CN103017480B - Liquefaction system for producing LNG (liquefied Natural gas) by utilizing pressure energy of pipeline - Google Patents
Liquefaction system for producing LNG (liquefied Natural gas) by utilizing pressure energy of pipeline Download PDFInfo
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- CN103017480B CN103017480B CN201210526647.9A CN201210526647A CN103017480B CN 103017480 B CN103017480 B CN 103017480B CN 201210526647 A CN201210526647 A CN 201210526647A CN 103017480 B CN103017480 B CN 103017480B
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- 239000003949 liquefied natural gas Substances 0.000 title abstract description 39
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 96
- 239000003345 natural gas Substances 0.000 claims abstract description 48
- 239000007789 gas Substances 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 238000001816 cooling Methods 0.000 claims abstract description 9
- 108091006146 Channels Proteins 0.000 claims description 74
- 238000000746 purification Methods 0.000 claims description 22
- 206010000060 Abdominal distension Diseases 0.000 claims description 21
- 208000024330 bloating Diseases 0.000 claims description 21
- 230000006835 compression Effects 0.000 claims description 9
- 238000007906 compression Methods 0.000 claims description 9
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 230000001172 regenerating effect Effects 0.000 abstract 4
- 239000007791 liquid phase Substances 0.000 abstract 1
- 239000012071 phase Substances 0.000 abstract 1
- 230000006837 decompression Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000032258 transport Effects 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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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
- F25J1/003—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"
- F25J1/0045—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 vaporising a liquid 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
- F25J1/02—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
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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
- F25J1/02—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
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed 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
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a gas liquefaction system, in particular to a liquefaction system for producing LNG (liquefied natural gas) by utilizing pressure energy of a natural gas pipeline. The natural gas from the high-pressure pipeline is divided into a liquefaction branch, a first precooling branch and a main cooling branch: the natural gas flow of the liquefaction branch comes from a high-pressure pipeline, the natural gas flow is compressed and cooled in sequence, the cold energy is obtained in a regenerative heat exchanger, the natural gas flow enters a gas-liquid separator after throttling, and the separated liquid phase is the produced LNG; the gas phase enters a low-pressure pipeline after passing through a regenerative heat exchanger to recover cold energy; the natural gas in the first precooling branch enters a low-pressure pipeline after being expanded by an expander and then is recovered in a heat regenerator; the main cold branch and the liquefaction branch are separated behind the cooler, and the natural gas in the main cold branch is cooled by the regenerative heat exchanger, throttled and expanded, then passes through the regenerative heat exchanger to recover cold energy, and finally enters the low-pressure pipeline. The system can produce LNG by utilizing the pressure energy of the pipeline, and the compressors are driven by the output work of the expansion machine without additional energy consumption.
Description
Technical field
The present invention relates to the liquefaction system of the LNG in derived energy chemical field, particularly a kind of liquefaction system utilizing pipeline pressure can produce LNG.
Background technology
Natural gas is a kind of high-quality, efficiently clean energy resource and industrial chemicals, is widely used in the every field of the development of the national economy.The natural gas pool of China nearly ninety percent concentrates on central and west regions, and the main gas line network that leans on transports to east, and annual design transport gas ability is at 90,000,000,000 m at present
3-1,000 hundred million m
3.Natural gas main pipeline is according to the difference of design; discharge pressure is at 4 to 10MPa; usually can be decompressed to 0.5 ~ below 1.2MPa through multi-step pressure reduction station after being transported to destination to recycle; this decompression process takes direct throttling usually; the a large amount of pressure energy wherein discharged is not utilized; the cold even avoiding throttling to produce causes damage to pipeline and equipment and needs additionally to consume the energy to heat the gas after throttling, causes serious high-grade energy waste.On the other hand, because low-pressure pipe network lays limitation, that supplies after high pressure pipe network decompression is limited in scope, and still has the user beyond a large amount of pipe network to utilize natural gas resource, needs to buy compressed natural gas or liquefied natural gas in addition.Therefore, utilize the pressure differential of high-low pressure pipeline enclosure in gas distributing system, realizing the process of a large amount of high-pressure natural gas decompression, will wherein liquefy by portion of natural gas, obtaining LNG, to supply the user beyond pipe network, is a kind of solution of killing two birds with one stone.There is the several technical scheme utilizing pipeline pressure energy at present, such as, all mention in patent CN202393170, CN202139209 and CN1409812A.For the situation that low pressure pipeline pressure is higher in its Patent CN202393170, the natural gas after expansion needs to enter low pressure pipeline through overcompression again, and the work done during compression of flash gas needs extra supply, and system needs extra power consumption.Expansion work in patent CN202139209 is not utilized, and system needs extra power consumption.And in patent CN1409812A, the post-expansion gas of precooling branch road returns circulation after recompression, system liquid rate can be made like this to improve still, and energy consumption is larger.In sum, the existing electrically-driven compressors that utilizes utilizing pipeline pressure energy LNG Technology to have improves gas pressure, what have utilizes the precooling of electric-driven refrigerating machine, and still need additional energy to input when reaching higher liquefied fraction, pressure energy utilization rate is not high.The present patent application proposes a kind of system and utilizes pipeline pressure can produce the technical scheme of LNG, cold is obtained by expanding from the natural gas of pressure duct, the pressure energy of natural gas is converted into cold energy, realize the liquefaction of portion of natural gas, produce LNG product and as commodity, also can may be used for peak regulation.In system for the portion gas of precooling without the need to doing deep purifying, alleviate purification pressure.
