, in liquid nitrogen storage tank 9
The boil-off gas nitrogen i of evaporation mixes with dirt nitrogen h and is sent to liquid air liquid nitrogen subcooler 18 and the re-heat of main heat exchanger 4 and provides
Cold；The oxygen-enriched liquid air e of the lower bottom of tower 5 of fractionation is crossed through liquid air liquid nitrogen subcooler 18 and is cooled to -183 DEG C and through the
Four choke valve 17 enters the upper top of tower 6 of fractionation as liquid phase feeding after depressurizing.
While gas nitrogen is condensed in boiling condenser again, liquid oxygen is evaporated into gas oxygen as the upper bottom of tower 6 of fractionation
Portion's gas phase backflow, is carried out continuously in column plate or filler with oxygen-enriched liquid air e and as the liquid nitrogen of liquid-phase reflux
Heat and mass, the bottom of towe of tower 6 extracts 4.8t/h purity up to high-purity liquid oxygen product f of 99.88% (wt) out in fractionation,
Liquid oxygen product f is routed directly to liquid oxygen storage tank；It is 99.5% from the upper lateral line withdrawal function 45kg/h amounts containing argon of tower 6 of fractionation
(wt) high-purity liquid argon product g, is sent to smart ar system and further refines；The top of tower 6 is extracted out in fractionation
15.5t/h nitrogen contents are the dirty nitrogen of 80.61% (wt), are entered after mixing with the boil-off gas nitrogen i evaporated in storage tank
Reclaimed by main heat exchanger 4 after the part re-heat of liquid air liquid nitrogen subcooler 18 and cold and emptied.
Embodiment 2
The present embodiment provides a kind of air-separating technology of utilization high-pressure liquefaction natural gas cold energy, in the present embodiment
The pressure of liquefied natural gas used is 8MPa, and the air-separating technology of the present embodiment is specific as follows：
The raw air a of 30t/h normal temperature and pressures is compressed to 0.6MPa by air compressor 1, in air precooling
30 DEG C are cooled in device 2, water, carbon dioxide, hydrogen sulfide, hydrocarbon are removed subsequently into air cleaning unit 3
The impurity such as class material, are purified air b.Purify air b in main heat exchanger 4 with cyclic nitrogen and from point
The boil-off gas nitrogen i heat exchange for evaporating the dirty nitrogen h at the top of tower 6 and being evaporated from liquid nitrogen storage tank 9, is cooled to
Into tower rectifying under the lower bottom of tower 5 participates in is fractionated after -173.1 DEG C, tower 5 is interior and phegma is in column plate under fractionation
Or continuous caloic exchange and condensation evaporation are carried out in filler, the bottom of tower 5 obtains 20t/h oxygen content under fractionation
It is the oxygen-enriched liquid air e of 37.8% (wt), the tower top of tower 5 obtains purity up to the height of 99.99% (wt) under fractionation
Purity gas nitrogen, condensation portion condensation of a part of gas nitrogen by boiling condenser again obtains liquid nitrogen, gained liquid nitrogen one
Used as the lower top liquid-phase reflux of tower 5 of fractionation, remaining is extracted out by the lower top of tower 5 of fractionation for part；Remaining 14.5t/h
Gas nitrogen is sent to the cooling of main heat exchanger 4 and is entered nitrogen cycle as cyclic nitrogen by the lower top of tower 5 extraction of fractionation.
