CN106052303A - Efficient expansion refrigeration methane-rich gas liquefaction method and device - Google Patents

Efficient expansion refrigeration methane-rich gas liquefaction method and device Download PDF

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Publication number
CN106052303A
CN106052303A CN201610395717.XA CN201610395717A CN106052303A CN 106052303 A CN106052303 A CN 106052303A CN 201610395717 A CN201610395717 A CN 201610395717A CN 106052303 A CN106052303 A CN 106052303A
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gas
heat exchanger
methane
high methane
heat exchange
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张惊涛
母斌
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Chengdu Sepmem Sci & Tech Co Ltd
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Chengdu Sepmem Sci & Tech Co Ltd
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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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
    • F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
    • F25B15/06—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being water vapour evaporated from a salt solution, e.g. lithium bromide
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0082—Methane
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0208—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
    • 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/061—Natural gas or substitute natural gas
    • F25J3/0615—Liquefied natural gas
    • 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general

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  • Engineering & Computer Science (AREA)
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  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention discloses an efficient expansion refrigeration methane-rich gas liquefaction method and device. The method includes the steps of methane-rich gas liquefaction and circulation refrigeration. Specifically, methane-rich gas and part of pre-heated gas are mixed and then enter a heat exchanger so as to be cooled, a cooled material is subjected to heavy hydrocarbon removal, and then an obtained material is sequentially subjected to throttling through throttling valves and separation through gas-liquid separators to form liquefied methane-rich gas and low-temperature flashed vapor; noncondensable gas in the liquefied methane-rich gas is guided out to serve as fuel gas and provide a motive power source for a whole system; and the low-temperature flashed vapor is subjected to heat exchange through the heat exchanger to obtain the pre-heated gas, the pre-heated gas is pressurized and then divided into two materials, one material is subjected to heat exchange through the heat exchanger and then delivered into an expansion machine so as to obtain an expansion material, and the expansion material is subjected to heat exchange through the heat exchanger and then mixed with the pre-heated gas so as to enter the next circulation. By means of the efficient expansion refrigeration methane-rich gas liquefaction method and device, the material utilization rate can be effectively increased, the energy consumption can be effectively reduced, and the production cost can be effectively reduced. The efficient expansion refrigeration methane-rich gas liquefaction method and device have the advantages of being low in equipment investment, small in methane loss, good in nitrogen separation effect, capable of recycling expansion work and the like.

Description

A kind of method and device of efficient expansion refrigeration high methane gas liquefaction
Technical field
The present invention relates to high methane gas condensation separation field, the side of a kind of efficient expansion refrigeration high methane gas liquefaction Method and device.The present invention can improve the utilization rate of material the most further, energy-saving and cost-reducing, has preferable effect, is worth big Scale promotion and application.
Background technology
In dense-air refrigeration cycle, working medium passes through compressor isentropic Compression, cools down through aftercooler, then at turbine expansion Constant entropy adiabatic expansion externally doing work in machine, thus obtain low-temperature airflow, produce cold.In recent years, swollen along with low temperature turbine Swollen machine (especially high-speed gas bearing turbo-expander) and the development of high-efficiency compact heat exchanger, the effect of turbine dense-air refrigeration cycle Rate is significantly improved, and can obtain the lowest cryogenic temperature and the widest refrigerating capacity scope, has high reliability.Therefore, In recent decades, inverse Brayton refrigeration cycle has obtained the biggest development, and range of application is more and more wider.Based on dense-air refrigeration cycle Advantage, its swell refrigeration circulate in be widely used.
In gas deliquescence process, swell refrigeration circulation is main uses nitrogen swell refrigeration, nitrogen-methane blended to expand system Cold and three kinds of forms of natural gas direc expansion refrigeration.Natural gas direc expansion refrigeration is to directly utilize high-pressure natural gas at decompressor Middle adiabatic expansion and make natural gas liquefaction, make full use of the pressure energy of natural gas itself, consume electric energy little, the equipment that saves is thrown Money.Use the gas-bearing expansion turbine that volume is little, lightweight, efficiency is high, run reliably and with long-term, system effect can be effectively improved Rate, in can be used for frequent operation and requiring the peak regulation type device of rapid starting/stopping.Develop into the liquefaction system of multiple expansion, and And expansion refrigerator also reaches its maturity, there is long-life, high reliability, low vibration, the feature such as lightweight, in natural gas liquefaction side There is good development prospect in face.Under the requirement that liquefaction tolerance strengthens increasingly, this circulation has bigger advantage: have equipment tight Gather, the advantage such as small investment, flexible adjustment, reliable operation.
