CN102660341A - Process and device utilizing pressure of natural gas to partially liquefy natural gas - Google Patents

Process and device utilizing pressure of natural gas to partially liquefy natural gas Download PDF

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Publication number
CN102660341A
CN102660341A CN2012101283456A CN201210128345A CN102660341A CN 102660341 A CN102660341 A CN 102660341A CN 2012101283456 A CN2012101283456 A CN 2012101283456A CN 201210128345 A CN201210128345 A CN 201210128345A CN 102660341 A CN102660341 A CN 102660341A
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gas
heat exchanger
natural gas
heavy hydrocarbon
liquefaction
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CN102660341B (en
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何振勇
蔚龙
刘丽梅
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Xindi Energy Engineering Technology Co Ltd
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Xindi Energy Engineering Technology 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
    • 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
    • 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
    • F25J1/02—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
    • 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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0232—Coupling of the liquefaction unit to other units or processes, so-called integrated processes integration within a pressure letdown station of a high pressure pipeline system
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
    • F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Abstract

The invention provides a process and a device utilizing pressure of natural gas to partially liquefy the natural gas. The principle of the process and the device is that pressure energy of high-pressure natural gas generated during pressure regulation of a natural gas pressure regulation station is fully utilized, obtained cold quantity is used for liquefying part of the natural gas in pipe networks through the expansion refrigeration technology, and the value of the natural gas is greatly improved. By arranging a recycle gas circuit, the shortcoming of poor adaptability of variable working conditions of the expansion refrigeration technology is overcome, and variable load adaptability of the device is remarkably improved. In addition, when the device works with normal load, work energy consumption of a unit product approximates zero, and energy required by liquefaction completely comes from the pressure energy between a high-pressure pipe network and a low-pressure pipe network.

Description

Utilize the technology and the device of pressure energy of natural gas partial liquefaction Sweet natural gas
Technical field
The present invention relates to a kind of technology and device that utilizes pressure energy of natural gas partial liquefaction Sweet natural gas; Utilize the pressure ability of Sweet natural gas voltage regulating station at pressure regulation process mesohigh Sweet natural gas self; Use swell refrigeration technology that a part of natural gas liquefaction in the pipe network is become natural gas liquids, and device have good varying load adaptive faculty.
Background technology
Pipeline gas generally is transported to through long distance pipeline with the high pressure mode and presses pipe network in the city, before supplying to the terminal user, need carry out step-down through voltage adjusting device usually and handle so that the pressure of Sweet natural gas can with mate with the gas facility.Containing in the HPG huge pressure can, through in the process of voltage adjusting device pressure regulation, this part pressure can be often by slatterning in vain.In addition, owing to the rapid step-down of Sweet natural gas, cooling, be easy to the safe operation of voltage adjusting device and pipe-line equipment is constituted a threat to.Cold excessively for fear of voltage adjusting device and pipe-line equipment; Eliminate the temperature drop that produces in the step-down process; Usually need in the pressure regulation process, dispose hot water boiler, and with the part Sweet natural gas gas that acts as a fuel, the Sweet natural gas of voltage adjusting device, pipe-line equipment and main line is heated.So not only waste the pressure ability, also can consume a part of Sweet natural gas.If this part pressure can be used, not only can obtain considerable income, the loss that also can reduce Sweet natural gas improves the utilization ratio of Sweet natural gas.
Utilize HPG pressure ability, pressure can be converted to the energy of forms such as heat energy, cold energy, mainly realize through devices such as decompressors at present, utilize decompressor pressure recovery ability, its refrigerating efficiency can be up to 70～80% usually.But the varying duty bad adaptability of decompressor, when the inlet gas fluctuations in discharge is big, refrigerating efficiency that will the remarkably influenced decompressor.
Therefore, being necessary to design a kind of new pressure can utilize flow process to overcome the defective of prior art.
Summary of the invention
The objective of the invention is to solve above-mentioned technical problem, a kind of adaptive technology of varying load that makes full use of the HPG energy and can improve device is provided.