The cyclic nitrogen d for extracting out at the lower top of tower 5 is fractionated through the re-heat of main heat exchanger 4 to -22 DEG C, subsequently into liquefaction
Heat exchange gas device 10 is cooled to -130 DEG C, then is compressed to 2MPa by first circulation nitrogen compressor 12, with
Liquefaction heat exchange gas device 10 is returned afterwards is cooled to -130 DEG C again, then by second circulation nitrogen compressor 13
5MPa is compressed to, return liquefaction heat exchange gas device 10 is cooled to -150 DEG C of whole liquefaction and obtains liquid circulation
Nitrogen n, liquid circulation nitrogen n return to main heat exchanger 4 and cross and be cooled to -173 DEG C, by after the decompression of first throttle valve 14
It is divided into two strands, one cyclic nitrogen d extracted out with the lower tower 5 of fractionation mixes return main heat exchanger 4 and completes nitrogen cycle,
Another strand of cold returned needed for the lower top of the tower 5 offer air of fractionation is separated；The top of tower 6 is extracted out in fractionation
15.5t/h nitrogen contents are the dirty nitrogen h of 80.61% (wt), are changed through liquid air liquid nitrogen subcooler 18 and liquefied natural gas
The re-heat of hot device 10 to 13 DEG C as waste nitrogen k discharge.The China and foreign countries of liquefied natural gas heat exchanger 10 for flow be 37.4t/h,
Pressure is 8MPa, the high-pressure liquefaction natural gas m that temperature is -150 DEG C, by liquefied natural gas heat exchanger 10
After extremely -82 DEG C of re-heat, the cold needed for refrigerant heat exchanger 11 provides refrigerant is sent to.
The liquid nitrogen that the lower top of tower 5 of fractionation is extracted out, crosses through liquid air liquid nitrogen subcooler 18 and is cooled to -183 DEG C, then takes out
Go out 0.56t/h by entering the upper top of tower 6 of fractionation after the decompression of second throttle 15 as liquid nitrogen reflux, remaining warp
3rd choke valve 16 enters liquid nitrogen storage tank 9 after being decompressed to 120kPa as liquid nitrogen product j, in liquid nitrogen storage tank 9
The boil-off gas nitrogen i of evaporation mixes with dirt nitrogen h and is sent to liquid air liquid nitrogen subcooler 18 and the re-heat of main heat exchanger 4 and provides
Cold；The oxygen-enriched liquid air e of the lower bottom of tower 5 of fractionation is crossed through liquid air liquid nitrogen subcooler 18 and is cooled to -183 DEG C and through the
Four choke valve 17 enters the upper top of tower 6 of fractionation as liquid phase feeding after depressurizing.
While gas nitrogen is condensed in boiling condenser again, liquid oxygen is evaporated into gas oxygen as the upper bottom of tower 6 of fractionation
Portion's gas phase backflow, is carried out continuously in column plate or filler with oxygen-enriched liquid air e and as the liquid nitrogen of liquid-phase reflux
Heat and mass, the bottom of towe of tower 6 extracts 4.8t/h purity up to high-purity liquid oxygen product f of 99.88% (wt) out in fractionation,
Liquid oxygen product f is routed directly to liquid oxygen storage tank；It is 99.5% from the upper lateral line withdrawal function 45kg/h amounts containing argon of tower 6 of fractionation
(wt) high-purity liquid argon product g, is sent to smart ar system and further refines；The top of tower 6 is extracted out in fractionation
15.5t/h nitrogen contents are the dirty nitrogen of 80.61% (wt), are entered after mixing with the boil-off gas nitrogen i evaporated in storage tank
Reclaimed by main heat exchanger 4 after the part re-heat of liquid air liquid nitrogen subcooler 18 and cold and emptied.
Embodiment 3
The present embodiment provides a kind of air-separating technology of utilization high-pressure liquefaction natural gas cold energy, in the present embodiment
The pressure of liquefied natural gas used is 5MPa, and the air-separating technology of the present embodiment is specific as follows：
The raw air a of 30t/h normal temperature and pressures is compressed to 0.6MPa by air compressor 1, in air precooling
30 DEG C are cooled in device 2, water, carbon dioxide, hydrogen sulfide, hydrocarbon are removed subsequently into air cleaning unit 3
The impurity such as class material, are purified air b.Purify air b in main heat exchanger 4 with cyclic nitrogen and from point
The boil-off gas nitrogen i heat exchange for evaporating the dirty nitrogen h at the top of tower 6 and being evaporated from liquid nitrogen storage tank 9, is cooled to
Into tower rectifying under the lower bottom of tower 5 participates in is fractionated after -173.1 DEG C, tower 5 is interior and phegma is in column plate under fractionation
Or continuous caloic exchange and condensation evaporation are carried out in filler, the bottom of tower 5 obtains 20t/h oxygen content under fractionation
It is the oxygen-enriched liquid air e of 37.8% (wt), the tower top of tower 5 obtains purity up to the height of 99.99% (wt) under fractionation
Purity gas nitrogen, condensation portion condensation of a part of gas nitrogen by boiling condenser again obtains liquid nitrogen, gained liquid nitrogen one
Used as the lower top liquid-phase reflux of tower 5 of fractionation, remaining is extracted out by the lower top of tower 5 of fractionation for part；Remaining 14.5t/h
Gas nitrogen is sent to the cooling of main heat exchanger 4 and is entered nitrogen cycle as cyclic nitrogen by the lower top of tower 5 extraction of fractionation.