Existing patent GB 2522421A discloses production process (the LNG production of a kind of liquefied natural gas Process), it has the drawback that
(1) heavy hydrocarbon separates difficulty；
(2) complex operation, equipment investment is higher；
(3) methane losses is big, and nitrogen separation effect is bad, and in liquefied natural gas, nitrogen content is higher；
(4) expansion work loses, and energy consumption is higher.
(5) reclaiming the fixed gas produced in use liquefaction process completely, package unit methane zero loses.
The disadvantages mentioned above existed based on GB 2522421A, applicant proposed the liquefaction of a kind of swell refrigeration high methane gas Method and device.On the Research foundation of early stage, applicant is studied further, to improve the utilization rate of material, reduces Energy consumption, has finally given the technical scheme of the application.
Summary of the invention
The goal of the invention of the present invention is: the production method (GB 2522421A) for existing liquefied natural gas exists weight Hydrocarbon separates difficulty, complex operation, and equipment investment is higher, and methane losses is big, and expansion work loses, the problem that energy consumption is more high, carries Method and device for the refrigeration high methane gas liquefaction of a kind of efficient expansion.The present invention has that flow process is simple, flexible operation, equipment are thrown Provide low, methane losses is little, nitrogen separation is respond well and reclaims the advantage such as expansion work, and energy consumption is low, liquefying high methane gas nitrogen content Low strong with adaptability to raw material.Meanwhile, the present invention can improve the utilization rate of material further, reduces energy consumption, reduces production cost, There is remarkable progress.
To achieve these goals, the present invention adopts the following technical scheme that
The method of a kind of efficient expansion refrigeration high methane gas liquefaction, comprises the steps:
(1) high methane gas liquefaction
After methane rich unstripped gas steam pre-with part mixes, it is cooled to-10 ~-90 DEG C through heat exchanger, enters back into heavy hydrocarbon separator and take off Heavy hydrocarbon, obtains low temperature dry gas, and low temperature dry gas is after heat exchanger cools down, more successively after reducing pressure by regulating flow, gas-liquid separation, respectively obtains Liquefying high methane gas, low-flash gas, liquefying high methane gas is as product collection, and low-flash gas, after heat exchanger heat exchange, enters Row supercharging, enters next one circulation；
If methane rich unstripped gas is without heavy hydrocarbon, then after methane rich unstripped gas steam pre-with part mixes, directly cool down through heat exchanger, then Successively after reducing pressure by regulating flow, gas-liquid separation, after separation, respectively obtain liquefying high methane gas, low-flash gas, liquefying high methane gas Collecting as product, low-flash gas, after heat exchanger heat exchange, carries out supercharging, enters next one circulation；
(2) open loop refrigeration
Low-flash gas, after heat exchanger heat exchange, obtains pre-steam, and pre-steam is carried out supercharging, is classified as first strand after supercharging Material, two strands of materials of second strand of material, first strand of material is sent in decompressor after heat exchanger heat exchange, or first strand of material is not It is sent directly in decompressor through heat exchanger heat exchange, obtains expanding material, expand material and mix with pre-steam after heat exchanger heat exchange Closing, enter next one circulation, second strand of material is steam pre-with the part that methane rich unstripped gas mixes in described step 1；
Or low-flash gas is after heat exchanger heat exchange, obtain pre-steam, pre-steam is carried out supercharging, after supercharging, be classified as first Stock material, two strands of materials of second strand of material, first strand of material is sent directly in decompressor, obtains expanding material, expands material warp Mixing with pre-steam after heat exchanger heat exchange, enter next one circulation, second strand of material is in described step 1 and methane rich raw material The pre-steam of part of gas mixing；
Another kind of replacement method is provided, comprises the steps:
(1) high methane gas liquefaction:
