CN105783420A - Double-refrigerant circulating natural gas liquefaction system based on wound-tube heat exchanger - Google Patents
Double-refrigerant circulating natural gas liquefaction system based on wound-tube heat exchanger Download PDFInfo
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- CN105783420A CN105783420A CN201610223836.7A CN201610223836A CN105783420A CN 105783420 A CN105783420 A CN 105783420A CN 201610223836 A CN201610223836 A CN 201610223836A CN 105783420 A CN105783420 A CN 105783420A
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 136
- 239000003345 natural gas Substances 0.000 title claims abstract description 66
- 239000003507 refrigerant Substances 0.000 title claims abstract description 26
- 238000001816 cooling Methods 0.000 claims abstract description 124
- 239000007788 liquid Substances 0.000 claims abstract description 42
- 230000006835 compression Effects 0.000 claims abstract description 34
- 238000007906 compression Methods 0.000 claims abstract description 34
- 239000007789 gas Substances 0.000 claims description 56
- 239000012071 phase Substances 0.000 claims description 56
- 239000007791 liquid phase Substances 0.000 claims description 53
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000005188 flotation Methods 0.000 abstract 1
- 230000026676 system process Effects 0.000 abstract 1
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 8
- 238000000034 method Methods 0.000 description 8
- 239000003949 liquefied natural gas Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 230000036772 blood pressure Effects 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 238000000605 extraction Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000001294 propane Substances 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 239000007792 gaseous phase Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 239000000112 cooling gas Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 1
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000008646 thermal stress Effects 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
- F25J1/02—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
- F25J1/0259—Modularity and arrangement of parts of the liquefaction unit and in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
-
- 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
- F25J1/0211—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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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
- F25J1/003—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
- F25J1/0052—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 vaporising a liquid refrigerant stream
- F25J1/0055—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 vaporising a liquid refrigerant stream originating from an incorporated cascade
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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
- F25J1/0211—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0214—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
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 provides a double-refrigerant circulating natural gas liquefaction system based on a wound-tube heat exchanger. The double-refrigerant circulating natural gas liquefaction system is characterized by comprising a precooling level compression module, a precooling level heat exchange module, a copious cooling level compression module and a copious cooling level heat exchange module which are connected, wherein the precooling level compression module comprises buffer tanks, compressors and coolers which are connected in sequence; a precooling refrigerant low-pressure outlet of the precooling level heat exchange module is connected with one of the buffer tanks; a natural gas first-level outlet is connected with a gas-liquid separator; the outlet of one of the coolers is connected with another gas-liquid separator; the copious cooling level compression module comprises buffer tanks, compressors and coolers which are connected in sequence; a copious cooling refrigerant low-pressure outlet of the copious cooling level heat exchange module is connected with one of the buffer tanks of the copious cooling level compression module; a natural gas second-level outlet is connected with the exterior; a natural gas second-level inlet is connected with one of the gas-liquid separators; the outlet of one of the coolers of the copious cooling level compression module is connected with a copious cooling refrigerant first-level inlet; and a copious cooling refrigerant first-level outlet is connected with a gas-liquid separator of the copious cooling level heat exchange module. According to the double-refrigerant circulating natural gas liquefaction system, two-level independent mixed refrigerants circulate and are overlaid, the system process is concise, the structure is compact, the production load operational flexibility is high, the integral machine adopts modularized design, and the system is applicable to offshore flotation natural gas production devices.
Description
Technical field
The present invention relates to a kind of natural gas liquefaction system, circulate natural gas liquefaction system especially with regard to a kind of two refrigerants based on wrap-round tubular heat exchanger.
Background technology
Gaseous natural gas under normal pressure after treatment is cooled to-162 DEG C by LNG (LiquefiedNaturalGas, liquefied natural gas), so as to condense into liquid.The liquid volume of LNG is about the 1/600 of its gaseous volume, is greatly saved storage and transportation space and cost, and has that calorific value is big, performance high, and therefore LNG is a kind of cleaning, the efficient energy.