The cyclic nitrogen d for extracting out at the lower top of tower 5 is fractionated through the re-heat of main heat exchanger 4 to -22 DEG C, subsequently into liquefaction
Heat exchange gas device 10 is cooled to -130 DEG C, then is compressed to 2MPa by first circulation nitrogen compressor 12, with
Liquefaction heat exchange gas device 10 is returned afterwards is cooled to -130 DEG C again, then by second circulation nitrogen compressor 13
4MPa is compressed to, return liquefaction heat exchange gas device 10 is cooled to -150 DEG C of whole liquefaction and obtains liquid circulation
Nitrogen n, liquid circulation nitrogen n return to main heat exchanger 4 and cross and be cooled to -172 DEG C, by after the decompression of first throttle valve 14
It is divided into two strands, one cyclic nitrogen d extracted out with the lower tower 5 of fractionation mixes return main heat exchanger 4 and completes nitrogen cycle,
Another strand of cold returned needed for the lower top of the tower 5 offer air of fractionation is separated；The top of tower 6 is extracted out in fractionation
15.5t/h nitrogen contents are the dirty nitrogen h of 80.61% (wt), are changed through liquid air liquid nitrogen subcooler 18 and liquefied natural gas
The re-heat of hot device 10 to 12 DEG C as waste nitrogen k discharge.The China and foreign countries of liquefied natural gas heat exchanger 10 for flow be 37.4t/h,
Pressure is 5MPa, the high-pressure liquefaction natural gas m that temperature is -150 DEG C, by liquefied natural gas heat exchanger 10
After extremely -90 DEG C of re-heat, the cold needed for refrigerant heat exchanger 11 provides refrigerant is sent to.
The liquid nitrogen that the lower top of tower 5 of fractionation is extracted out, crosses through liquid air liquid nitrogen subcooler 18 and is cooled to -183 DEG C, then takes out
Go out 0.56t/h by entering the upper top of tower 6 of fractionation after the decompression of second throttle 15 as liquid nitrogen reflux, remaining warp
3rd choke valve 16 enters liquid nitrogen storage tank 9 after being decompressed to 120kPa as liquid nitrogen product j, in liquid nitrogen storage tank 9
The boil-off gas nitrogen i of evaporation mixes with dirt nitrogen h and is sent to liquid air liquid nitrogen subcooler 18 and the re-heat of main heat exchanger 4 and provides
Cold；The oxygen-enriched liquid air e of the lower bottom of tower 5 of fractionation is crossed through liquid air liquid nitrogen subcooler 18 and is cooled to -183 DEG C and through the
Four choke valve 17 enters the upper top of tower 6 of fractionation as liquid phase feeding after depressurizing.
While gas nitrogen is condensed in boiling condenser again, liquid oxygen is evaporated into gas oxygen as the upper bottom of tower 6 of fractionation
Portion's gas phase backflow, is carried out continuously in column plate or filler with oxygen-enriched liquid air e and as the liquid nitrogen of liquid-phase reflux
Heat and mass, the bottom of towe of tower 6 extracts 4.8t/h purity up to high-purity liquid oxygen product f of 99.88% (wt) out in fractionation,
Liquid oxygen product f is routed directly to liquid oxygen storage tank；It is 99.5% from the upper lateral line withdrawal function 45kg/h amounts containing argon of tower 6 of fractionation
(wt) high-purity liquid argon product g, is sent to smart ar system and further refines；Top of tower is extracted out in fractionation
15.5t/h nitrogen contents are the dirty nitrogen of 80.61% (wt), are entered after mixing with the boil-off gas nitrogen i evaporated in storage tank
Reclaimed by main heat exchanger 4 after the part re-heat of liquid air liquid nitrogen subcooler 18 and cold and emptied.