Summary of the invention
The object of the invention is to propose a kind of gas liquefaction system utilizing pipeline can produce LNG, this system can utilize the pressure differential of high-low pressure pipeline enclosure in Natural gas letdown station, liquefies, portion of natural gas without the need to extra power consumption, while realizing high-pressure air source decompression, production part LNG.
Technical scheme of the present invention is as follows:
The liquefaction system utilizing pipeline pressure can produce LNG provided by the invention has two kinds of schemes.
The first liquefaction system utilizing pipeline pressure can produce LNG provided by the invention described, it comprises:
The first class purification device P1 be connected is exported with gas pipeline pressure piping, described first class purification device P1 export pipeline installs the first distributing valve T1, and described first class purification device P1 export pipeline is divided into first paragraph liquefaction branch road M01 and the first precooling branch road M1 two-way through this first distributing valve T1; Described first paragraph liquefaction branch road M01 is the first compressor C1 after being connected to the first distributing valve T1 successively and the first cooler D1;
Be connected to the second cleaner P2 on described first cooler D1 export pipeline, described second cleaner P2 export pipeline installs the second distributing valve T2, described second cleaner P2 export pipeline divides two pipelines through this second distributing valve T2, and this two pipeline is second segment liquefaction branch road M02 and main cold branch road M2; Described second segment liquefaction branch road M02 is high-pressure channel, the high-pressure channel of the second Recuperative heat exchanger H2, the first throttle bloating plant V1 and gas-liquid separator S1 of the first Recuperative heat exchanger H1 after being connected to the second distributing valve T2 successively; The cold branch road M2 of described master is the high-pressure channel of the first Recuperative heat exchanger H1 after being connected to the second distributing valve T2 successively, the high-pressure channel of the second Recuperative heat exchanger H2, the second throttling bloating plant V2, the low-pressure channel of the second Recuperative heat exchanger H2, the low-pressure channel of the first Recuperative heat exchanger H2 and the low pressure pipeline of gas pipeline;
Described gas-liquid separator S1 bottom end outlet is LNG product outlet, and gas-liquid separator S1 top exports the low-pressure channel, the low-pressure channel of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline that connect the second Recuperative heat exchanger H2 successively;
First precooling branch road M1 is the first decompressor E1 being connected to the first distributing valve T1, and this first decompressor E1 connects the low-pressure channel of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline successively; The work done during compression of described first compressor C1 is from the expansion work of the first decompressor E1.
Described first throttle bloating plant V1 is choke valve.
The liquefaction system utilizing pipeline pressure can produce LNG provided by the invention, also can comprise the second compressor C2 and the second cooler D2, and described second throttling bloating plant V2 is the second decompressor E2; After described second compressor C2 and the second cooler D2 is connected to the second distributing valve T2 successively and between the pressure piping of described first Recuperative heat exchanger H1 on pipeline; The work done during compression of described second compressor C2 is from the expansion work of the second decompressor E2.
Described first cooler D1 and the second cooler D2 is water-cooling cooler or air-cooled cooler; Cooler outlet natural gas temperature is 10 ~ 40 DEG C.