Low-flash gas, after heat exchanger heat exchange, obtains pre-steam, and pre-steam carries out supercharging, and by methane rich unstripped gas with pre- Steam mixes, and the material of mixing is cooled to-10 ~-90 DEG C through heat exchanger, enters back into heavy hydrocarbon separator and takes off heavy hydrocarbon, obtains low temperature and does Gas, low temperature dry gas after heat exchanger cools down, through reducing pressure by regulating flow, then carries out gas-liquid separation, respectively obtains liquefaction and be the richest in after separation again Alkane gas, low-flash gas, liquefying high methane gas is as product collection, and low-flash gas, after heat exchanger heat exchange, carries out supercharging, enters Enter next circulation；
If methane rich unstripped gas is without heavy hydrocarbon, then after methane rich unstripped gas steam pre-with part mixes, directly cool down through heat exchanger, then After reducing pressure by regulating flow, carry out gas-liquid separation, after separation, respectively obtain liquefying high methane gas, low-flash gas, liquefying high methane gas Collecting as product, low-flash gas, after heat exchanger heat exchange, carries out supercharging, enters next one circulation；
(2) closed-loop refrigeration
After cooling medium is intensified, then through heat exchanger heat exchange, enter in decompressor, or cooling medium intensified after without heat exchange Device heat exchange and be sent directly in decompressor, obtain expand material, expand material again after heat exchanger heat exchange, return supercharging, enter Next circulation；
In described step (1), the fixed gas in liquefying high methane gas is drawn, using the fixed gas of extraction as fuel gas, for whole Individual system provides power resources；
In described step (1), the pressure of methane rich unstripped gas is 1MPaG ~ 20MPaG, temperature is-30 ~ 60 DEG C, or described in be the richest in Alkane unstripped gas is the self-evaporating steam of LNG storage tank.
The pre-steam of described part mixes with methane rich unstripped gas, forms two strands of materials and enters heat exchanger；Or pre-steam is with rich Methane feed gas is thoroughly mixed, and is further divided into two strands of entrance heat exchangers.
In described step (1), low temperature dry gas is after heat exchanger cools down, then carries out reducing pressure by regulating flow, and the progression of throttling is one-level Throttling, two-step throttle, three grades of throttlings or level Four throttling.
Also include precooling step: outside cooling be connected with heat exchanger, by other portions in outside cooling heat exchanger Part carries out pre-cooling.
The typical cryogen that described outside cooling uses is the one in propylene, propane, ammonia, freon, water, BOG, lithium bromide Or it is multiple.
In step (2), according to the pressure and temperature of methane rich unstripped gas, mix with pre-steam in the suitable position of system.
In described step (1), low temperature dry gas is after heat exchanger cools down, then through reducing pressure by regulating flow, divides subsequently into the first gas-liquid Carrying out gas-liquid separation from device, respectively obtain the first liquid phase thing, the first gas gas-phase objects after separation, this first liquid phase thing is liquefaction and is the richest in Alkane gas, this first gas gas-phase objects is low-flash gas.
In described step (1), the first liquid phase thing, after reducing pressure by regulating flow, enters the second gas-liquid separator and carries out gas-liquid separation, Respectively obtaining second liquid phase thing, the second gas gas-phase objects after separation, this second liquid phase thing is liquefying high methane gas；Second gas gas-phase objects warp After heat exchanger heat exchange, draw as fixed gas, using the fixed gas of extraction as fuel gas, provide power resources for whole system.
For the device of the method for aforementioned efficient expansion refrigeration high methane gas liquefaction, including high methane gas liquefaction system, open Formula cycle refrigeration system；
Described high methane gas liquefaction system includes for carrying the feedstock supply unit of methane rich unstripped gas, heat exchanger, gas-liquid are divided From device, described feedstock supply unit, heat exchanger, gas-liquid separator are sequentially connected by pipeline；
Described open loop refrigeration system includes gas-liquid separator, heat exchanger, compressor, decompressor, described gas-liquid separator, changes Hot device, compressor, decompressor constitute open-cycle system by pipeline；
There is provided another kind of alternative, including high methane gas liquefaction system, closed-loop refrigeration system；
Described methane gas liquefaction system includes feedstock supply unit, heat exchanger, gas-liquid separator, compressor, described raw material supply Device, heat exchanger, gas-liquid separator, compressor are sequentially connected by pipeline；
Described closed-loop refrigeration system includes that compressor, heat exchanger, decompressor, described compressor, heat exchanger, decompressor pass through Pipeline constitutes closed circulation system.