According to an aspect of the present invention, a kind of technology of utilizing pressure energy of natural gas partial liquefaction Sweet natural gas is provided, this technology comprises:
The Sweet natural gas that high pressure pipe network comes at first gets into the heavy hydrocarbon system of taking off, the heavy hydrocarbon that dewaters, make the Sweet natural gas dew points at normal pressure reduce to≤-76 ℃, the heavy hydrocarbon component more than the C6 is removed to≤217ppm; Take off the refrigeration gas of heavy hydrocarbon system as resurgent gases, remove the middle pressure pipe network in downstream behind the refrigeration gas regeneration ending with liquefaction system;
The Sweet natural gas that goes out to take off the heavy hydrocarbon system is divided into liquefaction gas circuit and refrigeration gas circuit, and the liquefaction gas circuit gets into decarbonization system, with CO wherein 2Be removed to≤70ppm; The flashed vapour of decarbonization system with liquefaction system removes the middle pressure pipe network in downstream as resurgent gases behind the flashed vapour regeneration ending; After after the liquefaction gas circuit after the decarburization gets into main heat exchanger, being cooled to-85 ℃～-142 ℃; (pressure unit MPaG is a MPa to 0.3MPaG～0.6MPaG through the throttling valve throttling; Represent gauge pressure) and get into separatory in the gas-liquid separator (being the liquid separation in the gas-liquid separation operation), the gas-liquid separator bottom liquid phases is LNG, goes the LNG storage tank stores; The flashed vapour of liquefaction does not return the main heat exchanger re-heat from the gas-liquid separator top; Re-heat is gone the resurgent gases as decarbonization system to normal temperature, accomplish reproduction operation and remove the middle pipe network of pressing afterwards;
After being cooled to-25 ℃～-55 ℃ after the main heat exchanger that refrigeration gas circuit that the heavy hydrocarbon system comes gets into liquefaction system is taken off in dehydration, go out main heat exchanger; Get into the expanding end of high temperature decompressor; It is that main heat exchanger provides cold that main heat exchanger is returned in expansion back (for example temperature is reduced to-60 ℃～-105 ℃); Self re-heat is simultaneously gone the pressurized end supercharging of high temperature decompressor then to normal temperature, after then after first water cooler is cooled to normal temperature, getting into main heat exchanger again and being cooled to-30 ℃～-70 ℃; Get into the expanding end expansion cooling (for example temperature is reduced to-90 ℃～-145 ℃) of cryogenic expansion machine; The gas phase that goes out expanding end is returned main heat exchanger then provides cold, after the pressurized end that gets into cryogenic expansion machine simultaneously behind self re-heat to normal temperature is pressurized to about 0.3MPaG～1.0MPaG, after second water cooler is cooled to normal temperature, goes out liquefaction system;
The refrigeration gas that goes out liquefaction system is divided into three the tunnel: the first via as stated, the heavy hydrocarbon system is taken off by the heavy hydrocarbon system that goes to dewater as dehydration resurgent gases; The second the tunnel takes off the heavy hydrocarbon system with aforementioned dehydration accomplishes regenerated resurgent gases and aforementioned decarbonization system and accomplishes and press pipe network in going after the regenerated resurgent gases is converged; Third Road goes to the circulation gas loop as circulation gas, returns through the circulation gas compression system and takes off the heavy hydrocarbon system entry.
In a preferred embodiment, take off heavy hydrocarbon and adopt the pressure swing adsorption technique flow process, utilize in activated alumina, 3A molecular sieve or 4A molecular sieve, the gac etc. one or more, water in the virgin gas and heavy hydrocarbon are absorbed as sorbent material.
The pressure swing adsorption technique flow process is described for example, and here referring to Fig. 2, the flow process of taking off the two tower pressure swing adsorption techniques that the heavy hydrocarbon system adopted is following:
Pressure swing adsorption technique adopts two tower paralleling models, and wherein tower T1 is in adsorption process and another tower T2 is in regenerative process.With adsorption tower T1 is example, explains that two tower pressure swing adsorption technique flow processs are following:
A, adsorption process: virgin gas gets into the adsorption tower T1 that is in adsorbed state through valve V1A from adsorption tower T1 top.Under the selection absorption of sorbent material, component to be removed wherein (like water, heavy hydrocarbon etc., be used to remove carbonic acid gas like this flow process, then be carbonic acid gas) etc. is adsorbed, and the gas that is not adsorbed goes out system through valve V5A at the bottom of tower.When the mass transfer zone forward position (being called absorb leading-edge) that is adsorbed impurity arrives bed outlet reservation section, turn off virgin gas feed valve V1A and the virgin gas outlet valve V5A of this adsorption tower T1, stop absorption, adsorption bed begins to change over to regenerative process.
Following process is carried out in the regeneration of adsorption tower T1 successively: release, heating, cold blowing, the process of boosting.
B, stress-relief process: after adsorption tower T1 adsorption process finishes, open valve V2A and adsorption tower T1 is carried out release, pressure is reduced to enough low, its composite bed is regenerated to guarantee that resurgent gases can get among the adsorption tower T1 smoothly in the program process of back against the absorption direction; The gas release that part is adsorbed discharges, and the gas that discharges goes out system behind valve V2A.
C, heat-processed: after stress-relief process finishes; Open valve V6, V4A; Resurgent gases gets into adsorption tower T1 and heats after resurgent gases well heater E1 is heated to certain temperature (for example 230～250 ℃), and reverse purging is adsorbent bed; The impurity that is adsorbed on the sorbent material is desorbed fully, make the sorbent material among the T1 obtain regeneration.
D, cold blowing process: after heat-processed finishes, open valve V7, V4A, close V6, resurgent gases gets into the adsorption tower T1 that is in the cold blowing process, and reverse purging is adsorbent bed, makes bed temperature reduce to certain temperature (for example about 40 ℃); The resurgent gases that goes out adsorption tower T1 goes out system, the cold blowing end of processing successively through valve V3A, resurgent gases water cooler E2, branch flow container T3 behind cooling, the separatory.
E, the process of boosting: behind the cold blowing end of processing, open valve V1A feeding virgin gas adsorption tower T1 is boosted.Preferably; In order adsorption tower can be switched to reposefully adsorb and to guarantee that product purity does not fluctuate in this course next time; Need slowly and reposefully adsorption column pressure be risen to adsorptive pressure through the variable valve that boosts, to guarantee the steady of the process of boosting and to reduce the influence of the fluctuation of pressure in the process of boosting to the adsorption tower generation with virgin gas.