Described the second liquefaction system utilizing pipeline pressure can produce LNG provided by the invention, it comprises:
The first class purification device P1 be connected is exported with gas pipeline pressure piping, described first class purification device P1 export pipeline installs the first distributing valve T1, and described first class purification device P1 export pipeline is divided into first paragraph liquefaction branch road M01 and the first precooling branch road M1 two-way through the first distributing valve T1; Described first paragraph liquefaction branch road M01 is the first compressor C1 after being connected to the first distributing valve T1 successively and the first cooler D1;
Be connected to the second cleaner P2 on described first cooler D1 export pipeline, described second cleaner P2 is connected with the high-pressure channel of the first Recuperative heat exchanger H1; The high-pressure channel export pipeline of the first Recuperative heat exchanger H1 is installed the second distributing valve T2, and the high-pressure channel export pipeline of described first Recuperative heat exchanger H1 is divided into second segment liquefaction branch road M02 and main cold branch road M2 two-way through this second distributing valve T2; Described second segment liquefaction branch road M02 is high-pressure channel, the first throttle bloating plant V1 and gas-liquid separator S1 of the second Recuperative heat exchanger H2 after being connected to the second distributing valve T2 successively; The cold branch road M2 of described master is the high-pressure channel of the second Recuperative heat exchanger H2 after being connected to the second distributing valve T2 successively, the second throttling bloating plant V2, the low-pressure channel of the second Recuperative heat exchanger H2, the low-pressure channel of the first Recuperative heat exchanger H2 and the low pressure pipeline of gas pipeline;
Described gas-liquid separator S1 bottom end outlet is LNG product outlet, and gas-liquid separator S1 top exports the low-pressure channel, the low-pressure channel of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline that connect the second Recuperative heat exchanger H2 successively;
First precooling branch road M1 is the first decompressor E1 being connected to the first distributing valve T1, and this first decompressor E1 connects the low-voltage tube passage of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline successively; Described first decompressor E1 provides driving force for described first compressor C1.
The second provided by the invention utilizes pipeline pressure can produce the liquefaction system of LNG, also can comprise the 3rd Recuperative heat exchanger H3, the second compressor C2, the second cooler D2 and the second precooling branch road M3; The first throttle bloating plant V1 of described second liquefaction branch road M02 is choke valve; The second throttling bloating plant V2 of the cold branch road M2 of described master is the second decompressor E2;
Described 3rd Recuperative heat exchanger H3 is arranged at described first Recuperative heat exchanger H1 and and between Recuperative heat exchanger H2; Connecting line between first class purification device P1 and the second compressor D2 is provided with the 3rd distributing valve T3, is divided into two pipelines after the 3rd distributing valve T3, this two pipeline is the 3rd section of liquefaction branch road M03 and the second precooling branch road M3;
Described second compressor C2 and the second cooler D2 is connected between the pressure piping of the 3rd distributing valve T3 and the first Recuperative heat exchanger H1 successively;
3rd section of liquefaction branch road M03 is connected to the second compressor C2, the second cooler D2 between the 3rd distributing valve T3 and the second distributing valve T2 on connecting line, the pressure piping of the first Recuperative heat exchanger H1 and the pressure piping of the 3rd Recuperative heat exchanger H3 successively; The pressure piping outlet of described 3rd Recuperative heat exchanger H3 is connected with described second distributing valve T2;
Described precooling branch road M3 is connected to the pressure piping of the first Recuperative heat exchanger H1 after the 3rd distributing valve T3, the second decompressor E2, the low pressure pipeline of the 3rd Recuperative heat exchanger H3, the low pressure pipeline of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline in turn; The work done during compression of described second compressor C2 is from the expansion work of the second decompressor E2.
Described first cooler D1 and the second cooler D2 is water-cooling cooler or air-cooled cooler; Cooler outlet natural gas temperature is 10 ~ 40 DEG C.
The liquefaction system utilizing pipeline pressure can produce LNG provided by the invention, obtaining cold by expanding from the natural gas of pressure duct, the pressure energy of natural gas being converted into cold energy, realizing the liquefaction of portion of natural gas, producing LNG product and carry out storing or transporting.Because one-level precooling temperature is higher, this portion gas, without the need to doing deep purifying, alleviates purification pressure.In this system, the work done during compression of all compressors is from decompressor, has reclaimed pressure energy, and without the need to additional energy input, the LNG produced as commodity, also can may be used for peak regulation and use.