Described high methane gas liquefaction system includes for carrying the feedstock supply unit of methane rich unstripped gas, heat exchanger, weight Hydrocarbon separator, gas-liquid separator, described feedstock supply unit, heat exchanger, heavy hydrocarbon separator, gas-liquid separator are by pipeline successively It is connected.
In the present invention, the most liquescent gas containing methane includes: nitrogen, hydrogen, argon, oxygen or helium etc., this Bright by fixed gas extraction, and using the fixed gas of extraction as fuel gas, provide power resources for whole system.Use which, Material can be made to be fully used, there is preferable energy conservation and consumption reduction effects.
Improvement based on preceding method, the recycle gas compressor optional structure in the present invention is simply compact, easy to into sled Screw compressor, and only need single stage supercharging.Further, the method is used, it is possible to make appliance arrangement quantity reduce, reduce low Temperature size of heat exchanger, and cryogen side is without liquid form, the skid of the most middle-size and small-size liquefying plant, modularity, can move There is further scope of applicability in dynamic formula liquefying plant field.
Further, the first liquid phase thing, after reducing pressure by regulating flow, carries out secondary gas-liquid separation, the second gas gas-phase objects energy of isolated The enough fuel all doing gas electricity generator or gas driven, it is possible to enter back into fuel gas system after first doing pretreatment regeneration gas, The produced energy be enough to drive the main dynamics equipment of package unit.
The outside cooling also including matching with heat exchanger, the coolant that outside cooling uses be typically propylene, propane, One or more in ammonia, freon, water, BOG, lithium bromide.
The present invention has that regulating measure is abundant, flow process simple, flexible operation, adaptability to raw material are strong, equipment investment is low, methane Losing little, nitrogen separation is respond well, low power consumption and other advantages, has preferable application prospect.
In sum, owing to have employed technique scheme, the invention has the beneficial effects as follows:
(1), in the present invention, high methane gas is pre-cooled, expand after cool down again, hinge structure, there is more preferable refrigeration；
(2) in the present invention, using choke valve decompression, though efficiency is lower slightly, but cold is suitable, operates the easiest, and equipment investment is more Little；
(3) using in the present invention and throttle step by step, pressure drops at different levels are little so that the present invention has that energy consumption is lower, methane losses is little, nitrogen The advantage that separation is high；
(4) present invention can effectively reduce number of devices, reduces cryogenic heat exchanger size, and cryogen side is without liquid form, more It is prone to the skid of middle-size and small-size liquefying plant, modularity, has further scope of applicability in packaged type liquefying plant field；
(5) the second gas gas-phase objects in the present invention can act as the fuel of system, it is possible to enters back into combustion after first doing pretreatment regeneration gas Material gas system, the produced energy be enough to drive the main dynamics equipment of package unit；
(6) flexible operation of the present invention, methane losses is little, and energy consumption is low, especially at remote extreme rings such as edge gas well, offshore platforms High methane gas liquefaction in border is reclaimed has preferable application prospect.
Accompanying drawing explanation
Examples of the present invention will be described by way of reference to the accompanying drawings, wherein:
Fig. 1 is the principle schematic of embodiment 1.
In Fig. 1, T1 is pretreatment system, and P1 is decompressor, and C1 is recycle gas compressor, and E1 is cooler, and E2 is heat exchange Device, V1 is the first gas-liquid separator, and V2 is heavy hydrocarbon separator, and V3 is the second gas-liquid separator.
Fig. 2 is the principle schematic of embodiment 2.