Adsorption tower T1 has just accomplished complete " adsorption-regeneration " circulation after this process, for absorption is next time got ready.The absorption of adsorption tower T2 and regenerative process and adsorption tower T1 are identical, realize that through the action of controlling different valves two cone pulley flow operations reach the purpose of continuous purification gas.
As another kind of embodiment, following process is carried out in the regeneration of adsorption tower T1 successively: release, heating, cold blowing, release, the process of boosting.Before the process of boosting begins, open valve V2A and carry out release against the absorption direction, the resurgent gases that remains in the tower in the cold blowing process is fully discharged, the gas that discharges goes out system behind valve V2A.
Certainly, take off the heavy hydrocarbon system and also can adopt three tower pressure swing adsorption techniques.
In a preferred embodiment, it is the decarbonization system of main sorbent material that the liquefaction gas circuit gets into the 13X molecular sieve, adopts the pressure swing adsorption technique flow process, with CO wherein 2Be removed to≤70ppm, preferably extremely≤50ppm, more preferably extremely≤30ppm, further preferred≤20ppm.It is basic identical to be used for the pressure swing adsorption technique flow process of decarburization and pressure swing adsorption technique flow process that heavy hydrocarbon is taken off in aforementioned dehydration, is that the sorbent material that adopted is different, and the pressure swing adsorption technique flow process that is used for decarburization can be saved branch flow container T3 (not needing separatory).
In addition, be PTSA technology about pressure swing adsorption technique, not too preferably, also can be referring to Chinese patent ZL200810044270.7.
In a preferred embodiment; When gas consumption falls sharply (like night) when downstream,, start the circulation gas compression system for improving the varying load adaptive faculty of device; Make supercharging of part circulation gas and circulating involuting system inlet; With assurance device holdout device normal load still under the situation that gas consumption falls sharply, the steady and continuous operation of holding device has reduced the air demand that centering is pressed pipe network simultaneously.In a preferred embodiment, recycle gas compressor has the variable frequency adjustment function, can the flexible circulating flow rate and centering press the air demand of pipe network.
Second aspect of the present invention provides a kind of device that utilizes pressure energy of natural gas partial liquefaction Sweet natural gas, it is characterized in that, this device comprises the heavy hydrocarbon system of taking off, decarbonization system, liquefaction system and circulation gas compression system,
Wherein taking off the heavy hydrocarbon system has: a virgin gas access road; A gaseous phase outlet passage; A resurgent gases access road; A resurgent gases exit passageway, said gaseous phase outlet passage be divided into two branch roads promptly liquefy gas circuit with the refrigeration gas circuit, said resurgent gases exit passageway is connected with middle pressure pipe network;
Decarbonization system has: take off the gas phase access road that the liquefaction gas circuit of the said gaseous phase outlet passage of heavy hydrocarbon system is connected with dehydration; A clean gas outlet passage; A resurgent gases access road, a resurgent gases exit passageway, said resurgent gases exit passageway is connected with middle pressure pipe network;
The circulation gas compressed gas system comprises: compression set, an access road and an exit passageway;
Wherein liquefaction system comprises:
A main heat exchanger; It comprises at least six heat exchanger channels: the 5th and the 6th heat exchanger channels first, second, third, fourth,, and an end of said first heat exchanger channels is connected with the resurgent gases access road with the clean gas outlet passage of decarbonization system respectively with an end of second heat exchanger channels;
Gas-liquid separator, its inlet end is connected via the other end of throttling valve with first heat exchanger channels of said main heat exchanger, and the gas phase end of said gas-liquid separator is connected with the other end of second heat exchanger channels of main heat exchanger;
A high temperature decompressor, it comprises an expanding end and a pressurized end, the access road of said expanding end and exit passageway are connected with an end of the 3rd heat exchanger channels of said main heat exchanger, an end of the 4th heat exchanger channels respectively;
A cryogenic expansion machine, it comprises an expanding end and a pressurized end, the access road of said expanding end is connected with an end of the 5th heat exchanger channels of said main heat exchanger, an end of the 6th heat exchanger channels with exit passageway;
With first water cooler that the exit passageway of the pressurized end of said high temperature decompressor is connected, the other end of first water cooler is connected with the other end of the 5th heat exchanger channels;
With second water cooler that the exit passageway of the pressurized end of said cryogenic expansion machine is connected, the other end of second water cooler divide through pipeline three the tunnel take off the resurgent gases access road of heavy hydrocarbon system with said dehydration respectively, the access road of circulation gas compression system is connected with middle pressure pipe network;
The other end of the 3rd heat exchanger channels is connected with the refrigeration gas circuit of the said gaseous phase outlet passage that takes off the heavy hydrocarbon system, and the other end of the 4th heat exchanger channels is connected with the access road of the pressurized end of said high temperature decompressor;
The other end of the 6th heat exchanger channels is connected with the access road of the pressurized end of said cryogenic expansion machine;
The exit passageway of circulation gas compression system is connected with the virgin gas access road that takes off the heavy hydrocarbon system.