Accompanying drawing explanation
Fig. 1 is the system diagram utilizing pipeline pressure can produce the liquefaction system of LNG of the present invention in embodiment 1;
Fig. 2 is the system diagram utilizing pipeline pressure can produce the liquefaction system of LNG of the present invention in embodiment 2;
Fig. 3 is the system diagram utilizing pipeline pressure can produce the liquefaction system of LNG of the present invention in embodiment 3;
Fig. 4 is the system diagram utilizing pipeline pressure can produce the liquefaction system of LNG of the present invention in embodiment 4.
Detailed description of the invention
Below in conjunction with drawings and Examples, the present invention is further elaborated.
Embodiment 1: as shown in Figure 1, the liquefaction system of the present embodiment 1 comprises first class purification device P1, second cleaner P2, first compressor C1, the first cooler D1, the first decompressor E1, first Recuperative heat exchanger H1, second Recuperative heat exchanger H2, first throttle valve V1, second throttle V2 and gas-liquid separator S1;
First natural gas from pressure piping slightly purifies dehydration through first class purification device P1, then after the first distributing valve T1, is divided into two-way, and this two-way is respectively the first precooling branch road M1 and first paragraph liquefaction branch road M01;
The natural gas flow entering first paragraph liquefaction branch road M01 flows through the first compressor C1 successively and the first cooler D1 compresses and is cooled; Enter second cleaner P2 afterwards, slough after acid gas and impurity obtains deep purifying in second cleaner P2, after the second distributing valve T2, be divided into two-way, this two-way is respectively main cold branch road M2 and second segment liquefaction branch road M02;
The natural gas flow entering second segment liquefaction branch road M02 flows through the Article 1 high-pressure channel of the first Recuperative heat exchanger H1 and the Article 1 high-pressure channel of the second regenerator H2 successively, then after first throttle valve V1 throttling, enters gas-liquid separator S1; Liquid in gas-liquid separator S1 is flowed out from gas-liquid separator S1 lower part outlet by pipeline TK, for the LNG produced, gas in gas-liquid separator S1 flows out from gas-liquid separator S1 upper outlet, the Article 1 low-pressure channel of the Article 1 low-pressure channel and the first Recuperative heat exchanger H1 that flow through the second Recuperative heat exchanger H2 successively reclaims cold, finally enters low pressure pipeline;
Reclaim cold by the Article 3 low-pressure channel of the first Recuperative heat exchanger H1 after the natural gas flow flowed in the first precooling branch road M1 expands in the first decompressor E1, finally enter low pressure pipeline;
Flow into main cold branch road M2 natural gas flow successively by the Article 2 high-pressure channel of the first Recuperative heat exchanger H1 and the Article 2 high-pressure channel of the second Recuperative heat exchanger H2, then after second throttle V2 throttling expansion, reclaim cold through the Article 2 low-pressure channel of the second Recuperative heat exchanger H2 and the Article 2 low-pressure channel of the first Recuperative heat exchanger H1 successively again, finally enter low pressure pipeline.
The driving of described first compressor C1 is from the expansion work of described first decompressor E1;
The first distributing valve T1 of the present embodiment is positioned at first class purification device P1 exit, and the second distributing valve T2 is positioned at second cleaner P2 exit;
Natural Gas High-pressure Pipeline pressure in the present embodiment 1 is 4.1MPa, and low pressure pipeline is 0.58MPa, and gas discharge is 1705Nm
3under the gas source condition of/h, pressure energy can be utilized to produce 247Nm
3the LNG of/h, liquefied fraction is 14.5%, and required energy consumption is only the cooling tower pump energy consumption of the cooler D1 adopting water-cooled, and the liquefaction system utilizing pipeline pressure can produce LNG of the present invention has higher reliability and adaptability, and operating cost is low.
Embodiment 2:
As shown in Figure 2, the present embodiment 2 is with the difference of embodiment 1:
Second distributing valve T2 is between the first Recuperative heat exchanger H1 and the second Recuperative heat exchanger H2;
Second throttle V2 export pipeline in main cold branch road M2 connects into liquefaction branch road M02 at the d place of gas-liquid separator S1 upper outlet pipeline; The e point place of the first decompressor E1 export pipeline between the first Recuperative heat exchanger H1 and the second Recuperative heat exchanger H2 of the first precooling branch road M1 connects into the branch road M02 that liquefies;
System remainder is identical with embodiment 1.