To sum up, in air-separating technology provided in an embodiment of the present invention, on the one hand will the upper Deethanizer design of fractionation be every
Wall turriform formula, on the other hand optimizes improvement to cold recovery process, significantly reduces energy consumption and equipment
Investment.Air-separating technology stable operation provided in an embodiment of the present invention, it is safe, can largely produce height
The liquid oxygen of purity, liquid nitrogen, liquid argon, energy conservation and consumption reduction effects are notable, with economic benefit and Environmental Effect higher
Benefit.
The above is for only for ease of it will be understood by those skilled in the art that technical scheme, and without
To limit the present invention.All any modifications within the spirit and principles in the present invention, made, equivalent,
Improve etc., should be included within the scope of the present invention.
Claims (9)
1. a kind of air-separating technology of utilization high-pressure liquefaction natural gas cold energy, the high-pressure liquefaction natural gas
Pressure is 1MPa~10MPa；Characterized in that, the air-separating technology includes：
Saturated air from main heat exchanger (4) is by lower tower (5) bottom of fractionation into tower (5) under the fractionation
Rectifying is carried out, gas nitrogen and oxygen-enriched liquid air is obtained；
The oxygen-enriched liquid air enters tower (6) in the fractionation by upper tower (6) top of fractionation carries out rectifying, obtains
To liquid argon product and liquid oxygen product, the liquid argon product is from tower (6) lateral line withdrawal function, the liquid in the fractionation
Oxygen product is extracted out from tower (6) bottom in the fractionation；
A part of gas nitrogen is extracted out by lower tower (5) top of fractionation and boils condensation again by upper tower (6) bottom of fractionation
Device condensation obtains liquid nitrogen, as liquid nitrogen product and the upper tower (6) of fractionation and the lower tower of fractionation after the liquid nitrogen extraction
(5) liquid-phase reflux；Another part gas nitrogen is extracted out as cyclic nitrogen from tower (5) top under the fractionation,
The cyclic nitrogen is cooled down after the main heat exchanger (4) re-heat into liquefied natural gas heat exchanger (10), warp
The liquefied natural gas heat exchanger (10) is returned after cyclic nitrogen compressor compresses further to cool down, then through described
Tower (5) top is used as liquid-phase reflux under the fractionation is returned after main heat exchanger (4) supercooling；The liquefaction day
Cold logistics in right gas heat exchanger (10) includes the high-pressure liquefaction natural gas；
Wherein, tower (6) is internally provided with vertical clapboard (7) and horizontal baffle (8), institute in the fractionation
The one end for stating horizontal baffle (8) is connected with the upper end of the vertical clapboard (7), the horizontal baffle (8)
The other end be connected with the side wall of tower (6) in the fractionation；The withdrawn position of the liquid argon product is located at described
On the side wall that tower (6) is connected with the horizontal baffle (8) in fractionation and positioned at the horizontal baffle (8)
Lower section.
2. air-separating technology according to claim 1, it is characterised in that the oxygen-enriched liquid air is by institute
State and entered back into the fractionation after being cooled down through liquid air liquid nitrogen subcooler (18) after lower tower (5) bottom of fractionation is extracted out
Tower (6) carries out rectifying.
3. air-separating technology according to claim 2, it is characterised in that the liquid nitrogen is divided into after extracting out
Two parts, a part is by tower (5) under tower (5) the top return fractionation under the fractionation as described point
The liquid-phase reflux of lower tower (5) is evaporated, another part is further divided into after being cooled down through the liquid air liquid nitrogen subcooler (18)
Two parts；A part enters described point of tower (6) conduct in the fractionation by tower (6) top in the fractionation
The liquid-phase reflux of tower (6) is evaporated, another part is delivered to liquid nitrogen storage tank (9) as liquid nitrogen product.