In a preferred embodiment, described dehydration is taken off the heavy hydrocarbon system and is adopted the pressure swing adsorption technique flow process, utilizes in activated alumina, 3A molecular sieve or 4A molecular sieve, the gac one or more as sorbent material; Remove water and heavy hydrocarbon in the Sweet natural gas, make the Sweet natural gas dew points at normal pressure reduce to≤-76 ℃, the above heavy hydrocarbon component of C6 is removed to≤217ppm; Preferably extremely≤150ppm; More preferably extremely≤120ppm, further preferred≤80ppm, preferred≤50ppm especially.
In a preferred embodiment, said decarbonization system adopts the pressure swing adsorption technique flow process, is the decarbonization system of main sorbent material with the 13X molecular sieve, with CO wherein 2Be removed to≤70ppm, preferably extremely≤50ppm, more preferably extremely≤30ppm, further preferred≤20ppm.
In a preferred embodiment, the Sweet natural gas that high pressure pipe network comes is divided into two-way through after taking off the heavy hydrocarbon system, and one the tunnel is the gas that is liquefied, and is called the liquefaction gas circuit, and another road overwhelming majority gas is called the refrigeration gas circuit.After the liquefaction gas circuit connects decarbonization system; An end that connects first gas phase channel of liquefaction system main heat exchanger; The other end of first gas phase channel connects gas-liquid separator after connecting throttling valve; Gas-liquid separator top flashed vapour passage goes the resurgent gases of decarbonization system as decarbonization system after connecting second gas phase channel of main heat exchanger, and the resurgent gases outlet connects in the downstream presses pipe network.
In a preferred embodiment, connect the expanding end of high temperature decompressor behind the 3rd heat exchanger channels of refrigeration gas circuit connection main heat exchanger, the back gas phase that expands gets into the 4th heat exchanger channels of main heat exchanger, and the gas phase after the said expansion is that main heat exchanger provides cold; The outlet of the 4th heat exchanger channels connects the access road of the pressurized end of high temperature decompressor; The pressurized end outlet conduit connects the 5th heat exchanger channels that connects main heat exchanger behind first water cooler; After the other end through the 5th heat exchanger channels connected the expanding end access road of cryogenic expansion machine, the 6th heat exchanger channels that gets into main heat exchanger from the expanding end exit passageway was that main heat exchanger provides cold; The other end of natural gas via the 6th heat exchanger channels after the re-heat is connected to the pressurized end access road of cryogenic expansion machine; The pressurized end outlet conduit is divided into three the tunnel after connecting second water cooler: the first via is the resurgent gases pipeline; It is that system provides resurgent gases that the heavy hydrocarbon system is taken off in connection, and the resurgent gases outlet connects in the downstream presses pipe network; Press pipe network in the second tunnel connection downstream; Third Road is a circulation loop, is connected to through the circulation gas compression system and takes off the heavy hydrocarbon system entry.
In a preferred embodiment; When the downstream gas consumption falls sharply,, start the circulation gas compression system for improving the varying load adaptive faculty of device; Make supercharging of part circulation gas and circulating involuting system inlet; With assurance device holdout device normal load still under the situation that gas consumption falls sharply, the steady and continuous operation of holding device reduces the air demand that centering is pressed pipe network simultaneously.
In a preferred embodiment, the compressor of circulation gas compression system has the variable frequency adjustment function, can the flexible circulating flow rate and centering press the air demand of pipe network.
Advantage of the present invention:
1, through the configuration cycles air compressor, eliminated the defective of swell refrigeration technology varying duty bad adaptability, significantly promoted the varying load adaptive faculty of device;
2, made full use of HPG pressure can, and the cold that conversion obtains is used for the liquefaction of part Sweet natural gas, can be used as peak regulation with or as the fuel of the LNG fuel vehicles, the value of Sweet natural gas is increased dramatically;
3, adopt high and low temperature decompressor swell refrigeration technology, make cold and hot fluid heat exchange curve more mate;
4, energy-conservation, the downstream gas consumption is normal load when (as in the daytime), and the work energy consumption of unit product is approximately zero, and the required energy that liquefies is all from the pressure ability between the high and low pressure pipe network.
Description of drawings
Fig. 1 is a process flow sheet of the present invention, and wherein 1 for to take off the heavy hydrocarbon system, and 2 is decarbonization system; 3 is liquefaction system, and 4 is the circulation gas compression system, and 31 is main heat exchanger; 32 is throttling valve, and 33 is gas-liquid separator, and 34 is the high temperature decompressor; 35 is cryogenic expansion machine, and 36 is first water cooler, and 37 is second water cooler.
Fig. 2 is the process flow sheet that heavy hydrocarbon system 1 is taken off in dehydration of the present invention.Wherein T1, T2 are adsorption tower, and T3 is for dividing flow container, and E1 is the resurgent gases well heater, and E2 is the resurgent gases water cooler.
Embodiment
Principle of the present invention is to make full use of the pressure ability of Sweet natural gas voltage regulating station at pressure regulation process mesohigh Sweet natural gas self; Use high and low temperature decompressor swell refrigeration technology that a part of natural gas liquefaction in the pipe network is become natural gas liquids; And, improve the varying load adaptive faculty of device through the configuration cycles air circuit.