In Fig. 2, T1 is pretreatment system, and P1 is circulating air decompressor, and C1 is recycle gas compressor, and C2 is methane rich circulation Air compressor, E1 is methane rich recycle gas cooler, and E2 is heat exchanger, and E3 is recycle gas cooler, and V1 is the first gas-liquid separation Device, V2 is heavy hydrocarbon separator, and V3 is the second gas-liquid separator.
Detailed description of the invention
All features disclosed in this specification, or disclosed all methods or during step, except mutually exclusive Feature and/or step beyond, all can combine by any way.
Any feature disclosed in this specification, unless specifically stated otherwise, all can by other equivalence or there is similar purpose Alternative features is replaced.I.e., unless specifically stated otherwise, an example during each feature is a series of equivalence or similar characteristics ?.
Embodiment 1
The schematic flow sheet of the present embodiment is as it is shown in figure 1, this flow process comprises pretreatment system T1, decompressor P1, cycle compressor Machine C1, cooler E1, heat exchanger E2, heavy hydrocarbon separator V2, the first gas-liquid separator V1, the second gas-liquid separator V3 etc., each portion High methane gas liquefaction system and open loop refrigeration system is constituted by pipeline between part.
The processing step of the present embodiment is as follows.
(1) high methane gas liquefaction:
After unprocessed preprocessed system T1 of methane rich unstripped gas 1 processes, obtain methane rich unstripped gas 2.Methane rich unstripped gas 2 Steam 17(pre-with part hereinafter mentions) mix after, obtain material 3.After material 3 enters heat exchanger E2 cooling, obtain material 4. Material 4 goes out heat exchanger E2, enters heavy hydrocarbon separator V2 and takes off heavy hydrocarbon, and heavy hydrocarbon is drawn by material 6, the low temperature dry gas material after de-heavy hydrocarbon 5 enter back into heat exchanger E2 cooling, obtain material 7.Material 7 is drawn heat exchanger E2, after one-level choke valve I throttles, obtains thing Material 8.Material 8 enters the first gas-liquid separator V1 and carries out gas-liquid separation, through the liquid phase thing of the first gas-liquid separator V1 isolated Material 10 proceeds two-step throttle；Heat exchanger E2 re-heat is entered through the low-flash gas 9 of the first gas-liquid separator V1 isolated After, draw pre-steam 11.Pre-steam 11 is hereinafter mentioned with material 12() mix after, obtain material 13.Material 13 enters circulation In air compressor C1 after supercharging, obtain material 14, after material 14 cooled device E1 cooling, obtain material 15.Material 15 derivated Material 16,17 two strands of materials of material.Material 17 mixes with methane rich unstripped gas 2, obtains material 3, enters next one circulation.
Liquid phase material 10, after two-step throttle valve II throttles, enters the second gas-liquid separator V3 and carries out gas-liquid separation, separates After respectively obtain second liquid phase thing the 19, second gas gas-phase objects 20.Second liquid phase thing 19 is collected, obtains liquefying high methane gas and (i.e. produce Product gas).Second gas gas-phase objects 20, after heat exchanger E2 re-heat, obtains fixed gas 21, using the fixed gas 21 drawn as fuel gas, for Whole system provides power resources.
(2) open loop refrigeration
Material 16, after heat exchanger E2 cools down, obtains material 22.Material 22 enters in decompressor P1, after expansion, draws material 23. Or material 16 is without heat exchanger E2 heat exchange, and is sent directly in decompressor P1 expansion, draw material 23.Material 23 enters heat exchange Device E2 provides cold, obtains material 12 after heat exchange.After material 28 mixes with pre-steam 11, enter next one circulation.
In the present embodiment, the temperature of methane rich unstripped gas 2 is 40 DEG C, and pressure is 4000kPaA, and flow is 1250Nm3/h； Being difficult to liquefied gas (i.e. material 21) is 37 DEG C, and pressure is 150kPaA, and flow is 200Nm3/h；The temperature of product LNG is-158 DEG C, pressure is 150kPaA, and flow is 1050Nm3/h, is absolute pressure.
Relative to prior art, the present invention can save the energy of 5%-10%, simplifies technological process, reduces equipment investment 20%, there is preferable effect.
