CN104930815A - Marine natural gas liquefaction and NGL recycling system and application - Google Patents

Marine natural gas liquefaction and NGL recycling system and application Download PDF

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Publication number
CN104930815A
CN104930815A CN201510334802.0A CN201510334802A CN104930815A CN 104930815 A CN104930815 A CN 104930815A CN 201510334802 A CN201510334802 A CN 201510334802A CN 104930815 A CN104930815 A CN 104930815A
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China
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nitrogen
natural gas
heat exchanger
order
level
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CN201510334802.0A
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巨永林
陈卓
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Shanghai Jiaotong University
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Shanghai Jiaotong University
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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"
    • F25J1/004—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
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—Nitrogen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J1/0095—Oxides of carbon, e.g. CO2
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    • 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
    • F25J1/0204—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 as a single flow SCR cycle
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    • 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
    • F25J1/0205—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 as a dual level SCR refrigeration cascade
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F25J1/0267—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using flash gas as heat sink
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F25J1/0268—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using a dedicated refrigeration means
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    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F25J1/0277—Offshore use, e.g. during shipping
    • F25J1/0278—Unit being stationary, e.g. on floating barge or fixed platform
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    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • 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
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    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/80—Quasi-closed internal or closed external carbon dioxide refrigeration cycle

Abstract

The invention provides a marine LNGFPSO natural gas liquefaction and NGL recycling system. The system comprises an NGL fractionation module used for recycling natural gas condensate, a natural gas liquefaction module used for liquefying and supercooling natural gas, a CO2 transcritical circular precooling module and a nitrogen expansion refrigerating circulation module used for providing the cooling capacity for liquefying and supercooling natural gas. Compared with the prior art, the marine LNGFPSO natural gas liquefaction and NGL recycling system has the advantages that according to a marine LNG-FPSO prizing type nitrogen expansion natural gas liquefaction and NGL recycling technology, the process is simplified under the premise that the unit liquefaction energy consumption is low, and the process has the advantages that starting is fast, starting, shutting down and maintaining are convenient, equipment arrangement is compact, and prizing is convenient.

Description

Be applicable to marine natural gas liquefaction and NGL recovery system and application
Technical field
The invention belongs to chemical industry and cryogenic engineering technical field, be specifically related to a kind of be applicable to marine LNG-FPSO the liquefaction of skid-mounted type nitrogen expansion natural gas and NGL recovery system and method thereof.
Background technology
Natural gas and oil, coal, as fossil energy main in the world, occupy very large ratio in primary energy.Natural gas is as a kind of high-quality clean energy resource, and increasing country starts the development and utilization paying attention to natural gas resource.
Along with the continuous growth with natural gas consumption demand of continuing to optimize of China's energy resource structure, the present situation that the most gas field reserves of China are all little in addition, China's natural gas insufficiency of supply-demand is continuing to increase.It is predicted, the supply breach to the year two thousand twenty China's natural gas will reach 1000 × 10 8m 3.
On the other hand, there is the less marginal gas field of large volume production reserves, association gas field, gas field, deep-sea in China, individual well reserves are less, and distance gas transmission pipeline net work is far away, adopt pipe transmission method due to unreasonable economically and do not obtain effective exploitation and utilize, for a long time by emptying of igniting the torch.Conventional offshore natural gas exploitation, comprises offshore platform construction, lays sea-bottom natural gas conveyance conduit, on the bank natural gas liquefaction plant construction and build the infrastructure such as highway, the outer defeated harbour of LNG, investment is large, construction period is long, cash reclaims late, has a big risk.More than pin not enough, the technological development of FLNG and apparatus design are conceived to Low investment, fast operation and high benefit, collect the production of liquefied natural gas, store and be unloaded at all over the body, simplify the development process of offshore gas field, be specially adapted to the exploitation in marginal gas field and gas field, deep-sea, advantage is a lot of.
In addition, FLNG device is away from dense population areas, less on the impact of environment, and effectively prevent land LNG factory construction may pollution on the environment problem.FLNG device is convenient to migration, reusable, after the gas field exhaustion of exploitation, can be dragged to new gas field and again put into production.According to measuring and calculating, under the prerequisite of applicable application Floating Liquefied Natural Gas technology, Floating Liquefied Natural Gas process units is compared with the liquefied natural gas (LNG) plant on the bank of identical scale, and investment minimizing 20%, the completion time of project reduces 25%.