As shown in Figure 1, the device that utilizes pressure energy of natural gas partial liquefaction Sweet natural gas of the present invention comprises through the interconnective dehydration of pipeline and takes off heavy hydrocarbon system 1, decarbonization system 2, liquefaction system 3 and circulation gas compression system 4; Said liquefaction system 3 comprises the main heat exchanger 31 that is used for heat exchange; 33, one high temperature decompressors 34 of 32, one gas-liquid separators of a throttling valve; 35, the first water coolers 36 of a cryogenic expansion machine and second water cooler 37.
As shown in Figure 2, it is following to take off the flow process of (two towers) pressure swing adsorption technique that heavy hydrocarbon system 1 adopted:
Pressure swing adsorption technique adopts two tower paralleling models, and wherein tower T1 is in adsorption process and another tower T2 is in regenerative process.With adsorption tower T1 is example, explains that two tower pressure swing adsorption technique flow processs are following:
A, adsorption process: virgin gas gets into the adsorption tower T1 that is in adsorbed state through valve V1A from adsorption tower T1 top.Under the selection absorption of sorbent material, component to be removed wherein is (like water, heavy hydrocarbon etc.; If this flow process is used to remove carbonic acid gas in addition, then for carbonic acid gas) etc. be adsorbed, the gas that is not adsorbed goes out system through valve V5A at the bottom of tower.When the mass transfer zone forward position (being called absorb leading-edge) that is adsorbed impurity arrives bed outlet reservation section, turn off virgin gas feed valve V1A and the virgin gas outlet valve V5A of this adsorption tower T1, stop absorption, adsorption bed begins to change over to regenerative process.
Following process is carried out in the regeneration of adsorption tower T1 successively: release, heating, cold blowing, the process of boosting.
B, stress-relief process: after adsorption tower T1 adsorption process finishes, open valve V2A and adsorption tower T1 is carried out release, pressure is reduced to enough low, its composite bed is regenerated to guarantee that resurgent gases can get among the adsorption tower T1 smoothly in the program process of back against the absorption direction; The gas release that part is adsorbed discharges, and the gas that discharges goes out system behind valve V2A.
C, heat-processed: after stress-relief process finishes; Open valve V6, V4A; Resurgent gases gets into adsorption tower T1 and heats after resurgent gases well heater E1 is heated to certain temperature (for example 230～250 ℃), and reverse purging is adsorbent bed; The impurity that is adsorbed on the sorbent material is desorbed fully, make the sorbent material among the T1 obtain regeneration.
D, cold blowing process: after heat-processed finishes, open valve V7, V4A, close V6, resurgent gases gets into the adsorption tower T1 that is in the cold blowing process, and reverse purging is adsorbent bed, makes bed temperature reduce to certain temperature (for example about 40 ℃); The resurgent gases that goes out adsorption tower T1 goes out system, the cold blowing end of processing successively through valve V3A, resurgent gases water cooler E2, branch flow container T3 behind cooling, the separatory.
E, the process of boosting: behind the cold blowing end of processing, open valve V1A feeding virgin gas adsorption tower T1 is boosted.Preferably; In order adsorption tower can be switched to reposefully adsorb and to guarantee that product purity does not fluctuate in this course next time; Need slowly and reposefully adsorption column pressure be risen to adsorptive pressure through the variable valve that boosts, to guarantee the steady of the process of boosting and to reduce the influence of the fluctuation of pressure in the process of boosting to the adsorption tower generation with virgin gas.
Adsorption tower T1 has just accomplished complete " adsorption-regeneration " circulation after this process, for absorption is next time got ready.The absorption of adsorption tower T2 and regenerative process and adsorption tower T1 are identical, realize that through the action of controlling different valves two cone pulley flow operations reach the purpose of continuous purification gas.
As another kind of embodiment, following process is carried out in the regeneration of adsorption tower T1 successively: release, heating, cold blowing, release, the process of boosting.Before the process of boosting begins, open valve V2A and carry out release against the absorption direction, the resurgent gases that remains in the tower in the cold blowing process is fully discharged, the gas that discharges goes out system behind valve V2A.
The Sweet natural gas that high pressure pipe network comes is divided into two-way after taking off heavy hydrocarbon system 1 through above-mentioned dehydration, and one the tunnel is the gas that is liquefied, and is called the liquefaction gas circuit, and another road overwhelming majority gas is called the refrigeration gas circuit.After the liquefaction gas circuit connects decarbonization system 2; An end that connects first heat exchanger channels (gas phase channel) of main heat exchanger 31 in the liquefaction system 3; The other end of first gas phase channel connects throttling valve 32 backs and connects gas-liquid separator 33; After gas-liquid separator 33 top flashed vapour passages connect second heat exchanger channels (gas phase channel) of main heat exchanger 31, go the resurgent gases of decarbonization system 2 as decarbonization system 2, the resurgent gases outlet connects in the downstream presses pipe network;
Connect the expanding end of high temperature decompressor 34 behind the 3rd heat exchanger channels of refrigeration gas circuit connection main heat exchanger 31, the back gas phase that expands gets into the 4th heat exchanger channels of main heat exchanger 31, and the gas phase after the said expansion is that main heat exchanger 31 provides cold; The outlet of the 4th heat exchanger channels connects the pressurized end of high temperature decompressor 34; The pressurized end outlet conduit connects the 5th heat exchanger channels that first water cooler, 36 backs connect main heat exchanger 31; After the other end through the 5th heat exchanger channels connected the expanding end of cryogenic expansion machine 35, the 6th heat exchanger channels that gets into main heat exchanger 31 was that main heat exchanger 31 provides cold; The other end of natural gas via the 6th heat exchanger channels after the re-heat is connected to the pressurized end of cryogenic expansion machine 35; The pressurized end outlet conduit connects and is divided into three the tunnel: the one tunnel behind second water cooler 37 is the resurgent gases pipeline; Connect and take off heavy hydrocarbon system 1 for system provides resurgent gases, the resurgent gases outlet connects in the downstream presses pipe network; Press pipe network in one tunnel connection downstream; Another road is a circulation loop, is connected to through circulation gas compression system 4 and takes off heavy hydrocarbon system 1 inlet.
