CN106885448B - Utilize the air-separating technology of high-pressure liquefaction natural gas cold energy - Google Patents
Utilize the air-separating technology of high-pressure liquefaction natural gas cold energy Download PDFInfo
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- CN106885448B CN106885448B CN201510940475.3A CN201510940475A CN106885448B CN 106885448 B CN106885448 B CN 106885448B CN 201510940475 A CN201510940475 A CN 201510940475A CN 106885448 B CN106885448 B CN 106885448B
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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
- F25J3/04006—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
- F25J3/04406—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
- F25J3/04642—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
- 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 technologies using 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 and carries out rectifying, obtains gas nitrogen and oxygen-enriched liquid air；Oxygen-enriched liquid air enters the upper tower of fractionation and carries out rectifying, it is cooling that part gas nitrogen enters liquefied natural gas heat exchanger as cyclic nitrogen after main heat exchanger re-heat, liquefaction heat exchange gas device is returned after cyclic nitrogen compressor compresses further to cool down, then is returned after main heat exchanger is subcooled and be fractionated lower tower；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 and the upper end of vertical clapboard connect, and the other end of horizontal baffle is connect with the side wall for being fractionated upper tower；The withdrawn position of liquid argon product, which is located at, to be fractionated on the side wall that upper tower is connect with horizontal baffle, below horizontal baffle.The technique can directly obtain the liquid argon of purity 99.5% from the upper tower of fractionation, and low energy consumption, stable operation, safety.
Description
Technical field
The present invention relates to technical field of air separation, in particular to a kind of air using high-pressure liquefaction natural gas cold energy point
Separating process.
Background technique
Air separation abbreviation space division using cryogenic refrigeration, is inhaled using the difference of the physical property of each component in air
The process that the methods of attached, UF membrane separates oxygen, nitrogen, argon etc. from air in liquid form.It is obtained by air separation
To the products such as liquid oxygen, liquid nitrogen and liquid argon be widely used in metallurgy, petrochemical industry, machinery, chemical fertilizer, glass, military project, food, medical treatment
Equal fields.Air separation usually requires to carry out in a low temperature of 80~100K (- 193 DEG C~-173 DEG C), creates and maintain low temperature
Need to consume a large amount of energy.How energy consumption in air separation process become people extensive concern the problem of is reduced.
Liquefied natural gas (Liquefied Natural Gas, LNG) be natural gas (Natural Gas, LNG) it is purified,
Liquid mixture made of liquefaction, temperature are about -162 DEG C.Liquefied natural gas contains huge cold energy, works as liquefied natural gas
The cold energy discharged when under 0.1MPa pressure from -162 DEG C of re-heats to 5 DEG C is about 230kWh/t.And due to air separation
Temperature to be achieved needed in the process is also lower than the temperature of liquefied natural gas, therefore, the cold energy of liquefied natural gas is used for sky
Gas separation is the Optimum utilization ways of cold energy of liquefied natural gas.During actual fed, usually by the pressure of liquefied natural gas
It more than raising to higher pressure (such as 1MPa) is conveyed again.And when the pressure of liquefied natural gas improves, part of it
Cold energy is converted into pressure energy, so that the cold energy for discharging it in gasification is reduced, therefore, high-pressure liquefaction natural gas is come
It says, 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, China
The documents such as patent of invention CN101033910, Chinese invention patent CN101532768 and Chinese invention patent CN101846436
In all disclose air-separating technology using high-pressure liquefaction natural gas cold energy.In above-mentioned air-separating technology: in air point
The liquid oxygen and crude argon of liquid nitrogen, high-purity from the isolated high-purity of the fractionating column of unit.A part of high-purity liquid nitrogen is extracted out
It is compressed as cyclic nitrogen, makes liquefied natural gas gasifying with high-pressure liquefaction natural gas heat exchange in liquefied natural gas heat exchanger, gasify
The cold energy of process release passes to cyclic nitrogen, returns after cyclic nitrogen condensation liquefaction cold needed for offer air separation in fractionating column
Amount.It wherein, is from upper top of tower extraction nitrogen is fractionated in air-separating technology disclosed in CN101033910 as cyclic nitrogen, it should
Number of compression stages is more in technique, stream sizes are more, energy consumption is higher；Air-separating technology disclosed in CN101532768 is low using two sections
Warm cyclic nitrogen compression, operating pressure is high, and heat exchanger channel number is more, and process is complicated；Air separation work disclosed in CN101846436
Liquid nitrogen product obtains from the cyclic nitrogen after exchanging heat with high-pressure liquefaction natural gas in skill, increases high-pressure liquefaction natural gas leakage pair
The risk that product pollutes.
To sum up, in the implementation of the present invention, the inventor finds that the existing technology has at least the following problems: existing benefit
It is lower with the purity of argon obtained in fractionating column in the air-separating technology of high-pressure liquefaction natural gas cold energy, it needs to be delivered to crude argon
Tower is further refined, so that air separation process energy consumption is higher.Moreover, existing air-separating technology cannot make full use of
The cold energy of high-pressure liquefaction natural gas.
Summary of the invention
Low energy consumption, can make full use of the utilization high pressure liquid of cold energy in order to solve the above technical problem, the present invention provides a kind of
Change the air-separating technology of natural gas cold energy.
Specifically, including following technical scheme:
A kind of air-separating technology using high-pressure liquefaction natural gas cold energy, the pressure of the high-pressure liquefaction natural gas are
1MPa~10MPa；The air-separating technology includes: the saturated air from main heat exchanger as being fractionated described in lower tower bottom entrance
It is fractionated lower tower and carries out rectifying, obtain gas nitrogen and oxygen-enriched liquid air；The oxygen-enriched liquid air is entered in the fractionation by being fractionated upper tower top
Tower carries out rectifying, obtains liquid argon product and liquid oxygen product, and the liquid argon product is from tower lateral line withdrawal function in the fractionation, the liquid oxygen
Product is extracted out from tower bottom in the fractionation；A part of gas nitrogen is by being fractionated lower top of tower extraction by being fractionated boiling again for upper tower bottom
Condenser condenses to obtain liquid nitrogen, as liquid nitrogen product and the upper tower of fractionation and the liquid phase time for being fractionated lower tower after the liquid nitrogen extraction
Stream；Another part gas nitrogen is used as cyclic nitrogen from top of tower extraction under the fractionation, and the cyclic nitrogen is through the main heat exchanger re-heat
It is cooling to enter liquefied natural gas heat exchanger afterwards, it is further that the liquefied natural gas heat exchanger is returned after cyclic nitrogen compressor compresses
It is cooling, then top of tower is returned after main heat exchanger supercooling under the fractionation as liquid-phase reflux；The liquefied natural gas changes
Cold logistics in hot device includes the high-pressure liquefaction natural gas；Wherein, tower is internally provided with vertical clapboard and water in the fractionation
Flat partition board, one end of the horizontal baffle are connect with the upper end of the vertical clapboard, the other end of the horizontal baffle with it is described
The side wall connection of tower in fractionation；The withdrawn position of the liquid argon product is located at what tower in the fractionation was connect with the horizontal baffle
Lower section on side wall and positioned at the horizontal baffle.