Up to the present, the subject matter that floating LNG process units faces is the exercise performance of platform self, restricted deck arrangement space and relevant safety measure, and a large amount of research work concentrates on cargo containment system, production technology module, outer transferring technology aspect.Through the external technology about Floating Liquefied device and economy research in recent years, the feasibility of system gets the nod substantially.An external existing type FLNG/FLPG device is being built at present, and more than 10 type devices are in research.
Summary of the invention
The object of the present invention is to provide a kind of be applicable to marine LNG-FPSO the liquefaction of skid-mounted type nitrogen expansion natural gas and NGL recovery system and method thereof; this skid-mounted type nitrogen expansion natural gas liquefaction and NGL fractionation process simple; start fast; startup-shutdown and easy to maintenance; compact arrangement of equipment; be convenient to into sled; energy consumption is lower; cooling agent part is single phase gas circulation; and cold-producing medium is safe, nontoxic, environmental protection, non-combustible medium, greatly adapt to that marine LNG-FPSO platform rocks, the requirement of security and compactedness.NGL recovery section applies TDWC (TOP DIVIDING WALLCOLUMN, see Fig. 1) device, dethanizer and de-oil gas tower two tower are merged into a tower, bosom has a dividing plate to be separated in two in space, respectively there is a condenser on both sides, top, according to actual deviate from the needs of gas componant, different refrigeration dutys is provided respectively, a reboiler is arranged at bottom, the theoretical tray number on dividing plate both sides and pressure also can adjust according to actual needs respectively, can obtain again required various hydrocarbon components while simplified apparatus.
The present invention is achieved by the following technical solutions:
The invention provides a kind of natural gas liquefaction and the NGL recovery system that are applicable to marine LNG-FPSO, it comprises:
For reclaiming the NGL fractionation module of gas reducing liquid;
For liquefying and crossing the natural gas liquefaction module of cold natural gas;
CO 2trans critical cycle precooling module; And
For being liquefaction and the nitrogen expansion kind of refrigeration cycle module crossing the right air lift semen donors of cold day;
Wherein, described NGL fractionation module comprises the domethanizing column and TDWC device that are connected successively;
Described natural gas liquefaction module comprises the liquefaction ice chest sled block and natural gas storage sled block that are connected successively;
Described CO 2trans critical cycle precooling module comprises CO 2compression sled block and CO 2decompressor;
Described nitrogen expansion kind of refrigeration cycle module comprises nitrogen expansion supercharging sled block;
Described liquefaction ice chest sled block comprises the first order heat exchanger, second level heat exchanger, third level heat exchanger and the choke valve that are connected successively, described nitrogen expansion supercharging sled block comprises nitrogen first order supercharger connected successively, nitrogen first order cooler, nitrogen second level supercharger, nitrogen second-stage cooler and the nitrogen first order decompressor be connected successively and nitrogen second level decompressor, described CO 2compression sled block comprises the CO be connected successively 2first order supercharger, CO 2first order cooler, CO 2second level supercharger, CO 2second-stage cooler;
Described first order heat exchanger is connected with nitrogen second-stage cooler, described second level heat exchanger is connected with domethanizing column and nitrogen first order decompressor, the described nitrogen second level decompressor other end is also connected successively with third level heat exchanger, second level heat exchanger, first order heat exchanger, nitrogen first order supercharger, described CO 2the CO of trans critical cycle precooling module 2decompressor also with first order heat exchanger, CO 2first order supercharger is connected successively;
Liquid-phase outlet and the natural gas storage of described liquefied natural gas separator are prized block and are connected, and the gaseous phase outlet of described liquefied natural gas separator is connected successively with third level heat exchanger, second level heat exchanger first order heat exchanger.
Preferably, described CO 2first order supercharger, CO 2second level supercharger is respectively by CO 2decompressor, nitrogen first order decompressor drive.
Preferably, natural gas boosting sled block should also be comprised.
Preferably, generator sled block, liquid nitrogen Contingency supply unit, CO is also comprised 2one or more in Contingency supply unit, instrument control unit, instrument wind, PSA nitrogen unit.When source of the gas there is no an electric power system time, prize block for liquefaction flow path by described generator and electric energy be provided; Liquid nitrogen Contingency supply unit and CO 2contingency supply unit is as Emergency use.