The device that utilizes pressure energy of natural gas partial liquefaction Sweet natural gas of the present invention, the technical process of being adopted is following:
The Sweet natural gas that high pressure pipe network comes at first gets into the heavy hydrocarbon system 1 of taking off; Adopt the pressure swing adsorption technique flow process; Utilize in activated alumina, 3A molecular sieve or 4A molecular sieve, the gac etc. one or more as sorbent material; Water in the virgin gas and heavy hydrocarbon are absorbed, make the Sweet natural gas dew points at normal pressure reduce to≤-76 ℃, the above heavy hydrocarbon component of C6 is removed to≤217ppm; Take off the refrigeration gas of heavy hydrocarbon system as resurgent gases, remove the middle pressure pipe network in downstream behind the refrigeration gas regeneration ending with liquefaction system;
The Sweet natural gas that goes out to take off the heavy hydrocarbon system is divided into liquefaction gas circuit and refrigeration gas circuit, and it is the decarbonization system 2 of main sorbent material that the liquefaction gas circuit gets into the 13X molecular sieve, adopts the pressure swing adsorption technique flow process, with CO wherein 2Be removed to≤70ppm; Decarbonization system as resurgent gases, removes the middle pressure pipe network in downstream with the flashed vapour of liquefaction system 3 behind the flashed vapour regeneration ending; After after the liquefaction gas circuit after the decarburization gets into main heat exchanger 31 first heat exchanger channels, being cooled to-85 ℃～-142 ℃; To 0.3MPaG～0.6MPaG and get into gas-liquid separator 33 separatory, gas-liquid separator 33 bottom liquid phases are LNG, go the LNG storage tank stores through throttling valve 32 throttlings; The flashed vapour of liquefaction does not return main heat exchanger 31 second heat exchanger channels re-heats from gas-liquid separator 33 tops; Re-heat is gone the resurgent gases as decarbonization system 2 to normal temperature, accomplish reproduction operation and remove the middle pipe network of pressing afterwards;
The refrigeration gas circuit of taking off heavy hydrocarbon system 1 from dehydration goes out main heat exchanger 31 after getting into and being cooled to-25 ℃～-55 ℃ behind main heat exchanger 31 the 3rd heat exchanger channels of liquefaction system; Get into the expanding end access road of high temperature decompressor 34; It is that main heat exchanger 31 provides cold that main heat exchanger 31 the 4th heat exchanger channels is returned from the expanding end exit passageway in expansion back (for example temperature is reduced to-60 ℃～-105 ℃); While self re-heat is to normal temperature; Remove the pressurized end access road of high temperature decompressor 34 then; Pressurized end supercharging at high temperature decompressor 34; After then after first water cooler 36 is cooled to normal temperature, getting into main heat exchanger 31 the 5th heat exchanger channels again and be cooled to-30 ℃～-70 ℃ from the pressurized end exit passageway; Get into the expanding end access road of cryogenic expansion machine 35, in the cooling (for example temperature is reduced to-90 ℃～-145 ℃) of expanding of the expanding end of cryogenic expansion machine 35, the gas phase that goes out expanding end from the expanding end exit passageway is returned main heat exchanger 31 the 6th heat exchanger channels then provides cold; The pressurized end that simultaneously gets into cryogenic expansion machine 35 from the pressurized end access road of cryogenic expansion machine 35 behind self re-heat to normal temperature is pressurized to about 0.3MPaG～1.0MPaG, after second water cooler 37 goes out liquefaction system after being cooled to normal temperature;
The refrigeration gas that goes out liquefaction system is divided into three the tunnel: the one tunnel as stated, heavy hydrocarbon system 1 is taken off by the heavy hydrocarbon system 1 that goes to dewater as dehydration resurgent gases; One the tunnel takes off heavy hydrocarbon system 1 with aforementioned dehydration accomplishes regenerated resurgent gases and aforementioned decarbonization system 2 and accomplishes and press pipe network in going after the regenerated resurgent gaseses are converged; Third Road goes to the circulation gas loop as circulation gas, enters the mouth through circulation gas compression system retrieval system; When gas consumption falls sharply (like night) when downstream; For improving the varying load adaptive faculty of device; Start circulation gas compression system 4, make supercharging of part circulation gas and circulating involuting system inlet, with assurance device holdout device normal load still under the situation that gas consumption falls sharply; The steady and continuous of holding device is moved, and has reduced the air demand of centering pressure pipe network simultaneously.The compressor of circulation gas compression system 4 has the variable frequency adjustment function, can the flexible circulating flow rate and centering press the air demand of pipe network.