Further, after the oxygen-enriched liquid air is extracted out by tower bottom under the fractionation after liquid air liquid nitrogen subcooler is cooling again
Tower carries out rectifying on into the fractionation.
Further, it is divided into two parts after the liquid nitrogen extraction, a part returns to described point by top of tower under the fractionation
Liquid-phase reflux of the lower tower as tower under the fractionation is evaporated, another part is further divided into two after the liquid air liquid nitrogen subcooler is cooling
Point；A part enters liquid-phase reflux of the tower as tower in the fractionation in the fractionation, another portion by top of tower in the fractionation
It is allocated as being delivered to liquid nitrogen storage tank for liquid nitrogen product.
Further, also obtain dirty nitrogen in the fractionation in tower distillation process, the dirt nitrogen with come from the liquid nitrogen storage tank
Boil-off gas nitrogen together after the liquid air liquid nitrogen subcooler re-heat enter the main heat exchanger, as the cold of the main heat exchanger
It is discharged after hot logistics heat exchange in logistics, with the main heat exchanger.
Further, the quantity of the cyclic nitrogen compressor is at least 2；The circulation extracted out by top of tower under the fractionation
Nitrogen enters the main heat exchanger, laggard with the hot logistics heat exchange in the main heat exchanger as the cold logistics of the main heat exchanger
Enter the liquefied natural gas heat exchanger, is pressed with entering in First cyclic nitrogen compressor after high-pressure liquefaction natural gas heat exchange
Contracting, the cyclic nitrogen of compression are again introduced into the liquefied natural gas heat exchanger, under entering after high-pressure liquefaction natural gas heat exchange
It is compressed in one cyclic nitrogen compressor, repeats above-mentioned steps, returned to the master after the cyclic nitrogen is changed into liquid and change
Hot device is subcooled；Cyclic nitrogen after supercooling is divided into two parts, the cyclic nitrogen one of a part and the top of tower under the fractionation
It rises and enters the main heat exchanger, as the cold logistics of the main heat exchanger, another part enters institute by top of tower under the fractionation
State the lower tower of fractionation.
Further, the air-separating technology further include: raw air is compressed through air compressor, air precooler is pre-
Air is purified after the purification of cold and air cleaning unit, the purification air obtains institute after entering main heat exchanger cooling
State saturated air.
Further, the high-pressure liquefaction natural gas enters refrigerant after liquefied natural gas heat exchanger heat exchange and exchanges heat
Refrigerant in device, with the refrigerant heat exchanger exchanges heat；The raw material that the refrigerant is used to cool down in the air precooler is empty
Gas.
Further, the flow of the high-pressure liquefaction natural gas is 35~40t/h.
Further, the outlet pressure of the cyclic nitrogen compressor is 3.5MPa or more.
The beneficial effect of technical solution provided in an embodiment of the present invention is:
In air-separating technology provided in an embodiment of the present invention using high-pressure liquefaction natural gas cold energy, according to next door tower
Working principle is arranged vertical clapboard and horizontal baffle being fractionated inside upper tower, makes to be fractionated tower while playing existing air separation
The centrifugation of two towers of fractionating column and crude argon column in technique, can directly from be fractionated upper tower lateral line withdrawal function purity 99.5% with
On liquid argon product.Due to eliminating crude argon column, air-separating technology energy consumption provided in an embodiment of the present invention is significantly reduced.
Meanwhile heat exchanger channel number is few in air-separating technology provided in an embodiment of the present invention, heat-exchange system is high-efficient.To sum up, originally
The air-separating technology that inventive embodiments provide can make full use of the high-grade cryogenic cold energy of high-pressure liquefaction natural gas, and work
Skill process is simple, system operational safety is stablized, and significantly reduces energy consumption and equipment investment and operating cost.
Detailed description of the invention
To describe the technical solutions in the embodiments of the present invention more clearly, make required in being described below to embodiment
Attached drawing is briefly described, it should be apparent that, drawings in the following description are only some embodiments of the invention, for
For those of ordinary skill in the art, without creative efforts, it can also be obtained according to these attached drawings other
Attached drawing.
Fig. 1 is the flow chart of the air-separating technology provided in an embodiment of the present invention using high-pressure liquefaction natural gas cold energy；
Fig. 2 is the structural schematic diagram of main heat exchanger and liquefied natural gas heat exchanger.
Appended drawing reference respectively indicates:
1, air compressor；2, air precooler；3, air cleaning unit；4, main heat exchanger；
5, it is fractionated lower tower；6, tower in fractionation；7, vertical clapboard；8, horizontal baffle；9, liquid nitrogen storage tank；
10, liquefied natural gas heat exchanger；11, refrigerant heat exchanger；12, first circulation nitrogen compressor；
13, second circulation nitrogen compressor；14, first throttle valve；15, second throttle；
16, third throttle valve；17, the 4th throttle valve；18, liquid air liquid nitrogen subcooler；
A, raw air；B, air is purified；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 channel of A1-A2, main heat exchanger；The gaseous recycle nitrogen channel of B1-B2, main heat exchanger；
The dirty nitrogen channel of C1-C2, main heat exchanger；The liquid circulation nitrogen channel of D1-D2, main heat exchanger；
The liquefied natural gas channel of E1-E2, liquefied natural gas heat exchanger；
The second compressed nitrogen channel of F1-F2, liquefied natural gas heat exchanger；
The first compressed nitrogen channel of G1-G2, liquefied natural gas heat exchanger；
The gaseous recycle nitrogen channel of H1-H2, liquefied natural gas heat exchanger.
Specific embodiment
To keep technical solution of the present invention and advantage clearer, below in conjunction with attached drawing to embodiment of the present invention make into
One step it is described in detail.