Be applicable to the natural gas liquefaction of marine LNG-FPSO and a using method for NGL recovery system as the aforementioned, it is characterized in that, comprise the steps:
A, raw natural gas is entered after the supercharging of described natural gas boosting sled block, cooling the domethanizing column of described NGL fractionation module, deviate to remove the natural gas of heavy hydrocarbon from top, obtain heavy hydrocarbon from bottom, described heavy hydrocarbon enters TDWC device again, and from top, out one end obtains C 1, C 2, C 3gas, the other end obtains C 3, C 4gas, out obtains C from bottom 5+liquid;
B, by removing heavy hydrocarbon after natural gas pass into described liquefaction ice chest sled block, liquefy through first order heat exchanger, again through second level heat exchanger and third level heat exchanger excessively cold, after choke valve reducing pressure by regulating flow to LNG storage pressure, enter liquefied natural gas separator, separation obtains liquefied natural gas product and flash steam, described gas product is delivered to natural gas storage sled block to store, described flash steam is returned successively described third level heat exchanger, second level heat exchanger and first order heat exchanger and cold is provided;
C, by CO 2gas is through described CO 2the block supercharging of compression sled, be cooled to supercriticality after, enter expander, decrease temperature and pressure to Near The Critical Point enters described first order heat exchanger phase-change heat-exchange and overheated, for the precooling of nitrogen cold rewarming is provided after return the circulation of compression sled block again;
D, nitrogen passed into described nitrogen expansion supercharging sled block, described first order heat exchanger, second level heat exchanger precooling is entered successively after nitrogen first order supercharger, nitrogen first order cooler, nitrogen second level supercharger, nitrogen second-stage cooler supercharging cooling, nitrogen after precooling enters nitrogen first order decompressor, nitrogen second level expander refrigeration, the nitrogen obtaining low-temp low-pressure returns third level heat exchanger successively, second level heat exchanger, first order heat exchanger provide cold, obtains the nitrogen that temperature raises and reenters described nitrogen expansion supercharging sled block.
Preferably, in steps A, when described raw natural gas pressure is higher than 4.89Mpa, do not enable described natural gas boosting sled block.
Preferably, in step B, described LNG storage pressure is 0.23MPa.
Preferably, in step C, CO 2cyclic process is trans critical cycle, and phase-change heat-exchange in first order heat exchanger is also overheated.
Preferably, in step D, described nitrogen second level outlet pressure of expansion machine should higher than 0.1MPa.
Compared with prior art, the present invention has following beneficial effect:
1, the liquefaction of skid-mounted type nitrogen expansion natural gas and the NGL recovery process being applicable to marine LNG-FPSO of the present invention, under the prerequisite that guarantor unit's liquefaction observable index is lower, simple flow, it is fast that this flow process has startup, startup-shutdown and easy to maintenance, compact arrangement of equipment, is convenient to into the feature of sled;
2, natural gas liquefaction process cooling agent part of the present invention is single phase gas circulation, and cold-producing medium is safe, nontoxic, environmental protection, non-combustible medium, has greatly adapted to that marine LNG-FPSO platform rocks, the requirement of security and compactedness;
3, this natural gas liquefaction and NGL recovery process NGL recovery section apply TDWC (TOP DIVIDINGWALL COLUMN) device, two towers are merged into a tower, can obtain again required various hydrocarbon components while simplified apparatus;
The analog computation of the HYSYS software 4, extensively adopted by gas industries, proved liquefaction process energy consumption is lower, comparatively strong to different source of the gas adaptability, is relatively be applicable to the skid-mounted type natural gas liquefaction of marine LNG-FPSO and the liquefaction flow path of NGL retracting device.
Accompanying drawing explanation
By reading the detailed description done non-limiting example with reference to the following drawings, other features, objects and advantages of the present invention will become more obvious:
Fig. 1 is the structural representation of TDWC synthetic tower in the present invention;
Fig. 2 is skid-mounted type nitrogen expansion natural gas of the present invention liquefaction and NGL recovery process flow chart;
In figure: 1, domethanizing column, 2, TDWC synthetic tower, 3, first order heat exchanger, 4, second level heat exchanger, 5, third level heat exchanger, 6, choke valve, 7, liquefied natural gas separator, 8, nitrogen second level decompressor, 9, nitrogen first order decompressor, 10, nitrogen second-stage cooler, 11, nitrogen second level supercharger, 12, nitrogen first order cooler, 13, nitrogen first order supercharger, 14, CO 2first order supercharger, 15, CO 2first order cooler, 16, CO 2second level supercharger, 17, CO 2second-stage cooler, 18, CO 2decompressor; 21, the first condenser; 22, the second condenser; 23, dividing plate; 24, tower body; 25, reboiler.