Embodiment 2
The schematic flow sheet of the present embodiment is as in figure 2 it is shown, this flow process comprises pretreatment system T1, circulating air decompressor P1, circulation Air compressor C1, methane rich recycle gas compressor C2, methane rich recycle gas cooler E1, heat exchanger E2, recycle gas cooler E3, First gas-liquid separator V1, heavy hydrocarbon separator V2, the second gas-liquid separator V3, one-level choke valve I, two-step throttle valve II etc., respectively High methane gas liquefaction system and closed-loop refrigeration system is constituted by pipeline between parts.
The job step of this device is as follows:
(1) high methane gas liquefaction:
After unprocessed preprocessed system T1 of methane rich unstripped gas 1 processes, obtain methane rich unstripped gas 2.Methane rich unstripped gas 2 Hereinafter mention with material 13() mix after obtain material 3.Material 3 is gone out heat exchanger E2 by material 4 after entering heat exchanger E2 cooling, Entering heavy hydrocarbon separator V2 and take off heavy hydrocarbon, heavy hydrocarbon is drawn by material 6；Low temperature dry gas material 5 after de-heavy hydrocarbon enters back into heat exchanger E2 Cooling, obtains material 7.Material 7, after one-level choke valve I throttles, obtains material 8.Material 8 enters the first gas-liquid separator V1 and enters Row gas-liquid separation, proceeds two-step throttle through the liquid phase 10 of the first gas-liquid separator V1 isolated；Through the first gas-liquid separation After the low-flash gas 9 of device V1 isolated enters heat exchanger E2 re-heat, draw pre-steam 11.Pre-steam 11 circulates through methane rich After air compressor C2 supercharging, obtain material 12.Material 12 through methane rich recycle gas cooler E1 is cold go after, obtain material 13.Thing Material 13 mixes with methane rich unstripped gas 2, obtains material 3, enters next one circulation.
The first isolated liquid phase of gas-liquid separator V1 10, after two-step throttle valve II throttles, obtains material 14.Material 14 Enter the second gas-liquid separator V3 and carry out gas-liquid separation, after separation, respectively obtain second liquid phase thing the 15, second gas gas-phase objects 16.By Two liquid phase things 15 are collected, and obtain liquefying high methane gas (i.e. product gas).Second gas gas-phase objects 16, after heat exchanger E2 re-heat, obtains not Solidifying gas 17, using the fixed gas 17 of extraction as fuel gas, provides power resources for whole system.
(2) closed-loop refrigeration:
High methane gas, after recycle gas compressor C1 supercharging, draws material 18.After material 18 cooled device E3 cooling, obtain material 19.Material 19 enters heat exchanger E2 and cools down further, draws material 20.Material 20, after circulating air decompressor P1 expands, obtains Material 21.Or material 19 is sent directly in circulating air decompressor P1 expansion without heat exchanger E2 heat exchange, draw material 21.Thing Material 21 entrance heat exchanger E2 provide cold for heat exchanger, and draw material 22 and enter recycle gas compressor C1, starts the next one and follows Ring.
Relative to prior art, the present invention can save the energy of 1%-5%, simplifies technological process, reduces equipment investment 20%, there is preferable effect.
The invention is not limited in aforesaid detailed description of the invention.The present invention expands to any disclose in this manual New feature or any new combination, and the arbitrary new method that discloses or the step of process or any new combination.