The embodiment of the present invention provides a kind of air-separating technology using high-pressure liquefaction natural gas cold energy, is using pressure
The cold energy of the high-pressure liquefaction natural gas of 1MPa~10MPa carries out air separation；Referring to Fig. 1, which includes:
Saturated air c from main heat exchanger 4 enters the lower progress of tower 5 rectifying of fractionation by being fractionated lower 5 bottom of tower, obtains gas nitrogen
And oxygen-enriched liquid air e.Gained oxygen-enriched liquid air enters the upper tower 6 of fractionation by being fractionated upper 6 top of tower and carries out rectifying, obtain liquid argon product g and
Liquid oxygen product f, liquid argon product g are extracted out from upper 6 lateral line withdrawal function of tower, liquid oxygen product f is fractionated from upper 6 bottom of tower is fractionated；Brought about the desired sensation nitrogen
In a part condense to obtain liquid nitrogen by being fractionated the condenser that boils again of upper 6 bottom of tower by being fractionated at the top of lower tower 5 extraction, liquid nitrogen is taken out
As liquid nitrogen product j and the upper tower 6 of fractionation and the liquid-phase reflux for being fractionated lower tower 5 after out；Another part gas nitrogen is pushed up from lower tower 5 is fractionated
Portion's extraction is used as cyclic nitrogen d, and cyclic nitrogen d enters the cooling of liquefied natural gas heat exchanger 10 after 4 re-heat of main heat exchanger, through cyclic nitrogen
It is further cooling that liquefaction heat exchange gas device 10 is returned after compressor compresses, then is returned after the supercooling of main heat exchanger 4 and be fractionated lower tower 5
Top is as liquid-phase reflux；Cold logistics in liquefied natural gas heat exchanger 10 includes high-pressure liquefaction natural gas.
Wherein, tower 6 is internally provided with vertical clapboard 7 and horizontal baffle 8 in fractionation, one end of horizontal baffle 8 with vertically every
The upper end of plate 7 connects, and the other end of horizontal baffle 8 is connect with the side wall for being fractionated upper tower 6；The withdrawn position of liquid argon product g is located at
Lower section on the side wall that tower 6 is connect with horizontal baffle 8 in fractionation and positioned at horizontal baffle 8.
Air separation is substantially the separation process of a multicomponent mixture system.Traditional multicomponent separation process usually needs
Multiple rectifying columns are wanted, according to the relative volatility size of component, are successively separated from each rectifying column.Each rectifying column requires cold
Condenser and reboiler, it is high that this results in traditional separating technology to consume energy, long flow path, and investment is big.And the design of next door rectifying column is ground
Send out the very good solution above problem.By taking ternary mixture separates as an example, typical next door rectifying column is by conventional rectification sequence
Two towers be integrated into a tower, and separated with one piece of vertical partition, be divided into prefractionation section, public rectifying section, public stripping
Section and four parts of lateral line withdrawal function section are realized by the reasonable diffluence of overhead condenser reflux liquid phase and reboiler reflux gas phase
Three components efficiently separating in a tower.Process thermodynamics efficiency can be improved in the use of next door tower, reduces energy consumption and saves
Investment.
According to the working principle of above-mentioned next door tower, the upper tower 6 of fractionation is transformed in the embodiment of the present invention, is being fractionated upper tower
Vertical clapboard 7 and horizontal baffle 8 are set in 6, and vertical clapboard 7 and the combination of horizontal baffle 8 form inverted "L" shape, and horizontal baffle 8 plays
The effect bound.Rectifying column is divided into prefractionator and king-tower by vertical clapboard 7, and feed side is prefractionator, based on exit side
Tower.Horizontal baffle 8 separates the argon gas that the liquid nitrogen reflux for being fractionated upper 6 top of tower and king-tower rise as binding, so as to avoid
Flow back pollution of the liquid nitrogen to liquid argon product, improves the concentration of liquid argon.Tower 6 plays existing air separation simultaneously in improved fractionation
The centrifugation of two towers of fractionating column and crude argon column in technique, can directly from be fractionated upper tower lateral line withdrawal function purity 99.5% with
On liquid argon product.Due to eliminating crude argon column, significantly reduce air-separating technology energy consumption provided in an embodiment of the present invention.
The embodiment of the present invention is while optimizing fractionation upper tower 6, to cold recovery in air-separating technology
Improvement is also optimized in process.In the embodiment of the present invention, raw air a after the pre-treatments such as overcompression, pre-cooling, purification, into
Enter main heat exchanger 4, is cooled to saturation temperature (- 173 DEG C or so) after exchanging heat with logistics cold in main heat exchanger 4, obtains saturated air
c.Saturated air c enters lower 5 bottom of tower of fractionation and carries out rectifying.Saturated air c under fractionation in tower 5 with 5 tower top stream of tower under fractionation
Under condensation evaporation of the liquid-phase reflux in multilayer column plate or filler repeatedly obtain purity reach 99.99% high-purity gas nitrogen and
Oxygen-enriched liquid air e of the oxygen content 37% or so.Wherein, oxygen-enriched liquid air e is gathered in the bottom for being fractionated lower tower 5, and gas nitrogen is then assembled
The top of tower 5 under fractionation.The liquefaction that is condensed of brought about the desired sensation nitrogen a part obtains liquid nitrogen, and a part is for being fractionated in this part liquid nitrogen
Upper tower 6 and the liquid-phase reflux for being fractionated lower tower 5, remaining is delivered to liquid nitrogen storage tank 9 as liquid nitrogen product j and is stored.Remaining gas nitrogen
It is then extracted out as cyclic nitrogen d by being fractionated at the top of lower tower 5, through 4 re-heat of main heat exchanger, liquefied natural gas heat exchanger 10 is cooling, recycles
It is returned after the process flows such as nitrogen compressor compresses, the supercooling of main heat exchanger 4 and is fractionated lower 5 top of tower, provided to be fractionated the rectifying of lower tower 5
Cooling capacity.Gained oxygen-enriched liquid air e then enters the upper progress of tower 6 rectifying of fractionation by being fractionated upper 6 top of tower, by being fractionated upper 6 bottom of tower extraction
Purity reaches 99.88% high-purity liquid oxygen product f, in the liquid argon product g for being fractionated upper 6 lateral line withdrawal function purity 99.5% of tower.Liquid argon
The withdrawn position of product g is located at the lower section for being fractionated on the side wall that upper tower 6 is connect with horizontal baffle 8 and being located at horizontal baffle 8.
Using above-mentioned air-separating technology, heat exchanger channel quantity can be reduced, improves 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 the high-grade of high-pressure liquefaction natural gas
Cryogenic cold energy, and process flow is simple, system operational safety is stablized, significantly reduce energy consumption and equipment investment and operation at
This.
Further, it in above-mentioned air-separating technology, the size of vertical clapboard 7 and horizontal baffle 8 and is being fractionated
The not stringent restriction in position in upper tower 6, those skilled in the art can be determines according to actual conditions.For example, vertical clapboard 7
Height can for be fractionated upper 6 tower height of tower 1/5,1/4,1/3,1/2 etc., the length of horizontal baffle 8 can be straight to be fractionated upper tower 6
1/5,1/4,1/3,1/2 etc. of diameter, horizontal baffle 8 can be the 1/ of upper 6 tower height of tower of fractionation apart from the distance for being fractionated upper 6 tower top of tower
5,1/4,1/3,1/2 etc..