Detailed description of the invention
Below in conjunction with specific embodiment, the present invention is described in detail.Following examples will contribute to those skilled in the art and understand the present invention further, but not limit the present invention in any form.It should be pointed out that to those skilled in the art, without departing from the inventive concept of the premise, some distortion and improvement can also be made.These all belong to protection scope of the present invention.
Of the present invention be applicable to marine LNG-FPSO the liquefaction of skid-mounted type nitrogen expansion natural gas and NGL recovery process flow process as shown in Figure 2, this system comprises NGL fractionation module, natural gas liquefaction module (also claiming natural gas liquefaction loop), CO 2trans-critical cycle pre-cooling cycle module (also claims CO 2trans-critical cycle pre-cooling cycle loop) and nitrogen expansion kind of refrigeration cycle module (also claiming nitrogen expansion refrigeration cycle).
Described NGL fractionation module comprises the domethanizing column 1 and TDWC (TOP DIVIDINGWALLCOLUMN) synthetic tower 2 that are connected successively, and domethanizing column 1 and TDWC (TOP DIVIDINGWALL COLUMN) synthetic tower 2 can form NGL fractionation sled block.
The structure of TDWC (TOP DIVIDINGWALL COLUMN) synthetic tower 2 as shown in Figure 1, comprise the first condenser 21, second condenser 22, dividing plate 23, tower body 24 and reboiler 25, the top outer of tower body 24 is provided with two fluid passages, two fluid passages are respectively equipped with the first condenser 21 and the second condenser 22, the inside top of tower body 24 is installed with dividing plate 23, the bottom of tower body 24 is provided with a fluid passage, this fluid passage is provided with self-boiled device 25, during use, a fluid passage of the fluid passage and the second condenser 22 that are provided with the first condenser 21 in TDWC synthetic tower 2 is all connected with second level heat exchanger, the fluid passage being provided with self-boiled device 25 is connected with third level heat exchanger.
Described natural gas liquefaction loop comprises the first order heat exchanger 3, second level heat exchanger 4, third level heat exchanger 5, choke valve 6, the liquefied natural gas separator 7 that are connected successively; The liquid-phase outlet of described liquefied natural gas separator 7 is connected with LNG tank, and the gaseous phase outlet of described liquefied natural gas separator 7 is connected successively with third level heat exchanger 5, second level heat exchanger 4, first order heat exchanger 3.
Described first order heat exchanger 3, second level heat exchanger 4, third level heat exchanger 5, choke valve 6, liquefied natural gas separator 7 can form liquefaction ice chest sled block.
Described CO 2the pre-cold loop of trans critical cycle comprises the CO be connected successively 2first order supercharger 14, CO 2first order cooler 15, CO 2second level supercharger 16, CO 2second-stage cooler 17 and CO 2decompressor 18; Described CO 2decompressor 18 also respectively with first order heat exchanger 3, CO in natural gas liquefaction loop 2first order supercharger 14 is connected successively.
Described CO 2first order supercharger 14, CO 2first order cooler 15, CO 2second level supercharger 16 and CO 2second-stage cooler 17 forms CO 2compression sled block.
Described nitrogen expansion refrigeration cycle comprises nitrogen first order supercharger 13 connected successively, nitrogen first order cooler 12, nitrogen second level supercharger 11, nitrogen second-stage cooler 10 and the nitrogen first order decompressor 9 be connected successively and nitrogen second level decompressor 8; Described natural gas liquefaction loop first order heat exchanger 3 is also connected with nitrogen second-stage cooler 10, the second level, described natural gas liquefaction loop heat exchanger 4 is also connected with nitrogen first order decompressor 9, and described nitrogen second level decompressor 8 other end is also connected successively with natural gas liquefaction loop third level heat exchanger 5, second level heat exchanger 4, first order heat exchanger 3, nitrogen first order supercharger 13.