Claims (10)

1. a technology of utilizing pressure energy of natural gas partial liquefaction Sweet natural gas is characterized in that, this technology comprises:
The Sweet natural gas that high pressure pipe network comes at first gets into the heavy hydrocarbon system of taking off, the heavy hydrocarbon that dewaters, make the Sweet natural gas dew points at normal pressure reduce to≤-76 ℃, the heavy hydrocarbon component more than the C6 is removed to≤217ppm; Take off the refrigeration gas of heavy hydrocarbon system as resurgent gases, remove the middle pressure pipe network in downstream behind the refrigeration gas regeneration ending with liquefaction system;
The Sweet natural gas that goes out to take off the heavy hydrocarbon system is divided into liquefaction gas circuit and refrigeration gas circuit, and the liquefaction gas circuit gets into decarbonization system, with CO wherein 2Be removed to≤70ppm; The flashed vapour of decarbonization system with liquefaction system removes the middle pressure pipe network in downstream as resurgent gases behind the flashed vapour regeneration ending; After after the liquefaction gas circuit after the decarburization gets into main heat exchanger, being cooled to-85 ℃～-142 ℃; To 0.3MPaG～0.6MPaG and get into separatory in the gas-liquid separator, the gas-liquid separator bottom liquid phases is natural gas liquids through the throttling valve throttling, goes LNG tank to store; The flashed vapour of liquefaction does not return the main heat exchanger re-heat from the gas-liquid separator top; Re-heat is gone the resurgent gases as decarbonization system to normal temperature, accomplish reproduction operation and remove the middle pipe network of pressing afterwards;
After being cooled to-25 ℃～-55 ℃ after the main heat exchanger that refrigeration gas circuit that the heavy hydrocarbon system comes gets into liquefaction system is taken off in dehydration, go out main heat exchanger; Get into the expanding end of high temperature decompressor; Returning main heat exchanger after the expansion is that main heat exchanger provides cold; Self re-heat is simultaneously gone the pressurized end supercharging of high temperature decompressor then to normal temperature, after then after first water cooler is cooled to normal temperature, getting into main heat exchanger again and being cooled to-30 ℃～-70 ℃; The expanding end that gets into cryogenic expansion machine expands and lowers the temperature; The gas phase that goes out expanding end is returned main heat exchanger then provides cold, after the pressurized end that gets into cryogenic expansion machine simultaneously behind self re-heat to normal temperature is pressurized to about 0.3MPaG～1.0MPaG, after second water cooler is cooled to normal temperature, goes out liquefaction system;
The refrigeration gas that goes out liquefaction system is divided into three the tunnel: the first via as stated, the heavy hydrocarbon system is taken off by the heavy hydrocarbon system that goes to dewater as dehydration resurgent gases; The second the tunnel takes off the heavy hydrocarbon system with aforementioned dehydration accomplishes regenerated resurgent gases and aforementioned decarbonization system and accomplishes and press pipe network in going after the regenerated resurgent gases is converged; Third Road goes to the circulation gas loop as circulation gas, returns through the circulation gas compression system and takes off the heavy hydrocarbon system entry.
2. the technology of utilizing pressure energy of natural gas partial liquefaction Sweet natural gas according to claim 1; It is characterized in that; Take off heavy hydrocarbon and adopt the pressure swing adsorption technique flow process; Utilize in activated alumina, 3A molecular sieve or 4A molecular sieve, the gac etc. one or more as sorbent material, water in the virgin gas and heavy hydrocarbon are absorbed.
3. the technology of utilizing pressure energy of natural gas partial liquefaction Sweet natural gas according to claim 3 is characterized in that, it is the decarbonization system of main sorbent material that the liquefaction gas circuit gets into the 13X molecular sieve, adopts the pressure swing adsorption technique flow process, with CO wherein 2Be removed to≤70ppm.
4. the device that utilizes pressure energy of natural gas partial liquefaction Sweet natural gas according to claim 1; It is characterized in that: when the downstream gas consumption falls sharply,, start the circulation gas compression system for improving the varying load adaptive faculty of device; Make supercharging of part circulation gas and circulating involuting system inlet; With assurance device holdout device normal load still under the situation that gas consumption falls sharply, the steady and continuous operation of holding device reduces the air demand that centering is pressed pipe network simultaneously.
5. the device that utilizes pressure energy of natural gas partial liquefaction Sweet natural gas according to claim 4 is characterized in that: the compressor of circulation gas compression system has the variable frequency adjustment function, can the flexible circulating flow rate and centering press the air demand of pipe network.