4. air-separating technology according to claim 3, it is characterised in that tower (6) in the fractionation
Dirty nitrogen is also obtained in distillation process, the dirty nitrogen is passed through together with the boil-off gas nitrogen from the liquid nitrogen storage tank (9)
Enter the main heat exchanger (4) after the liquid air liquid nitrogen subcooler (18) re-heat, as the main heat exchanger
(4) discharged after the hot logistics heat exchange in cold logistics, with the main heat exchanger (4).
5. air-separating technology according to claim 1, it is characterised in that the cyclic nitrogen compressor
Quantity be at least 2；
The cyclic nitrogen extracted out by tower (5) top under the fractionation enters the main heat exchanger (4), used as described
Enter the liquid after hot logistics heat exchange in the cold logistics of main heat exchanger (4), with the main heat exchanger (4)
Change heat exchange gas device (10), First cyclic nitrogen compressor is entered after being exchanged heat with the high-pressure liquefaction natural gas
Middle compression, the cyclic nitrogen of compression is again introduced into the liquefied natural gas heat exchanger (10), with the high-pressure liquefaction
Enter in next cyclic nitrogen compressor after heat exchange gas and compress, repeat above-mentioned steps, followed when described
Ring nitrogen is changed into after liquid and returns to the main heat exchanger (4) and be subcooled；
Cyclic nitrogen after supercooling is divided into two parts, a part with from the circulation at the top of tower (5) under the fractionation
Nitrogen enters the main heat exchanger (4) together, as the cold logistics of the main heat exchanger (4), another part by
Tower (5) top enters tower (5) under the fractionation under the fractionation.
6. air-separating technology according to claim 1, it is characterised in that the air-separating technology
Also include：
Raw air is compressed through air compressor (1), air precooler (2) precooling and purification of air are filled
Air is purified after putting (3) purification, the purify air is obtained after entering the main heat exchanger (4) cooling
To the saturated air.
7. air-separating technology according to claim 7, it is characterised in that the high-pressure liquefaction is natural
Gas enters refrigerant heat exchanger (11) after being exchanged heat through the liquefied natural gas heat exchanger (10), is changed with the refrigerant
Refrigerant in hot device (11) is exchanged heat；The refrigerant is used to cool down the original in the air precooler (2)
Material air.
8. air-separating technology according to claim 1, it is characterised in that the high-pressure liquefaction is natural
The flow of gas is 35~40t/h.
9. air-separating technology according to claim 1, it is characterised in that the cyclic nitrogen compressor
Outlet pressure be more than 3.5MPa.
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|---|---|---|---|---|
| CN101943512A (en) * | 2010-09-29 | 2011-01-12 | 中国海洋石油总公司 | Air separation method utilizing cold energy of liquefied natural gas |
| CN104110940A (en) * | 2014-06-19 | 2014-10-22 | 中国寰球工程公司 | Efficient air separation device utilizing liquefied natural gas cold energy |
| CN104807286A (en) * | 2014-10-31 | 2015-07-29 | 刘继福 | Nitrogen liquefaction system allowing recycling of LNG (Liquefied Natural Gas) cold energy |
| CN204718302U (en) * | 2015-06-04 | 2015-10-21 | 刘琳琳 | A kind of oxygen enrichment system of efficiency utilization LNG cold energy |
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2015
- 2015-12-16 CN CN201510940475.3A patent/CN106885448B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101943512A (en) * | 2010-09-29 | 2011-01-12 | 中国海洋石油总公司 | Air separation method utilizing cold energy of liquefied natural gas |
| CN104110940A (en) * | 2014-06-19 | 2014-10-22 | 中国寰球工程公司 | Efficient air separation device utilizing liquefied natural gas cold energy |
| CN104807286A (en) * | 2014-10-31 | 2015-07-29 | 刘继福 | Nitrogen liquefaction system allowing recycling of LNG (Liquefied Natural Gas) cold energy |
| CN204718302U (en) * | 2015-06-04 | 2015-10-21 | 刘琳琳 | A kind of oxygen enrichment system of efficiency utilization LNG cold energy |
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