Described nitrogen first order supercharger 13, nitrogen first order cooler 12, nitrogen second level supercharger 11, nitrogen second-stage cooler 10 and nitrogen first order decompressor 9, nitrogen second level decompressor 8 form nitrogen expansion supercharging sled block.
At CO 2in Trans-critical cycle pre-cooling cycle loop, described CO 2first order supercharger 14, CO 2second level supercharger 16 is respectively by CO 2described in decompressor 18 and nitrogen expansion refrigeration cycle, nitrogen first order decompressor 9 drives.
Skid-mounted type nitrogen expansion natural gas liquefaction of the present invention and NGL recovery system also comprise generator sled block, liquid nitrogen Contingency supply unit, CO 2one or more in Contingency supply unit, instrument control unit, instrument wind, PSA nitrogen unit.When source of the gas there is no an electric power system time, prize block for liquefaction flow path by described generator and electric energy be provided; Liquid nitrogen Contingency supply unit and CO 2contingency supply unit is as Emergency use.
The method applying skid-mounted type nitrogen expansion natural gas of the present invention liquefaction and NGL recovery system liquefied natural gas and recovery NGL is specifically shown in following examples:
embodiment 1:
Natural gas molar constituent 1.54%N 2, 86.39%CH 4, 6.47%C 2h 6, 2.87%C 3h 8, 0.72%i-C 4h 10, 0.82%n-C 4h 10, 0.41%i-C 5h 12, 0.31%n-C 5h 12, 0.31%n-C 6h 14, 0.16%C7+, pressure 4.9MPa, temperature 35 DEG C, flow 1.512*10 4kgmol/h, the concrete steps of the liquefaction of skid-mounted type nitrogen expansion natural gas and NGL recovery process are as follows:
1, raw natural gas enters domethanizing column 1 rectifying, obtains heavy hydrocarbon from bottom, and temperature is 84.95 DEG C, and pressure is 4.9MPa, and top obtains natural gas, and temperature is-78.24 DEG C, and pressure is 4.89MPa;
2, the heavy hydrocarbon obtained through step 1 enters TDWC synthetic tower 2 rectifying, obtains C from bottom 5+, temperature is 166.7 DEG C, and pressure is 2.11MPa, and one end, top obtains C 1, C 2, C 3, temperature is 6.142 DEG C, and pressure is 2.725MPa, and the other end obtains C 3, C 4(oil gas), temperature is 58.79 DEG C, and pressure is 2.1MPa;
3, the natural gas obtained through step 1 liquefies and crosses be chilled to-154.6 DEG C through second level heat exchanger 4, third level heat exchanger 5;
4, the liquefied natural gas supercooled liquid obtained through step 3 by choke valve 6 reducing pressure by regulating flow to 0.2MPa after, enter liquefied natural gas separator 7, obtain liquefied natural gas product from bottom, flashed vapour returns three heat exchangers (third level heat exchanger 5, second level heat exchanger 4 and first order heat exchanger 3) and provides cold;
5, CO 2gas is through two-step supercharging machine (CO 2first order supercharger 14, CO 2second level supercharger 16) be pressurized to 2.5MPa, through cooler (CO 2first order cooler 15, CO2 second-stage cooler 17) be cooled to 40 DEG C;
6, through the cooled high pressure CO of step 5 2gas passes through CO 2after expander, decrease temperature and pressure enters first order heat exchanger 3 heat exchange to critical point (temperature is-76.99 DEG C, and pressure is 0.185MPa), and temperature is increased to 37 DEG C, returns CO 2first order supercharger 14, completes circulation;
7, nitrogen is pressurized to 2.2MPa through two-step supercharging machine (nitrogen first order supercharger 13, nitrogen second level supercharger 11), is cooled to 40 DEG C through cooler (nitrogen first order cooler 12, nitrogen second-stage cooler 10);
8, enter first order heat exchanger 3 successively through the cooled high pressure nitrogen of step 7, second level heat exchanger 4 is chilled to-60 DEG C in advance;
9, enter double expansion machine (nitrogen first order decompressor 9, nitrogen second level decompressor 8) successively through the nitrogen of step 8 precooling to expand and be depressurized to 0.14MPa, return three heat exchangers (third level heat exchanger 5, second level heat exchanger 4 and first order heat exchanger 3) after temperature reduces to-156.4 DEG C and cold is provided, and own temperature is raised;
10, the nitrogen after step 9 rewarming is to-17.89 DEG C reenters nitrogen first order supercharger 13 and completes circulation.