The advantage of system in the present embodiment 2 compared with embodiment 1 is: the first Recuperative heat exchanger H1 is binary channels, second Recuperative heat exchanger H2 is 3 passages, its manufacture difficulty and cost are all less than in embodiment 1, increase reliability and reduce initial cost when not changing running effect.
Embodiment 3:
As shown in Figure 3, the present embodiment 3 is with the difference of embodiment 1: the throttling expansion equipment choosing second decompressor E2 of main cold branch road M2, adds the second compressor C2 and the second cooler D2, be specially:
After main cold branch road M2 isolates from the distributing valve T2 in second cleaner P2 exit, Article 2 high-pressure channel through the first Recuperative heat exchanger H1 enters the second decompressor E2, the Article 2 low-pressure channel of Article 2 low-pressure channel and the first Recuperative heat exchanger H1 that the natural gas after the second decompressor E2 expands flows through the second Recuperative heat exchanger H2 successively reclaims cold, finally enters low pressure pipeline;
The natural gas of first paragraph liquefaction branch road M01 from second cleaner P2 out afterwards after the second compressor C2 and subsequent the second cooler D2, after entering the Article 1 high-pressure channel of the first Recuperative heat exchanger H1 and the Article 1 high-pressure channel of the second Recuperative heat exchanger H2 again, after first throttle valve V1, entering gas-liquid separator S1; The driving merit of the second compressor C2 is from the second decompressor E2;
Identical with embodiment 1 of system remainder.
System in the present embodiment 3, under gas source condition in the same manner as in Example 1, can produce 324Nm
3the LNG of/h, liquefied fraction is 19%, higher than the system in embodiment 1.But owing to adopting two decompressor and double-compressor, system complexity is higher.
Embodiment 4:
As shown in Figure 4, the pipeline pressure that utilizes of the present embodiment 4 can produce the liquefaction system of LNG, and its structure comprises:
Export with gas pipeline pressure piping the first class purification device P1 be connected, after the first distributing valve T1 on this first class purification device P1 export pipeline, be divided into first paragraph liquefaction branch road M01 and the first precooling branch road M1 two-way; Described first paragraph liquefaction branch road M01 is the first compressor C1 after being connected to the first distributing valve T1 successively and the first cooler D1;
Be connected to the second cleaner P2 on described first cooler D1 export pipeline, described second cleaner P2 is connected with the pressure piping of the first Recuperative heat exchanger H1; The pressure piping export pipeline of the first Recuperative heat exchanger H1 is established the second distributing valve T2, after this second distributing valve T2, is divided into second segment liquefaction branch road M02 and main cold branch road M2 two-way; Described second segment liquefaction branch road M02 is pressure piping, the first throttle bloating plant V1 and gas-liquid separator S1 of the second Recuperative heat exchanger H2 after being connected to the second distributing valve T2 successively; The cold branch road M2 of described master is the pressure piping of the second Recuperative heat exchanger H2 after being connected to the second distributing valve T2 successively, the second throttling bloating plant V2, the low pressure pipeline of the second Recuperative heat exchanger H2, the low pressure pipeline of the first Recuperative heat exchanger H2 and the low pressure pipeline of gas pipeline;
Described gas-liquid separator S1 bottom end outlet is LNG product outlet, and gas-liquid separator S1 top exports the low pressure pipeline, the low pressure pipeline of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline that connect the second Recuperative heat exchanger H2 successively;
First precooling branch road M1 is the first decompressor E1 being connected to the first distributing valve T1, and this first decompressor E1 connects the low pressure pipeline of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline successively; Described first decompressor E1 provides driving force for described first compressor C1.