Further, in above-mentioned air-separating technology, oxygen-enriched liquid air e is by being fractionated after lower 5 bottom of tower is extracted out through liquid air
Liquid nitrogen subcooler 18 is cooled to -183 DEG C or so, then enters after the decompression of the 4th throttle valve 17 and be fractionated upper 6 top of tower as liquid phase
Charging.
Further, in above-mentioned air-separating technology, the liquid nitrogen condensed by 5 top gas nitrogen of tower under being fractionated is by dividing
It evaporates and is divided into two parts after extracting out at the top of lower tower 5, a part is fractionated lower tower 5 as tower 5 under being fractionated by returning at the top of tower 5 under being fractionated
Liquid-phase reflux, another part are further divided into two parts after liquid air liquid nitrogen subcooler 18 is cooled to -183 DEG C or so；A part is through
Upper tower 6 is fractionated as the liquid-phase reflux for being fractionated upper tower 6, another part by being fractionated at the top of upper tower 6 to enter after the decompression of two throttle valves 15
Liquid nitrogen storage tank 9 is delivered to as liquid nitrogen product j after the decompression of third throttle valve 16.
Further, in above-mentioned air-separating technology, oxygen-enriched liquid air e is in being fractionated upper 6 distillation process of tower, except terrible
To outside the liquid oxygen product f and liquid argon product g of high-purity, the dirty nitrogen h of nitrogen content 80% or so is also obtained；Simultaneously in liquid nitrogen storage tank 9
It can generate and also contain certain cold energy in a certain amount of boil-off gas nitrogen j, dirty nitrogen h and boil-off gas nitrogen j, therefore by dirty nitrogen h and steaming
After the nitrogen j that gets angry is delivered to 18 re-heat of liquid air liquid nitrogen subcooler together, then enters back into main heat exchanger 4 and be used as the cold object of main heat exchanger 4
Hot logistics heat exchange in a part of stream, with main heat exchanger 4, is then discharged as waste nitrogen k.Using such technique, not only make
The cold energy contained in dirty nitrogen h and boil-off gas nitrogen j is fully used, and restores dirty nitrogen h and the temperature of boil-off gas nitrogen j to normal
Temperature, direct emission will not impact environment.
Further, in above-mentioned air-separating technology, the quantity of cyclic nitrogen compressor is at least 2；By being fractionated down
The cyclic nitrogen d extracted out at the top of tower 5 enters main heat exchanger 4, as the cold logistics of main heat exchanger 4, with the hot logistics in main heat exchanger 4
Enter liquefied natural gas heat exchanger 10 after heat exchange, enters First cyclic nitrogen pressure after exchanging heat with the high-pressure liquefaction natural gas m of outer confession
It is compressed in contracting machine, the cyclic nitrogen of compression is again introduced into liquefied natural gas heat exchanger 10, enters after exchanging heat with high-pressure liquefaction natural gas
It is compressed in next cyclic nitrogen compressor, repeats above-mentioned steps, until cyclic nitrogen d returns to main heat exchanger after being changed into liquid
4 are subcooled；Liquid circulation nitrogen n after supercooling is divided into two parts after the decompression of first throttle valve 14, a part with from fractionation
The cyclic nitrogen at lower 5 top of tower enters main heat exchanger 4 together, and as the cold logistics of main heat exchanger 4, another part, which returns, is fractionated lower tower
5 tops, which enter, is fractionated lower tower 5.It will be appreciated by persons skilled in the art that every recycle after a recycle compressor compresses
The pressure of nitrogen d correspondinglys increase, and the pressure of cyclic nitrogen d reaches 3.5MPa or more after afterbody cyclic nitrogen compressor compresses, i.e.,
The outlet pressure of afterbody cyclic nitrogen compressor reaches 3.5MPa or more.
Further, in above-mentioned air-separating technology, in fractionation tower 6 and being fractionated between lower tower 5 be provided with boil again it is cold
Condenser；Condenser is boiled again is located at the bottom for being fractionated upper tower 6.The part gas nitrogen for being fractionated lower 5 top of tower boils condenser by above-mentioned again
Liquefaction, condensation heat vaporization are fractionated the liquid oxygen of upper 6 tower bottom of tower.Since the boiling point of nitrogen at the same pressure is lower than oxygen, point
It evaporates lower tower 5 to run under a higher operating pressure, provides motive force as condenser is boiled again.
Further, in above-mentioned air-separating technology, raw air a is being cooled to saturation into main heat exchanger 4
Before, it is first purified through the compression of air compressor 1, the pre-cooling of air precooler 2 and air cleaning unit 3, to be purified air
B, purification air b obtain saturated air c after entering back into the cooling of main heat exchanger 4.Wherein, air compressor 1 compresses raw air a
To 0.5MPa~0.7MPa or so, raw air a is cooled to 25~35 DEG C by air precooler 2 in advance, and air cleaning unit 3 removes original
Expect water, carbon dioxide, hydrogen sulfide and hydrocarbons in air a etc. to pipeline and the harmful impurity of equipment.Air cleaning dress
It sets the 3 concrete type embodiment of the present invention to be not particularly limited, conventional technical means in the art.
Further, in above-mentioned air-separating technology, high-pressure liquefaction natural gas m is changed through liquefied natural gas heat exchanger 10
Still there is a part of cold energy in order to make its cold energy be fully used can be transported to refrigerant heat exchanger 11 after heat, and it is cold
Refrigerant in matchmaker's heat exchanger 11 exchanges heat, and provides cold energy for refrigerant therein.Refrigerant can be used in cooling air forecooler 2
Raw air a.Refrigerant can be the cooling mediums such as water, glycol water.
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..
According to the above, the cold logistics in main heat exchanger 4 includes two parts: a part is by taking out at the top of the upper tower 6 of fractionation
The boil-off gas nitrogen i evaporated in dirty nitrogen h and liquid nitrogen storage tank 9 out, another part are by being fractionated the circulation extracted out at the top of lower tower 5
The liquid circulation nitrogen that nitrogen and part are obtained through the supercooling of main heat exchanger 4.Hot logistics in main heat exchanger 4 equally includes two parts:
A part is purification air b, and another part is the liquid circulation nitrogen from liquefied natural gas heat exchanger 10.
Cold logistics in liquefied natural gas heat exchanger 10 be it is outer for high-pressure liquefaction natural gas m, hot logistics includes two parts: one
Branch is the cyclic nitrogen from main heat exchanger 4, and another part is the cyclic nitrogen after the pressurization of each cyclic nitrogen compressor.
Air-separating technology provided in an embodiment of the present invention is made further specifically below by specific test data
It is bright.