Draw through analog computation, the often consumption 1.244*10 of the liquefaction of this skid-mounted type nitrogen expansion natural gas and NGL recovery process 5the merit amount of kWh, can obtain 1.331*10 4kmolLNG, 349.9kmolC 1, C 2, C 3, 968.6kmolC 3, C 4(oil gas), 223.7kmol C 5+, the LNG liquefied fraction of this liquefaction process is 98%.
embodiment 2(situation for China's South China Sea certain associated gas source marine):
Natural gas molar constituent 1.1%N 2, 90.9%CH 4, 4.2%C 2h 6, 1.6%C 3h 8, 0.4%i-C 4h 10, 0.4%n-C 4h 10, 0.2%i-C 5h 12, 0.1%n-C 5h 12, 0.2%n-C 6h 14, 0.9%C 7+, pressure 5MPa, temperature 40 DEG C, flow 20*10 4nm 3/ d, the concrete steps of the liquefaction of skid-mounted type nitrogen expansion natural gas and NGL recovery process are as follows:
1, raw natural gas enters domethanizing column 1 rectifying, obtains heavy hydrocarbon from bottom, and temperature is 136.8 DEG C, and pressure is 4.9MPa, and top obtains natural gas, and temperature is-74.73 DEG C, and pressure is 4.89MPa;
2, the heavy hydrocarbon obtained through step 1 enters TDWC synthetic tower 2 rectifying, obtains C from bottom 5+, temperature is 195.3 DEG C, and pressure is 2.11MPa, and one end, top obtains C 1, C 2, C 3, temperature is 3.695 DEG C, and pressure is 2.725MPa, and the other end obtains C 3, C 4(oil gas), temperature is 64.9 DEG C, and pressure is 2.1MPa;
3, the natural gas obtained through step 1 liquefies and crosses be chilled to-153.4 DEG C through second level heat exchanger 4, third level heat exchanger 5;
4, the liquefied natural gas supercooled liquid obtained through step 3 by choke valve 6 reducing pressure by regulating flow to 0.2MPa after, enter liquefied natural gas separator 7, obtain liquefied natural gas product from bottom, flashed vapour returns three heat exchangers (third level heat exchanger 5, second level heat exchanger 4 and first order heat exchanger 3) and provides cold;
5, CO 2gas is through two-step supercharging machine (CO 2first order supercharger 14, CO 2second level supercharger 16) be pressurized to 2.5MPa, through cooler (CO 2first order cooler 15, CO 2second-stage cooler 17) be cooled to 40 DEG C;
6, through the cooled high pressure CO of step 5 2gas passes through CO 2after expander, decrease temperature and pressure enters first order heat exchanger 3 heat exchange to critical point (temperature is-76.99 DEG C, and pressure is 0.185MPa), and temperature is increased to 37 DEG C, returns CO 2first order supercharger 14, completes circulation;
7, nitrogen is pressurized to 2.2MPa through two-step supercharging machine (nitrogen first order supercharger 13, nitrogen second level supercharger 11), is cooled to 40 DEG C through cooler (nitrogen first order cooler 12, nitrogen second-stage cooler 10);
8, enter first order heat exchanger 3 successively through the cooled high pressure nitrogen of step 7, second level heat exchanger 4 is chilled to-60 DEG C in advance;
9, enter double expansion machine (nitrogen first order decompressor 9, nitrogen second level decompressor 8) successively through the nitrogen of step 8 precooling to expand and be depressurized to 0.14MPa, return three heat exchangers (third level heat exchanger 5, second level heat exchanger 4 and first order heat exchanger 3) after temperature reduces to-156.4 DEG C and cold is provided, and own temperature is raised;
10, the nitrogen after step 9 rewarming is to-6.164 DEG C reenters nitrogen first order supercharger 13 and completes circulation.
Draw through analog computation, the often consumption 2.852*10 of the liquefaction of this skid-mounted type nitrogen expansion natural gas and NGL recovery process 3the merit amount of kWh, can obtain 347.6kmolLNG, 1.492kmolC 1, C 2, C 3, 9.146kmolC 3, C 4(oil gas), 6.493kmol C 5+, the LNG liquefied fraction of this liquefaction process is 98%.Comparing embodiment 1 and embodiment 2 can find, this liquefaction process can adapt to unstripped gas change within the specific limits, only need certain the several parameter in adjusting process, prove that this liquefaction process has stronger adaptability to different source of the gas.