6. a device that utilizes pressure energy of natural gas partial liquefaction Sweet natural gas is characterized in that, this device comprises through dehydration and take off heavy hydrocarbon system, decarbonization system, liquefaction system and circulation gas compression system,
Wherein taking off the heavy hydrocarbon system has: a virgin gas access road; A gaseous phase outlet passage; A resurgent gases access road; A resurgent gases exit passageway, said gaseous phase outlet passage be divided into two branch roads promptly liquefy gas circuit with the refrigeration gas circuit, said resurgent gases exit passageway is connected with middle pressure pipe network;
Decarbonization system has: take off the gas phase access road that the liquefaction gas circuit of the said gaseous phase outlet passage of heavy hydrocarbon system is connected with dehydration; A clean gas outlet passage; A resurgent gases access road, a resurgent gases exit passageway, said resurgent gases exit passageway is connected with middle pressure pipe network;
The circulation gas compressed gas system comprises: compression set, an access road and an exit passageway;
Wherein liquefaction system comprises:
A main heat exchanger; It comprises at least six heat exchanger channels: the 5th and the 6th heat exchanger channels first, second, third, fourth,, and an end of said first heat exchanger channels is connected with the resurgent gases access road with the clean gas outlet passage of decarbonization system respectively with an end of second heat exchanger channels;
Gas-liquid separator, its inlet end is connected via the other end of throttling valve with first heat exchanger channels of said main heat exchanger, and the gas phase end of said gas-liquid separator is connected with the other end of second heat exchanger channels of main heat exchanger;
A high temperature decompressor, it comprises an expanding end and a pressurized end, the access road of said expanding end and exit passageway are connected with an end of the 3rd heat exchanger channels of said main heat exchanger, an end of the 4th heat exchanger channels respectively;
A cryogenic expansion machine, it comprises an expanding end and a pressurized end, the access road of said expanding end is connected with an end of the 5th heat exchanger channels of said main heat exchanger, an end of the 6th heat exchanger channels with exit passageway;
With first water cooler that the exit passageway of the pressurized end of said high temperature decompressor is connected, the other end of first water cooler is connected with the other end of the 5th heat exchanger channels;
With second water cooler that the exit passageway of the pressurized end of said cryogenic expansion machine is connected, the other end of second water cooler divide through pipeline three the tunnel take off the resurgent gases access road of heavy hydrocarbon system with said dehydration respectively, the access road of circulation gas compression system is connected with middle pressure pipe network;
The other end of the 3rd heat exchanger channels is connected with the refrigeration gas circuit of the said gaseous phase outlet passage that takes off the heavy hydrocarbon system, and the other end of the 4th heat exchanger channels is connected with the access road of the pressurized end of said high temperature decompressor;
The other end of the 6th heat exchanger channels is connected with the access road of the pressurized end of said cryogenic expansion machine;
The exit passageway of circulation gas compression system is connected with the virgin gas access road that takes off the heavy hydrocarbon system.
7. the device that utilizes pressure energy of natural gas partial liquefaction Sweet natural gas according to claim 6; It is characterized in that; Described dehydration is taken off the heavy hydrocarbon system and is adopted the pressure swing adsorption technique flow process, utilizes in activated alumina, 3A molecular sieve or 4A molecular sieve, the gac one or more as sorbent material, removes water and heavy hydrocarbon in the Sweet natural gas; Make the Sweet natural gas dew points at normal pressure reduce to≤-76 ℃, the above heavy hydrocarbon component of C6 is removed to≤217ppm.
8. the device that utilizes pressure energy of natural gas partial liquefaction Sweet natural gas according to claim 6 is characterized in that, said decarbonization system adopts the pressure swing adsorption technique flow process, is the decarbonization system of main sorbent material with the 13X molecular sieve, with CO wherein 2Be removed to≤70ppm.
9. the device that utilizes pressure energy of natural gas partial liquefaction Sweet natural gas according to claim 6 is characterized in that, when the downstream gas consumption falls sharply; For improving the varying load adaptive faculty of device; Start the circulation gas compression system, make supercharging of part circulation gas and circulating involuting system inlet, with assurance device holdout device normal load still under the situation that gas consumption falls sharply; The steady and continuous operation of holding device reduces the air demand that centering is pressed pipe network simultaneously.
10. the device that utilizes pressure energy of natural gas partial liquefaction Sweet natural gas according to claim 9 is characterized in that the compressor of circulation gas compression system has the variable frequency adjustment function, can the flexible circulating flow rate and centering press the air demand of pipe network.
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CN106369935B (en) * 2016-10-27 2022-04-12 西南石油大学 Air separation system and method utilizing pressure energy of high-pressure natural gas pipe network
CN107569981A (en) * 2017-10-11 2018-01-12 杨正山 A kind of coal-burning power plant's flue gas collecting carbonic anhydride coupled biological charcoal preparation technology
CN112739970A (en) * 2018-09-20 2021-04-30 乔治洛德方法研究和开发液化空气有限公司 Plant and method for purifying and liquefying natural gas
CN112739970B (en) * 2018-09-20 2023-03-28 乔治洛德方法研究和开发液化空气有限公司 Plant and method for purifying and liquefying natural gas
CN109351144A (en) * 2018-11-30 2019-02-19 东华工程科技股份有限公司 The purification production system and technique of converter gas
CN114777412A (en) * 2022-04-01 2022-07-22 中国科学院理化技术研究所 Hydrogen liquefying plant with thermal siphon type hydrogen subcooler
CN114777412B (en) * 2022-04-01 2023-03-24 中国科学院理化技术研究所 Hydrogen liquefying plant with thermal siphon type hydrogen subcooler

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