The air-separating technology of following example 1~3 can be realized by following air-seperation system, referring to Fig. 1 and be tied
Fig. 2 is closed, which includes: air compression pre-cooling unit, air cleaning member, air rectification cell and liquefaction day
So air cooling can recovery unit.Wherein,
It includes air compressor 1 and air precooler 2 that air, which compresses pre-cooling unit,；
Air cleaning member includes the air for removing the impurity such as water in air, carbon dioxide, hydrogen sulfide, hydrocarbons
Purification device 3；
Air rectification cell includes being fractionated tower 6, being fractionated lower tower 5, positioned at being fractionated upper tower 6 and be fractionated between lower tower 5 again
Boil condenser, liquid air liquid nitrogen subcooler 18 and liquid nitrogen storage tank 9；Wherein, tower 6 is internally provided with vertical clapboard 7 and water in fractionation
One end of flat partition board 8, horizontal baffle 8 is connect with the upper end of vertical clapboard 7, the other end of horizontal baffle 8 and the side for being fractionated upper tower 6
Wall connection.
Cold energy of liquefied natural gas recovery unit includes main heat exchanger 4, liquefied natural gas heat exchanger 10, the compression of first circulation nitrogen
Machine 12, second circulation nitrogen compressor 13 and refrigerant heat exchanger 11.Wherein, feeding air channel A1- is provided in main heat exchanger 4
A2, dirty nitrogen channel C 1-C2, gaseous recycle nitrogen channel B1-B2 and liquid circulation nitrogen channel D1-D2.Liquefied natural gas heat exchanger
Liquefied natural gas channel E1-E2, gaseous recycle nitrogen channel H1-H2, the first compressed nitrogen channel G1-G2 and second are provided in 10
Compressed nitrogen channel F1-F2.
Air compressor 1, air precooler 2, air cleaning unit 3, main heat exchanger 4 feeding air channel A1-A2 with
And it is sequentially connected positioned at the air intlet for being fractionated lower 5 bottom of tower.
Positioned at the oxygen-enriched liquid air outlet of lower 5 bottom of tower of fractionation, liquid air liquid nitrogen subcooler 18 and it is located at fractionation above 6 top of tower
Oxygen-enriched liquid air import be sequentially connected.
Two liquid nitrogen branches, one and 5 top of tower under being fractionated is arranged in liquid nitrogen exit at the top of the lower tower 5 of fractionation
Phegma entrance be connected, another is further divided into two branches after liquid air liquid nitrogen subcooler 18.One be located at fractionation on
The phegma entrance at 6 top of tower is connected, and another is connected with liquid nitrogen storage tank 9.
It is natural positioned at cyclic nitrogen outlet, the gaseous recycle nitrogen channel B1-B2 of main heat exchanger 4, the liquefaction for being fractionated lower 5 top of tower
The first pressure of the gaseous recycle nitrogen channel H1-H2 of gas heat exchanger 10, first circulation nitrogen compressor 12, liquefied natural gas heat exchanger 10
Contracting nitrogen channel G1-G2, second circulation nitrogen compressor 13, liquefied natural gas heat exchanger 10 the second compressed nitrogen channel F1-F2 and
The liquid circulation nitrogen channel D1-D2 of main heat exchanger 4 is sequentially connected；The liquid circulation nitrogen channel D1-D2 of main heat exchanger 4 exports setting
Two branches, one is connected with and positioned at being fractionated the cyclic nitrogen entrance at lower 5 top of tower, another with the gaseous state of main heat exchanger 4
Cyclic nitrogen channel is connected.
Nitrogen-free channel positioned at the outlet of dirty nitrogen, liquid air liquid nitrogen subcooler 18 and the main heat exchanger 4 that are fractionated at the top of upper tower 6 is suitable
It is secondary to be connected.
The liquefied natural gas channel 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 for being fractionated upper tower 6 in fractionation, and the liquid argon outlet of tower 6 is located in fractionation in fractionation
Lower section on the side wall that tower 6 is connect with horizontal baffle 8 and positioned at horizontal baffle 8.
The liquid circulation nitrogen channel outlet of main heat exchanger 4 is nearby provided with first throttle valve 14；Liquid air liquid nitrogen subcooler 18
It is provided with second throttle 15 on the pipeline being connected with the phegma import for being fractionated upper tower 6, on the pipeline being connected with liquid nitrogen storage tank 9
It is provided with third throttle valve 16, is provided with the 4th throttle valve 17 on the pipeline being connected with the oxygen-enriched liquid air import for being fractionated upper tower 6.
Embodiment 1
The present embodiment provides a kind of air-separating technology using high-pressure liquefaction natural gas cold energy, liquid used in the present embodiment
The pressure for changing natural gas 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 pressure is compressed to 0.6MPa by air compressor 1, drops in air precooler 2
Temperature removes the impurity such as water, carbon dioxide, hydrogen sulfide, hydrocarbons to 30 DEG C, subsequently into air cleaning unit 3, is purified
Air b.Air b is purified in main heat exchanger 4 with cyclic nitrogen and from the dirty nitrogen h for being fractionated upper 6 top of tower and from liquid nitrogen storage tank 9
The boil-off gas nitrogen i of middle evaporation exchanges heat, and enters after being cooled to -173.1 DEG C and is fractionated the lower lower tower rectifying of 5 bottom of tower participation, under fractionation
It carries out continuous caloic in tower 5 in column plate or filler with phegma to exchange and condensation evaporation, 5 bottom of tower obtains under fractionation
20t/h oxygen content is the oxygen-enriched liquid air e of 37.8% (wt), and 5 tower top of tower obtains purity up to the high-purity of 99.99% (wt) under fractionation
Gas nitrogen is spent, a part of gas nitrogen condenses to obtain liquid nitrogen by boiling the condensation portion of condenser again, and gained liquid nitrogen a part is as fractionation
Lower 5 top liquid-phase reflux of tower, remaining is extracted out by being fractionated at the top of lower tower 5；Remaining 14.5t/h gas nitrogen is as cyclic nitrogen by being fractionated down
Extraction is sent to 4 cooling supply of main heat exchanger and enters nitrogen cycle at the top of tower 5.