Above specific embodiments of the invention are described.It is to be appreciated that the present invention is not limited to above-mentioned particular implementation, those skilled in the art can make various distortion or amendment within the scope of the claims, and this does not affect flesh and blood of the present invention.

Claims (10)

1. be applicable to natural gas liquefaction and a NGL recovery system of marine LNG-FPSO, it is characterized in that, comprising:
For reclaiming the NGL fractionation module of gas reducing liquid;
For liquefying and crossing the natural gas liquefaction module of cold natural gas;
CO 2trans critical cycle precooling module; And
For being liquefaction and the nitrogen expansion kind of refrigeration cycle module crossing the right air lift semen donors of cold day;
Wherein, described NGL fractionation module comprises the domethanizing column and TDWC device that are connected successively;
Described natural gas liquefaction module comprises the liquefaction ice chest sled block and natural gas storage sled block that are connected successively;
Described CO 2trans critical cycle precooling module comprises CO 2compression sled block and decompressor;
Described nitrogen expansion kind of refrigeration cycle module comprises nitrogen expansion supercharging sled block;
Described liquefaction ice chest sled block comprises the first order heat exchanger, second level heat exchanger, third level heat exchanger and the choke valve that are connected successively, described nitrogen expansion supercharging sled block comprises nitrogen first order supercharger connected successively, nitrogen first order cooler, nitrogen second level supercharger, nitrogen second-stage cooler and the nitrogen first order decompressor be connected successively and nitrogen second level decompressor, described CO 2compression sled block comprises the CO be connected successively 2first order supercharger, CO2 first order cooler, CO 2second level supercharger, CO 2second-stage cooler;
Described first order heat exchanger is connected with nitrogen second-stage cooler and domethanizing column, described second level heat exchanger is also connected with nitrogen first order decompressor, the described nitrogen second level decompressor other end is also connected successively with third level heat exchanger, second level heat exchanger, first order heat exchanger, nitrogen first order supercharger, described CO 2the decompressor of trans critical cycle precooling module also with first order heat exchanger, CO 2first order supercharger is connected successively;
Liquid-phase outlet and the natural gas storage of described liquefied natural gas separator are prized block and are connected, and the gaseous phase outlet of described liquefied natural gas separator is connected successively with third level heat exchanger, second level heat exchanger first order heat exchanger.
2. be applicable to natural gas liquefaction and the NGL recovery system of marine LNG-FPSO as claimed in claim 1, it is characterized in that, described CO 2first order supercharger, nitrogen first order supercharger are driven by nitrogen first order decompressor, nitrogen second level decompressor respectively.
3. be applicable to natural gas liquefaction and the NGL recovery system of marine LNG-FPSO as claimed in claim 1 or 2, it is characterized in that, also should comprise natural gas boosting sled block and natural gas storage sled block.
4. be applicable to natural gas liquefaction and the NGL recovery system of marine LNG-FPSO as claimed in claim 3, it is characterized in that, also comprise generator sled block, liquid nitrogen Contingency supply unit, CO 2one or more in Contingency supply unit, instrument control unit, instrument wind, PSA nitrogen unit.
5. be applicable to the natural gas liquefaction of marine LNG-FPSO and a using method for NGL recovery system as claimed in claim 3, it is characterized in that, comprise the steps:
A, raw natural gas is entered after the supercharging of described natural gas boosting sled block, cooling the domethanizing column of described NGL fractionation module, deviate to remove the natural gas of heavy hydrocarbon from top, obtain heavy hydrocarbon from bottom, described heavy hydrocarbon enters TDWC device again, and from top, out one end obtains C 1, C 2, C 3gas, the other end obtains C 3, C 4gas, out obtains C from bottom 5+liquid;
B, by removing heavy hydrocarbon after natural gas pass into described liquefaction ice chest sled block, liquefy through first order heat exchanger, again through second level heat exchanger and third level heat exchanger excessively cold, after choke valve reducing pressure by regulating flow to LNG storage pressure, enter liquefied natural gas separator, separation obtains liquefied natural gas product and flash steam, described gas product is delivered to natural gas storage sled block to store, described flash steam is returned successively described third level heat exchanger, second level heat exchanger and first order heat exchanger and cold is provided;
C, by CO 2gas is through described CO 2the block supercharging of compression sled, be cooled to supercriticality after, enter choke valve throttling, decrease temperature and pressure to Near The Critical Point enters described first order heat exchanger phase-change heat-exchange and overheated, for the precooling of nitrogen and natural gas cold rewarming is provided after return CO again 2the circulation of compression sled block;
D, nitrogen passed into described nitrogen expansion supercharging sled block, described first order heat exchanger, second level heat exchanger precooling is entered successively after nitrogen first order supercharger, nitrogen first order cooler, nitrogen second level supercharger, nitrogen second-stage cooler supercharging cooling, nitrogen after precooling enters nitrogen first order decompressor, nitrogen second level expander refrigeration, the nitrogen obtaining low-temp low-pressure returns third level heat exchanger successively, second level heat exchanger, first order heat exchanger provide cold, obtains the nitrogen that temperature raises and reenters described nitrogen expansion supercharging sled block.