Claims (10)

1. the method for an efficient expansion refrigeration high methane gas liquefaction, it is characterised in that comprise the steps:
(1) high methane gas liquefaction
After methane rich unstripped gas steam pre-with part mixes, it is cooled to-10 ~-90 DEG C through heat exchanger, enters back into heavy hydrocarbon separator and take off Heavy hydrocarbon, obtains low temperature dry gas, and low temperature dry gas is after heat exchanger cools down, more successively after reducing pressure by regulating flow, gas-liquid separation, respectively obtains Liquefying high methane gas, low-flash gas, liquefying high methane gas is as product collection, and low-flash gas, after heat exchanger heat exchange, enters Row supercharging, enters next one circulation；
If methane rich unstripped gas is without heavy hydrocarbon, then after methane rich unstripped gas steam pre-with part mixes, directly cool down through heat exchanger, then Successively after reducing pressure by regulating flow, gas-liquid separation, after separation, respectively obtain liquefying high methane gas, low-flash gas, liquefying high methane gas Collecting as product, low-flash gas, after heat exchanger heat exchange, carries out supercharging, enters next one circulation；
(2) open loop refrigeration
Low-flash gas, after heat exchanger heat exchange, obtains pre-steam, and pre-steam is carried out supercharging, is classified as first strand after supercharging Material, two strands of materials of second strand of material, first strand of material is sent in decompressor after heat exchanger heat exchange, or first strand of material is not It is sent directly in decompressor through heat exchanger heat exchange, obtains expanding material, expand material and mix with pre-steam after heat exchanger heat exchange Close, enter next one circulation；
Another kind of replacement method is provided, comprises the steps:
(1) high methane gas liquefaction:
Low-flash gas, after heat exchanger heat exchange, obtains pre-steam, and pre-steam carries out supercharging, and by methane rich unstripped gas with pre- Steam mixes, and the material of mixing is cooled to-10 ~-90 DEG C through heat exchanger, enters back into heavy hydrocarbon separator and takes off heavy hydrocarbon, obtains low temperature and does Gas, low temperature dry gas after heat exchanger cools down, through reducing pressure by regulating flow, then carries out gas-liquid separation, respectively obtains liquefaction and be the richest in after separation again Alkane gas, low-flash gas, liquefying high methane gas is as product collection, and low-flash gas, after heat exchanger heat exchange, carries out supercharging, enters Enter next circulation；
If methane rich unstripped gas is without heavy hydrocarbon, then after methane rich unstripped gas steam pre-with part mixes, directly cool down through heat exchanger, then After reducing pressure by regulating flow, carry out gas-liquid separation, after separation, respectively obtain liquefying high methane gas, low-flash gas, liquefying high methane gas Collecting as product, low-flash gas, after heat exchanger heat exchange, carries out supercharging, enters next one circulation；
(2) closed-loop refrigeration
After cooling medium is intensified, then through heat exchanger heat exchange, enter in decompressor, or cooling medium intensified after without heat exchange Device heat exchange and be sent directly in decompressor, obtain expand material, expand material again after heat exchanger heat exchange, return supercharging, enter Next circulation；
In described step (1), the fixed gas in liquefying high methane gas is drawn, using the fixed gas of extraction as fuel gas, for whole Individual system provides power resources；
In described step (1), the pressure of methane rich unstripped gas is 1MPaG ~ 20MPaG, temperature is-30 ~ 60 DEG C, or described in be the richest in Alkane unstripped gas is the self-evaporating steam of LNG storage tank.
The method of efficient expansion refrigeration high methane gas liquefaction the most according to claim 1, it is characterised in that described part preheats Gas mixes with methane rich unstripped gas, forms two strands of materials and enters heat exchanger；Or pre-steam is thoroughly mixed with methane rich unstripped gas, then It is divided into two strands of entrance heat exchangers.
The method of efficient expansion the most according to claim 1 or claim 2 refrigeration high methane gas liquefaction, it is characterised in that described step (1), in, low temperature dry gas, after heat exchanger cools down, then carries out reducing pressure by regulating flow, the progression of throttling be one-level throttling, two-step throttle, three Level throttling or level Four throttling.
4. according to the method for efficient expansion refrigeration high methane gas liquefaction described in any one of claim 1 ~ 3, it is characterised in that also wrap Include precooling step: outside cooling be connected with heat exchanger, carry out pre-cooling by the miscellaneous part in outside cooling heat exchanger.
The method of efficient expansion refrigeration high methane gas liquefaction the most according to claim 4, it is characterised in that described outside cooling The typical cryogen used is one or more in propylene, propane, ammonia, freon, water, BOG, lithium bromide.
6. according to the method for efficient expansion refrigeration high methane gas liquefaction described in any one of claim 1 ~ 5, it is characterised in that step (2), in, according to the pressure and temperature of methane rich unstripped gas, mix with pre-steam in the suitable position of system.