The cyclic nitrogen d extracted out at the top of lower tower 5 is fractionated through 4 re-heat of main heat exchanger to -22 DEG C, is changed subsequently into liquefied natural gas
Hot device 10 is cooled to -130 DEG C, is compressed to 1.5MPa using first circulation nitrogen compressor 12, is then returned to liquefied natural gas and changes
Hot device 10 is cooled to -130 DEG C again, is compressed to 3.5MPa using second circulation nitrogen compressor 13, returns to liquefied natural gas and changes
Hot device 10 is cooled to -150 DEG C of whole liquefaction and obtains liquid circulation nitrogen n, and liquid circulation nitrogen n, which returns to main heat exchanger 4 and crosses, is cooled to -172
DEG C, it is divided into two strands after the decompression of first throttle valve 14, one mixes return main heat exchange with the cyclic nitrogen d that lower tower 5 is extracted out is fractionated
Device 4 completes nitrogen cycle, and another burst of return is fractionated cooling capacity needed for offer air separation at the top of lower tower 5；It is extracted out at the top of tower 6 in fractionation
15.5t/h nitrogen content is the dirty nitrogen h of 80.61% (wt), through 10 re-heat of liquid air liquid nitrogen subcooler 18 and liquefied natural gas heat exchanger
It is discharged to 10 DEG C as waste nitrogen k.10 China and foreign countries of liquefied natural gas heat exchanger for flow are 37.4t/h, pressure 1MPa, temperature be-
150 DEG C of high-pressure liquefaction natural gas m is sent to refrigerant heat exchanger after 10 re-heat of liquefied natural gas heat exchanger extremely -125.5 DEG C
Cooling capacity needed for 11 offer refrigerants.
It is fractionated the liquid nitrogen extracted out at the top of lower tower 5, is crossed through liquid air liquid nitrogen subcooler 18 and is cooled to -183 DEG C, then extract 0.56t/ out
H, which enters to be fractionated at the top of upper tower 6 after the decompression of second throttle 15, is used as liquid nitrogen reflux, remaining is decompressed to through third throttle valve 16
Enter liquid nitrogen storage tank 9 as liquid nitrogen product j after 120kPa, the boil-off gas nitrogen i evaporated in liquid nitrogen storage tank 9 is mixed with dirt nitrogen h and is sent to
Liquid air liquid nitrogen subcooler 18 and 4 re-heat of main heat exchanger provide cooling capacity；The oxygen-enriched liquid air e of lower 5 bottom of tower is fractionated through liquid air liquid nitrogen mistake
Cooler 18, which is crossed to be cooled to -183 DEG C and enter after the decompression of the 4th throttle valve 17, is fractionated upper 6 top of tower as liquid phase feeding.
While boiling that gas nitrogen is condensed in condenser again, liquid oxygen is evaporated into gas oxygen as being fractionated upper 6 bottom gas phase of tower
Reflux, the liquid nitrogen in column plate or filler with oxygen-enriched liquid air e and as liquid-phase reflux carries out continuous heat and mass, in fractionation
6 tower bottom of tower extracts 4.8t/h purity out and is routed directly to liquid oxygen storage tank up to high-purity liquid oxygen product f of 99.88% (wt), liquid oxygen product f；
From upper 6 lateral line withdrawal function 45kg/h amount containing argon of tower is fractionated for the high-purity liquid argon product g of 99.5% (wt), smart ar system is sent into one
One-step refining；It is being fractionated the dirty nitrogen that extraction 15.5t/h nitrogen content is 80.61% (wt) at the top of upper tower 6, with the evaporation evaporated in storage tank
Cooling capacity is recycled by main heat exchanger 4 after entering the 18 part re-heat of liquid air liquid nitrogen subcooler after gas nitrogen i mixing and is emptied.
Embodiment 2
The present embodiment provides a kind of air-separating technology using high-pressure liquefaction natural gas cold energy, liquid used in the present embodiment
The pressure for changing natural gas 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 pressure is compressed to 0.6MPa by air compressor 1, drops in air precooler 2
Temperature removes the impurity such as water, carbon dioxide, hydrogen sulfide, hydrocarbons to 30 DEG C, subsequently into air cleaning unit 3, is purified
Air b.Air b is purified in main heat exchanger 4 with cyclic nitrogen and from the dirty nitrogen h for being fractionated upper 6 top of tower and from liquid nitrogen storage tank 9
The boil-off gas nitrogen i of middle evaporation exchanges heat, and enters after being cooled to -173.1 DEG C and is fractionated the lower lower tower rectifying of 5 bottom of tower participation, under fractionation
It carries out continuous caloic in tower 5 in column plate or filler with phegma to exchange and condensation evaporation, 5 bottom of tower obtains under fractionation
20t/h oxygen content is the oxygen-enriched liquid air e of 37.8% (wt), and 5 tower top of tower obtains purity up to the high-purity of 99.99% (wt) under fractionation
Gas nitrogen is spent, a part of gas nitrogen condenses to obtain liquid nitrogen by boiling the condensation portion of condenser again, and gained liquid nitrogen a part is as fractionation
Lower 5 top liquid-phase reflux of tower, remaining is extracted out by being fractionated at the top of lower tower 5；Remaining 14.5t/h gas nitrogen is as cyclic nitrogen by being fractionated down
Extraction is sent to 4 cooling supply of main heat exchanger and enters nitrogen cycle at the top of tower 5.
The cyclic nitrogen d extracted out at the top of lower tower 5 is fractionated through 4 re-heat of main heat exchanger to -22 DEG C, is changed subsequently into liquefied natural gas
Hot device 10 is cooled to -130 DEG C, is compressed to 2MPa using first circulation nitrogen compressor 12, is then returned to liquefied natural gas heat exchange
Device 10 is cooled to -130 DEG C again, is compressed to 5MPa using second circulation nitrogen compressor 13, returns to liquefaction heat exchange gas device
10, which are cooled to -150 DEG C of whole liquefaction, obtains liquid circulation nitrogen n, and liquid circulation nitrogen n, which returns to main heat exchanger 4 and crosses, is cooled to -173 DEG C, warp
It crosses after first throttle valve 14 depressurizes and is divided into two strands, mix return main heat exchanger 4 complete with the cyclic nitrogen d that lower tower 5 is extracted out is fractionated for one
At nitrogen cycle, another burst of return is fractionated cooling capacity needed for offer air separation at the top of lower tower 5；It is extracted out at the top of tower 6 in fractionation
15.5t/h nitrogen content is the dirty nitrogen h of 80.61% (wt), through 10 re-heat of liquid air liquid nitrogen subcooler 18 and liquefied natural gas heat exchanger
It is discharged to 13 DEG C as waste nitrogen k.10 China and foreign countries of liquefied natural gas heat exchanger for flow are 37.4t/h, pressure 8MPa, temperature be-
150 DEG C of high-pressure liquefaction natural gas m is sent to refrigerant heat exchanger 11 and mentions after 10 re-heat of liquefied natural gas heat exchanger extremely -82 DEG C
For cooling capacity needed for refrigerant.