Its structure also can comprise the 3rd Recuperative heat exchanger H3, the second compressor C2, the second cooler D2 and the second precooling branch road M3; The second throttling bloating plant V2 of the cold branch road M2 of described master is the second decompressor E2;
Described 3rd Recuperative heat exchanger H3 is arranged at described first Recuperative heat exchanger H1 and and between Recuperative heat exchanger H2; Connecting line between first class purification device P1 and the second compressor D2 is provided with the 3rd distributing valve T3, is divided into two pipelines after the 3rd distributing valve T3, this two pipeline is the 3rd section of liquefaction branch road M03 and the second precooling branch road M3;
Described second compressor C2 and the second cooler D2 is connected between the pressure piping of the 3rd distributing valve T3 and the first Recuperative heat exchanger H1 successively;
3rd section of liquefaction branch road M03 is connected to the second compressor C2, the second cooler D2 between the 3rd distributing valve T3 and the second distributing valve T2 on connecting line, the pressure piping of the first Recuperative heat exchanger H1 and the pressure piping of the 3rd Recuperative heat exchanger H3 successively; The pressure piping outlet of described 3rd Recuperative heat exchanger H3 is connected with described second distributing valve T2;
Described precooling branch road M3 is connected to the pressure piping of the first Recuperative heat exchanger H1 after the 3rd distributing valve T3, the second decompressor E2, the low pressure pipeline of the 3rd Recuperative heat exchanger H3, the low pressure pipeline of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline in turn; The work done during compression of described second compressor C2 is from the expansion work of the second decompressor E2.
Described first cooler D1 and the second cooler are water-cooling cooler or air-cooled cooler; Gas pipeline pressure piping outlet temperature is 10 ~ 40 DEG C.Described first throttle bloating plant V1 is choke valve.
The pipeline pressure that utilizes shown in Fig. 4 can produce the liquefaction system of LNG, and its flow process is as follows:
First natural gas from pressure piping slightly purifies dehydration through first class purification device P1, then after the first distributing valve T1, is divided into two-way, and this two-way is respectively the first precooling branch road M1 and first paragraph liquefaction branch road M01;
The natural gas flow entering first paragraph liquefaction branch road M01 compresses through the first compressor C1 and the first cooler D1 and is cooled successively, enter second cleaner P2 afterwards, slough after acid gas and impurity obtains deep purifying in second cleaner P2, after the 3rd distributing valve T3, be divided into two-way, this two-way is respectively the second precooling branch road M3 and the 3rd section of liquefaction branch road M03;
The natural gas flow entering the 3rd section of liquefaction branch road M03 compresses through the second compressor C2 and the second cooler D2 and is cooled successively, then after entering the Article 1 high-pressure channel of the first Recuperative heat exchanger H1 and the Article 1 high-pressure channel of the 3rd regenerator H3, after the second distributing valve T2, be divided into two-way, this two-way is respectively main cold branch road M2 and second segment liquefaction branch road M02;
The natural gas flow entering second segment liquefaction branch road M02 flows through the Article 1 high-pressure channel of the second regenerator H2, then after first throttle valve V1 throttling, enters gas-liquid separator S1; Liquid in gas-liquid separator S1 is flowed out from gas-liquid separator S1 lower part outlet by pipeline TK, for the LNG produced, gas in gas-liquid separator S1 flows out from gas-liquid separator S1 upper outlet, flow through the Article 1 low-pressure channel of the second Recuperative heat exchanger H2, the Article 1 low-pressure channel of the 3rd Recuperative heat exchanger H3 and the Article 1 low-pressure channel of the first Recuperative heat exchanger H1 successively and reclaim cold, finally enter the low pressure pipeline of natural gas;
Reclaim cold by the Article 3 low-pressure channel of the first Recuperative heat exchanger H1 after the natural gas flow flowing into the first precooling branch road M1 expands in the first decompressor E1, finally enter low pressure pipeline;
The natural gas flow flowing into main cold branch road M2 flows through the Article 2 high-pressure channel of the second Recuperative heat exchanger H2, then after second throttle V2 throttling expansion, reclaim cold through the Article 2 low-pressure channel of the Article 2 low-pressure channel of the second Recuperative heat exchanger H2, the Article 2 low-pressure channel of the 3rd regenerator and the first Recuperative heat exchanger H1 successively again, finally enter the low pressure pipeline of natural gas.
First the natural gas flow flowing into the second precooling branch road M3 flows through the Article 2 high-pressure channel of Recuperative heat exchanger H1, then the second decompressor E2 is entered, natural gas after expansion reclaims cold through the Article 3 low-pressure channel of the 3rd Recuperative heat exchanger H3 and the Article 4 low-pressure channel of the first Recuperative heat exchanger H1 successively, finally enters natural gas low pressure pipeline.
System in the present embodiment 4, under gas source condition in the same manner as in Example 1, can produce 321Nm
3the LNG of/h, liquefied fraction is 18.8%.Equally, compare in embodiment 1, liquefied fraction is higher, and pressure energy recovering effect is better, but owing to adopting two decompressor and double-compressor, system relative complex.