6. using method according to claim 5, is characterized in that, in steps A, when described raw natural gas pressure is higher than 4.89Mpa, does not enable described natural gas boosting sled block.
7. using method according to claim 5, it is characterized in that, in steps A, TDWC device is a synthetic tower, the inside of described synthetic tower is provided with the dividing plate be separated in two in space in synthetic tower, the top of synthetic tower and bottom are respectively equipped with a condenser and a reboiler, according to actual needs, provide different refrigeration dutys and thermic load respectively; The theoretical cam curve on dividing plate both sides also can adjust according to actual needs respectively.
8. using method according to claim 5, is characterized in that, in step B, described LNG storage pressure is 0.23MPa.
9. using method according to claim 5, is characterized in that, in step C, and CO 2cyclic process is trans critical cycle, and phase-change heat-exchange in first order heat exchanger is also superheated to supercriticality.
10. using method according to claim 5, is characterized in that, in step D, described nitrogen second level outlet pressure of expansion machine should higher than 0.1MPa.
CN201510334802.0A 2015-06-16 2015-06-16 Marine natural gas liquefaction and NGL recycling system and application Pending CN104930815A (en)

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Cited By (8)

* Cited by examiner, † Cited by third party
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CN106440656A (en) * 2016-11-02 2017-02-22 中国寰球工程有限公司 Natural gas liquefying system for carbon dioxide precooling double-stage nitrogen expansion
CN106642986A (en) * 2016-07-15 2017-05-10 上海利策科技股份有限公司 Natural gas liquefaction device used for offshore platform
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CN106642986A (en) * 2016-07-15 2017-05-10 上海利策科技股份有限公司 Natural gas liquefaction device used for offshore platform
CN106440656A (en) * 2016-11-02 2017-02-22 中国寰球工程有限公司 Natural gas liquefying system for carbon dioxide precooling double-stage nitrogen expansion
CN106440656B (en) * 2016-11-02 2022-02-15 中国寰球工程有限公司 Carbon dioxide precooling two-stage nitrogen expansion natural gas liquefaction system
CN106642985A (en) * 2016-12-01 2017-05-10 中国寰球工程有限公司 Quickly driving system used in floating liquid natural gas unit and driving method thereof
CN106642985B (en) * 2016-12-01 2019-07-02 中国寰球工程有限公司 A kind of rapid Start-Up system and its starting method for floating natural gas liquefaction device
CN108731375A (en) * 2018-06-24 2018-11-02 西南石油大学 A kind of mini gas liquefaction system of carbon dioxide precooling single-stage nitrogen expansion
CN109401802A (en) * 2018-11-22 2019-03-01 天津市振津石油天然气工程有限公司 It is a kind of for removing the skid-mounted unit of heavy hydrocarbon component in natural gas
CN112226259A (en) * 2020-10-20 2021-01-15 中海石油(中国)有限公司 High-efficient compact marine oil field associated gas recycle device
CN112556446A (en) * 2020-12-08 2021-03-26 江苏科技大学 Oil gas condensation recovery system of crude oil tanker and working method thereof
CN112556446B (en) * 2020-12-08 2022-08-19 江苏科技大学 Oil gas condensation recovery system of crude oil tanker and working method thereof
CN113108549A (en) * 2021-04-23 2021-07-13 吉林大学 Offshore natural gas liquefaction system integrating nitrogen expansion cycle with mixed refrigerant

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