It is fractionated the liquid nitrogen extracted out at the top of lower tower 5, is crossed through liquid air liquid nitrogen subcooler 18 and is cooled to -183 DEG C, then extract 0.56t/ out
H, which enters to be fractionated at the top of upper tower 6 after the decompression of second throttle 15, is used as liquid nitrogen reflux, remaining is decompressed to through third throttle valve 16
Enter liquid nitrogen storage tank 9 as liquid nitrogen product j after 120kPa, the boil-off gas nitrogen i evaporated in liquid nitrogen storage tank 9 is mixed with dirt nitrogen h and is sent to
Liquid air liquid nitrogen subcooler 18 and 4 re-heat of main heat exchanger provide cooling capacity；The oxygen-enriched liquid air e of lower 5 bottom of tower is fractionated through liquid air liquid nitrogen mistake
Cooler 18, which is crossed to be cooled to -183 DEG C and enter after the decompression of the 4th throttle valve 17, is fractionated upper 6 top of tower as liquid phase feeding.
While boiling that gas nitrogen is condensed in condenser again, liquid oxygen is evaporated into gas oxygen as being fractionated upper 6 bottom gas phase of tower
Reflux, the liquid nitrogen in column plate or filler with oxygen-enriched liquid air e and as liquid-phase reflux carries out continuous heat and mass, in fractionation
6 tower bottom of tower extracts 4.8t/h purity out and is routed directly to liquid oxygen storage tank up to high-purity liquid oxygen product f of 99.88% (wt), liquid oxygen product f；
From upper 6 lateral line withdrawal function 45kg/h amount containing argon of tower is fractionated for the high-purity liquid argon product g of 99.5% (wt), smart ar system is sent into one
One-step refining；It is being fractionated the dirty nitrogen that extraction 15.5t/h nitrogen content is 80.61% (wt) at the top of upper tower 6, with the evaporation evaporated in storage tank
Cooling capacity is recycled by main heat exchanger 4 after entering the 18 part re-heat of liquid air liquid nitrogen subcooler after gas nitrogen i mixing and is emptied.
Embodiment 3
The present embodiment provides a kind of air-separating technology using high-pressure liquefaction natural gas cold energy, liquid used in the present embodiment
The pressure for changing natural gas 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 pressure is compressed to 0.6MPa by air compressor 1, drops in air precooler 2
Temperature removes the impurity such as water, carbon dioxide, hydrogen sulfide, hydrocarbons to 30 DEG C, subsequently into air cleaning unit 3, is purified
Air b.Air b is purified in main heat exchanger 4 with cyclic nitrogen and from the dirty nitrogen h for being fractionated upper 6 top of tower and from liquid nitrogen storage tank 9
The boil-off gas nitrogen i of middle evaporation exchanges heat, and enters after being cooled to -173.1 DEG C and is fractionated the lower lower tower rectifying of 5 bottom of tower participation, under fractionation
It carries out continuous caloic in tower 5 in column plate or filler with phegma to exchange and condensation evaporation, 5 bottom of tower obtains under fractionation
20t/h oxygen content is the oxygen-enriched liquid air e of 37.8% (wt), and 5 tower top of tower obtains purity up to the high-purity of 99.99% (wt) under fractionation
Gas nitrogen is spent, a part of gas nitrogen condenses to obtain liquid nitrogen by boiling the condensation portion of condenser again, and gained liquid nitrogen a part is as fractionation
Lower 5 top liquid-phase reflux of tower, remaining is extracted out by being fractionated at the top of lower tower 5；Remaining 14.5t/h gas nitrogen is as cyclic nitrogen by being fractionated down
Extraction is sent to 4 cooling supply of main heat exchanger and enters nitrogen cycle at the top of tower 5.
The cyclic nitrogen d extracted out at the top of lower tower 5 is fractionated through 4 re-heat of main heat exchanger to -22 DEG C, is changed subsequently into liquefied natural gas
Hot device 10 is cooled to -130 DEG C, is compressed to 2MPa using first circulation nitrogen compressor 12, is then returned to liquefied natural gas heat exchange
Device 10 is cooled to -130 DEG C again, is compressed to 4MPa using second circulation nitrogen compressor 13, returns to liquefaction heat exchange gas device
10, which are cooled to -150 DEG C of whole liquefaction, obtains liquid circulation nitrogen n, and liquid circulation nitrogen n, which returns to main heat exchanger 4 and crosses, is cooled to -172 DEG C, warp
It crosses after first throttle valve 14 depressurizes and is divided into two strands, mix return main heat exchanger 4 complete with the cyclic nitrogen d that lower tower 5 is extracted out is fractionated for one
At nitrogen cycle, another burst of return is fractionated cooling capacity needed for offer air separation at the top of lower tower 5；It is extracted out at the top of tower 6 in fractionation
15.5t/h nitrogen content is the dirty nitrogen h of 80.61% (wt), through 10 re-heat of liquid air liquid nitrogen subcooler 18 and liquefied natural gas heat exchanger
It is discharged to 12 DEG C as waste nitrogen k.10 China and foreign countries of liquefied natural gas heat exchanger for flow are 37.4t/h, pressure 5MPa, temperature be-
150 DEG C of high-pressure liquefaction natural gas m is sent to refrigerant heat exchanger 11 and mentions after 10 re-heat of liquefied natural gas heat exchanger extremely -90 DEG C
For cooling capacity needed for refrigerant.
It is fractionated the liquid nitrogen extracted out at the top of lower tower 5, is crossed through liquid air liquid nitrogen subcooler 18 and is cooled to -183 DEG C, then extract 0.56t/ out
H, which enters to be fractionated at the top of upper tower 6 after the decompression of second throttle 15, is used as liquid nitrogen reflux, remaining is decompressed to through third throttle valve 16
Enter liquid nitrogen storage tank 9 as liquid nitrogen product j after 120kPa, the boil-off gas nitrogen i evaporated in liquid nitrogen storage tank 9 is mixed with dirt nitrogen h and is sent to
Liquid air liquid nitrogen subcooler 18 and 4 re-heat of main heat exchanger provide cooling capacity；The oxygen-enriched liquid air e of lower 5 bottom of tower is fractionated through liquid air liquid nitrogen mistake
Cooler 18, which is crossed to be cooled to -183 DEG C and enter after the decompression of the 4th throttle valve 17, is fractionated upper 6 top of tower as liquid phase feeding.
While boiling that gas nitrogen is condensed in condenser again, liquid oxygen is evaporated into gas oxygen as being fractionated upper 6 bottom gas phase of tower
Reflux, the liquid nitrogen in column plate or filler with oxygen-enriched liquid air e and as liquid-phase reflux carries out continuous heat and mass, in fractionation
6 tower bottom of tower extracts 4.8t/h purity out and is routed directly to liquid oxygen storage tank up to high-purity liquid oxygen product f of 99.88% (wt), liquid oxygen product f；
From upper 6 lateral line withdrawal function 45kg/h amount containing argon of tower is fractionated for the high-purity liquid argon product g of 99.5% (wt), smart ar system is sent into one
One-step refining；It is being fractionated the dirty nitrogen that upper top of tower extraction 15.5t/h nitrogen content is 80.61% (wt), with the evaporation evaporated in storage tank
Cooling capacity is recycled by main heat exchanger 4 after entering the 18 part re-heat of liquid air liquid nitrogen subcooler after gas nitrogen i mixing and is emptied.