Claims (10)
1. utilize pipeline pressure can produce a liquefaction system of LNG, it comprises:
The first class purification device (P1) be connected is exported with gas pipeline pressure piping, described first class purification device (P1) export pipeline installs the first distributing valve (T1), and described first class purification device (P1) export pipeline is divided into first paragraph liquefaction branch road (M01) and the first precooling branch road (M1) two-way through this first distributing valve (T1); Described first paragraph liquefaction branch road (M01) is the first compressor (C1) and the first cooler (D1) that are connected to the first distributing valve (T1) successively;
Be connected to the second cleaner (P2) on described first cooler (D1) export pipeline, described second cleaner (P2) export pipeline is installed the second distributing valve (T2), described second cleaner (P2) export pipeline is through this second distributing valve (T2) point two pipelines, and this two pipeline is second segment liquefaction branch road (M02) and main cold branch road (M2); Described second segment liquefaction branch road (M02) is the high-pressure channel of the first Recuperative heat exchanger (H1) being connected to the second distributing valve (T2) successively, the high-pressure channel of the second Recuperative heat exchanger (H2), first throttle bloating plant (V1) and gas-liquid separator (S1); The cold branch road of described master (M2) is the high-pressure channel of the first Recuperative heat exchanger (H1) being connected to the second distributing valve (T2) successively, the high-pressure channel of the second Recuperative heat exchanger (H2), the second throttling bloating plant (V2), the low-pressure channel of the second Recuperative heat exchanger (H2), the low-pressure channel of the first Recuperative heat exchanger (H2) and the low pressure pipeline of gas pipeline;
Described gas-liquid separator (S1) bottom end outlet is LNG product outlet, and gas-liquid separator (S1) top exports the low-pressure channel, the low-pressure channel of the first Recuperative heat exchanger (H1) and the low pressure pipeline of gas pipeline that connect the second Recuperative heat exchanger (H2) successively;
First precooling branch road (M1) is for being connected to first decompressor (E1) of the first distributing valve (T1), and this first decompressor (E1) connects the low-pressure channel of the first Recuperative heat exchanger (H1) and the low pressure pipeline of gas pipeline successively; The work done during compression of described first compressor (C1) is from the expansion work of the first decompressor (E1).
2. according to the liquefaction system utilizing pipeline pressure can produce LNG according to claim 1, it is characterized in that, described first throttle bloating plant (V1) is choke valve.
3. according to the liquefaction system utilizing pipeline pressure can produce LNG according to claim 1, it is characterized in that, also comprise the second compressor (C2) and the second cooler (D2), described second throttling bloating plant (V2) is the second decompressor (E2); Described second compressor (C2) and the second cooler (D2) to be connected between the second distributing valve (T2) and described first Recuperative heat exchanger (H1) high-pressure channel on pipeline successively; The work done during compression of described second compressor (C2) is from the expansion work of the second decompressor (E2).
4. according to the liquefaction system utilizing pipeline pressure can produce LNG according to claim 1, it is characterized in that, described first cooler (D1) is water-cooling cooler or air-cooled cooler; Cooler outlet natural gas temperature is 10 ~ 40 DEG C.
5. according to the liquefaction system utilizing pipeline pressure can produce LNG according to claim 3, it is characterized in that, described second cooler (D2) is water-cooling cooler or air-cooled cooler; Cooler outlet natural gas temperature is 10 ~ 40 DEG C.