7. according to the method for efficient expansion refrigeration high methane gas liquefaction described in any one of claim 1 ~ 6, it is characterised in that described In step (1), low temperature dry gas is after heat exchanger cools down, then through reducing pressure by regulating flow, carries out gas-liquid subsequently into the first gas-liquid separator Separating, respectively obtain the first liquid phase thing, the first gas gas-phase objects after separation, this first liquid phase thing is liquefying high methane gas, and this is first years old Gas gas-phase objects is low-flash gas.
The method of efficient expansion refrigeration high methane gas liquefaction the most according to claim 7, it is characterised in that described step (1) In, the first liquid phase thing, after reducing pressure by regulating flow, enters the second gas-liquid separator and carries out gas-liquid separation, respectively obtain the second liquid after separation Phase thing, the second gas gas-phase objects, this second liquid phase thing is liquefying high methane gas；Second gas gas-phase objects is after heat exchanger heat exchange, as not Solidifying gas is drawn, and using the fixed gas of extraction as fuel gas, provides power resources for whole system.
9. for the device of method described in aforementioned any one of claim 1 ~ 8, it is characterised in that include that high methane gas liquefaction is System, open loop refrigeration system；
Described high methane gas liquefaction system includes for carrying the feedstock supply unit of methane rich unstripped gas, heat exchanger, gas-liquid are divided From device, described feedstock supply unit, heat exchanger, gas-liquid separator are sequentially connected by pipeline；
Described open loop refrigeration system includes gas-liquid separator, heat exchanger, compressor, decompressor, described gas-liquid separator, changes Hot device, compressor, decompressor constitute open-cycle system by pipeline；
There is provided another kind of alternative, including high methane gas liquefaction system, closed-loop refrigeration system；
Described methane gas liquefaction system includes feedstock supply unit, heat exchanger, gas-liquid separator, compressor, described raw material supply Device, heat exchanger, gas-liquid separator, compressor are sequentially connected by pipeline；
Described closed-loop refrigeration system includes that compressor, heat exchanger, decompressor, described compressor, heat exchanger, decompressor pass through Pipeline constitutes closed circulation system.
Device the most according to claim 6, it is characterised in that described high methane gas liquefaction system includes being the richest in for conveying The feedstock supply unit of alkane unstripped gas, heat exchanger, heavy hydrocarbon separator, gas-liquid separator, described feedstock supply unit, heat exchanger, Heavy hydrocarbon separator, gas-liquid separator are sequentially connected by pipeline.
CN201610395717.XA 2016-06-07 2016-06-07 Efficient expansion refrigeration methane-rich gas liquefaction method and device Pending CN106052303A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109999529A (en) * 2019-04-22 2019-07-12 中科瑞奥能源科技股份有限公司 Chemical industry tail gas process for separating and recovering and device

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1743436A (en) * 2005-09-27 2006-03-08 华南理工大学 Natural gas liquefying method for gas peak regulation and light hydrocarbon recovery
CN100404987C (en) * 2002-01-18 2008-07-23 Bp北美公司 Integrated processing of natural gas into liquid products
CN101338964A (en) * 2008-08-14 2009-01-07 苏州制氧机有限责任公司 Natural gas liquefaction device and liquefaction flow path
CN103582792A (en) * 2011-06-15 2014-02-12 盖斯康萨特有限公司 Process for liquefaction of natural gas

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100404987C (en) * 2002-01-18 2008-07-23 Bp北美公司 Integrated processing of natural gas into liquid products
CN1743436A (en) * 2005-09-27 2006-03-08 华南理工大学 Natural gas liquefying method for gas peak regulation and light hydrocarbon recovery
CN101338964A (en) * 2008-08-14 2009-01-07 苏州制氧机有限责任公司 Natural gas liquefaction device and liquefaction flow path
CN103582792A (en) * 2011-06-15 2014-02-12 盖斯康萨特有限公司 Process for liquefaction of natural gas

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109999529A (en) * 2019-04-22 2019-07-12 中科瑞奥能源科技股份有限公司 Chemical industry tail gas process for separating and recovering and device

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Application publication date: 20161026