To sum up, in air-separating technology provided in an embodiment of the present invention, on the one hand will be fractionated upper Deethanizer design is that next door is tower-shaped
On the other hand formula optimizes cold recovery process, significantly reduce energy consumption and equipment investment.The embodiment of the present invention
The air-separating technology stable operation of offer, highly-safe, liquid oxygen, liquid nitrogen, the liquid argon of energy mass production high-purity are energy-saving
Significant effect, has high economic benefit and environmental benefit.
The above is merely for convenience of it will be understood by those skilled in the art that technical solution of the present invention, not to limit
The present invention.All within the spirits and principles of the present invention, any modification, equivalent replacement, improvement and so on should be included in this
Within the protection scope of invention.
Claims (9)
1. a kind of air-separating technology using high-pressure liquefaction natural gas cold energy, the pressure of the high-pressure liquefaction natural gas is 1MPa
~10MPa；It is characterized in that, the air-separating technology includes:
Saturated air from main heat exchanger (4) enters tower (5) progress rectifying under the fractionation by being fractionated lower tower (5) bottom, obtains
To gas nitrogen and oxygen-enriched liquid air；
The oxygen-enriched liquid air enters tower (6) progress rectifying in the fractionation by being fractionated upper tower (6) top, obtains liquid argon product and liquid
Oxygen product, the liquid argon product is from tower (6) lateral line withdrawal function in the fractionation, and the liquid oxygen product is from tower (6) bottom in the fractionation
Portion's extraction；
A part of gas nitrogen condenses to obtain liquid by being fractionated to extract out at the top of lower tower (5) by the condenser that boils again for being fractionated upper tower (6) bottom
Nitrogen, as liquid nitrogen product and the liquid-phase reflux of fractionation upper tower (6) and fractionation lower tower (5) after the liquid nitrogen extraction；Another part
The extraction at the top of tower (5) under the fractionation of gas nitrogen is used as cyclic nitrogen, and the cyclic nitrogen enters after the main heat exchanger (4) re-heat
Liquefied natural gas heat exchanger (10) is cooling, and the liquefied natural gas heat exchanger (10) is returned after cyclic nitrogen compressor compresses into one
Step cooling, then returned after the main heat exchanger (4) supercooling and be used as liquid-phase reflux under the fractionation at the top of tower (5)；The liquefaction
Cold logistics in heat exchange gas device (10) includes the high-pressure liquefaction natural gas；
Wherein, tower (6) is internally provided with vertical clapboard (7) and horizontal baffle (8) in the fractionation, the horizontal baffle (8)
One end is connect with the upper end of the vertical clapboard (7), the side of tower (6) on the other end of the horizontal baffle (8) and the fractionation
Wall connection；The withdrawn position of the liquid argon product is located on the side wall that tower (6) is connect with the horizontal baffle (8) in the fractionation
And it is located at the lower section of the horizontal baffle (8).
2. air-separating technology according to claim 1, which is characterized in that the oxygen-enriched liquid air is by tower under the fractionation
(5) tower (6) in the fractionation is entered back into after the extraction of bottom after liquid air liquid nitrogen subcooler (18) are cooling and carries out rectifying.
3. air-separating technology according to claim 2, which is characterized in that it is divided into two parts after liquid nitrogen extraction, one
Divide by returning to liquid-phase reflux of the tower (5) as tower (5) under the fractionation under the fractionation at the top of tower (5) under the fractionation, it is another
Part is further divided into two parts after the liquid air liquid nitrogen subcooler (18) is cooling；A part by the fractionation at the top of tower (6) into
Enter liquid-phase reflux of the tower (6) as tower (6) in the fractionation, another part in the fractionation and is delivered to liquid nitrogen as liquid nitrogen product
Storage tank (9).
4. air-separating technology according to claim 3, which is characterized in that in the fractionation in tower (6) distillation process also
Dirty nitrogen is obtained, the dirt nitrogen is together with the boil-off gas nitrogen from the liquid nitrogen storage tank (9) through the liquid air liquid nitrogen subcooler (18)
Enter the main heat exchanger (4) after re-heat, as the heat in the cold logistics of the main heat exchanger (4), with the main heat exchanger (4)
It is discharged after logistics heat exchange.
5. air-separating technology according to claim 1, which is characterized in that the quantity of the cyclic nitrogen compressor is at least
2；
The main heat exchanger (4) are entered by the cyclic nitrogen extracted out at the top of tower (5) under the fractionation, as the main heat exchanger (4)
Cold logistics, and enter the liquefied natural gas heat exchanger (10) after the hot logistics heat exchange in the main heat exchanger (4), and it is described
Enter in First cyclic nitrogen compressor after high-pressure liquefaction natural gas heat exchange and compress, the cyclic nitrogen of compression is again introduced into the liquefaction
Enter in next cyclic nitrogen compressor after heat exchange gas device (10), with high-pressure liquefaction natural gas heat exchange and compress, repeats
Above-mentioned steps are carried out, the main heat exchanger (4) is returned after the cyclic nitrogen is changed into liquid and is subcooled；
Cyclic nitrogen after supercooling is divided into two parts, and a part enters together with the cyclic nitrogen at the top of tower (5) under the fractionation
The main heat exchanger (4), as the cold logistics of the main heat exchanger (4), another part at the top of tower (5) under the fractionation by entering
Tower (5) under the fractionation.
6. air-separating technology according to claim 1, which is characterized in that the air-separating technology further include:
Raw air is compressed through air compressor (1), is obtained after air precooler (2) pre-cooling and air cleaning unit (3) purification
To purification air, the purification air obtains the saturated air after entering the main heat exchanger (4) cooling.
7. air-separating technology according to claim 1, which is characterized in that the high-pressure liquefaction natural gas is through the liquefaction
The refrigerant entered in refrigerant heat exchanger (11), with the refrigerant heat exchanger (11) after heat exchange gas device (10) heat exchange is changed
Heat；The refrigerant is used to cool down the raw air in the air precooler (2).
8. air-separating technology according to claim 1, which is characterized in that the flow of the high-pressure liquefaction natural gas is 35
~40t/h.
9. air-separating technology according to claim 1, which is characterized in that the outlet pressure of the cyclic nitrogen compressor is
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
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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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