6. utilize pipeline pressure can produce a liquefaction system of LNG, it comprises:
The first class purification device (P1) be connected is exported with gas pipeline pressure piping, described first class purification device (P1) export pipeline installs the first distributing valve (T1), and described first class purification device (P1) export pipeline is divided into first paragraph liquefaction branch road (M01) and the first precooling branch road (M1) two-way through the first distributing valve (T1); Described first paragraph liquefaction branch road (M01) is the first compressor (C1) and the first cooler (D1) that are connected to the first distributing valve (T1) successively;
Be connected to the second cleaner (P2) on described first cooler (D1) export pipeline, described second cleaner (P2) is connected with the high-pressure channel of the first Recuperative heat exchanger (H1); The high-pressure channel export pipeline of the first Recuperative heat exchanger (H1) installs the second distributing valve (T2), and the high-pressure channel export pipeline of described first Recuperative heat exchanger (H1) is divided into second segment liquefaction branch road (M02) and main cold branch road (M2) two-way through this second distributing valve (T2); Described second segment liquefaction branch road (M02) is the high-pressure channel of the second Recuperative heat exchanger (H2) being connected to the second distributing valve (T2) successively, first throttle bloating plant (V1) and gas-liquid separator (S1); The cold branch road of described master (M2) is the high-pressure channel of the second Recuperative heat exchanger (H2) being connected to the second distributing valve (T2) successively, the second throttling bloating plant (V2), the low-pressure channel of the second Recuperative heat exchanger (H2), the low-pressure channel of the first Recuperative heat exchanger (H2) and the low pressure pipeline of gas pipeline;
Described gas-liquid separator (S1) bottom end outlet is LNG product outlet, and gas-liquid separator (S1) top exports the low-pressure channel, the low-pressure channel of the first Recuperative heat exchanger (H1) and the low pressure pipeline of gas pipeline that connect the second Recuperative heat exchanger (H2) successively;
First precooling branch road (M1) is for being connected to first decompressor (E1) of the first distributing valve (T1), and this first decompressor (E1) connects the low-pressure channel of the first Recuperative heat exchanger (H1) and the low pressure pipeline of gas pipeline successively; Described first decompressor (E1) provides driving force for described first compressor (C1).
7. according to the liquefaction system utilizing pipeline pressure can produce LNG according to claim 6, it is characterized in that, also comprise the 3rd Recuperative heat exchanger (H3), the second compressor (C2), the second cooler (D2) and the second precooling branch road (M3); First throttle bloating plant (V1) in described second segment liquefaction branch road (M02) is choke valve; Second throttling bloating plant (V2) of the cold branch road of described master (M2) is the second decompressor (E2);
Described 3rd Recuperative heat exchanger (H3) is arranged between described first Recuperative heat exchanger (H1) and the second Recuperative heat exchanger (H2); Connecting line between second cleaner (P2) and the second compressor (C2) is provided with the 3rd distributing valve (T3), 3rd distributing valve (T3) is divided into two pipelines, and this two pipeline is the 3rd section of liquefaction branch road (M03) and the second precooling branch road (M3);
Described second compressor (C2) and the second cooler (D2) are connected between the 3rd distributing valve (T3) and the high-pressure channel of the first Recuperative heat exchanger (H1) successively;
3rd section of liquefaction branch road (M03) is be connected to the second compressor (C2), the second cooler (D2), the high-pressure channel of the first Recuperative heat exchanger (H1) and the high-pressure channel of the 3rd Recuperative heat exchanger (H3) between the 3rd distributing valve (T3) and the second distributing valve (T2) on connecting line successively; The high-pressure channel outlet of described 3rd Recuperative heat exchanger (H3) is connected with described second distributing valve (T2);
Described precooling branch road (M3) is the high-pressure channel of the first Recuperative heat exchanger (H1) being connected to the 3rd distributing valve (T3) successively, the second decompressor (E2), the low-pressure channel of the 3rd Recuperative heat exchanger (H3), the low-pressure channel of the first Recuperative heat exchanger (H1) and the low pressure pipeline of gas pipeline; The work done during compression of described second compressor (C2) is from the expansion work of the second decompressor (E2).
8. according to the liquefaction system utilizing pipeline pressure can produce LNG according to claim 6, it is characterized in that, described first cooler (D1) is water-cooling cooler or air-cooled cooler; Cooler outlet natural gas temperature is 10 ~ 40 DEG C.
9. according to the liquefaction system utilizing pipeline pressure can produce LNG according to claim 7, it is characterized in that, described second cooler (D2) is water-cooling cooler or air-cooled cooler; Cooler outlet natural gas temperature is 10 ~ 40 DEG C.
10. according to the liquefaction system utilizing pipeline pressure can produce LNG according to claim 6, it is characterized in that, described first throttle bloating plant (V1) is choke valve.
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| CN103398545B (en) * | 2013-07-29 | 2015-06-10 | 中国科学院理化技术研究所 | System for producing liquefied natural gas by multistage compression and throttling of feed gas |
| CN103983084A (en) * | 2014-05-03 | 2014-08-13 | 宁波鲍斯能源装备股份有限公司 | Natural gas pressure energy comprehensive utilization complete equipment |
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| US10281203B2 (en) | 2016-08-05 | 2019-05-07 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for liquefaction of industrial gas by integration of methanol plant and air separation unit |
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