Natural gas liquefaction flow process mainly includes three kinds: Cascade, mix refrigerant liquefaction flow path and the liquefaction flow path with decompressor.Wherein, Cascade unit is excessively complicated, and cost of investment is high, is mainly used in the Basicloadtype liquefaction plant of early stage；Liquefaction flow path with decompressor has the advantages such as cost of investment is low, flow process is simple, but system power dissipation is big, liquefied fraction is low, is therefore only applicable to small-scaled natural gas liquification device；And mix refrigerant liquefaction flow path, in power consumption, liquefied fraction, system complexity and adaptability, relatively first two liquefaction process has obvious advantage, is particularly suitable for large-scale natural gas liquefaction device.The Basicloadtype natural gas liquefaction device of current more than 80% adopts propane pre-cooling mix refrigerant liquefaction flow path.The main cryogenic heat exchanger of this liquefaction flow path adopts wrap-round tubular heat exchanger, and single line maximum loadability is up to 5,000,000 tons/year.In order to improve production capacity, after propane pre-cooling mix refrigerant liquefaction flow path has been improved, after wound tube heat exchanger, add an independent Guan Bi nitrogen swell refrigeration circulation, make single line production capacity reach 9,000,000 tons/year.Although the type natural gas liquefaction process production capacity is higher, but system flow is excessively complicated, equipment size is huge and the cost of investment of needs is high, therefore cannot meet offshore production operating mode preferably.
Summary of the invention
For the problems referred to above, it is an object of the invention to provide the two refrigerants based on wrap-round tubular heat exchanger that a kind of cost of investment is low and system flow is simplified and circulate natural gas liquefaction system.
For achieving the above object, the present invention takes techniques below scheme: a kind of two refrigerants based on wrap-round tubular heat exchanger circulates natural gas liquefaction system, it is characterised in that: it includes the pre-cooling level compression module, pre-cooling level heat exchange module, deep cooling level compression module and the deep cooling level heat exchange module that are connected by pipeline；Described pre-cooling level compression module includes the first surge tank, the first compressor and the first cooler that least one set is sequentially connected with by pipeline；Described pre-cooling level heat exchange module includes one first main cryogenic heat exchanger, and described first main cryogenic heat exchanger is provided with a natural gas one-level entrance, a natural gas primary outlet, one first liquid phase cryogen entrance, one first gas phase cryogen entrance, a pre-cooling cryogen low tension outlet, a deep cooling cryogen one-level entrance and a deep cooling cryogen primary outlet；Described pre-cooling cryogen low tension outlet is connected with described first surge tank by pipeline, and described first liquid phase cryogen entrance and described first gas phase cryogen entrance are connected with one first gas-liquid separator respectively；Described natural gas primary outlet is connected by pipeline and one second gas-liquid separator；The outlet of described first cooler is connected with described first gas-liquid separator by pipeline；Described deep cooling level compression module includes the second surge tank, the second compressor and the second cooler that least one set is sequentially connected with by pipeline；Described deep cooling level heat exchange module includes one second main cryogenic heat exchanger, and described second main cryogenic heat exchanger is provided with a natural gas secondary inlet, a natural gas secondary exit port, a second liquid phase cryogen entrance, one second gas phase cryogen entrance and a deep cooling cryogen low tension outlet；Described deep cooling cryogen low tension outlet is connected with described second surge tank by pipeline, and described second liquid phase cryogen entrance and described second gas phase cryogen entrance are connected with one the 3rd gas-liquid separator respectively；Described natural gas secondary exit port is by pipeline and choke valve and external connection；Described natural gas secondary inlet is connected with described second gas-liquid separator by pipeline；The outlet of described second cooler is connected with described deep cooling cryogen one-level entrance by pipeline；Described deep cooling cryogen primary outlet is connected with described 3rd gas-liquid separator by pipeline.
Described first main cryogenic heat exchanger is additionally provided with one first outlet of liquid phase cryogen and one first liquid phase cryogen low-pressure inlet；Described first liquid phase cryogen outlet is connected with described first liquid phase cryogen low-pressure inlet by pipeline and choke valve, is used for making liquid phase cryogen decrease temperature and pressure.
Described first main cryogenic heat exchanger is additionally provided with one first outlet of gas phase cryogen and one first gas phase cryogen low-pressure inlet；Described first gas phase cryogen outlet is connected with described first gas phase cryogen low-pressure inlet by pipeline and choke valve, is used for making gas phase cryogen decrease temperature and pressure.
Described second main cryogenic heat exchanger is additionally provided with the outlet of second liquid phase cryogen and a second liquid phase cryogen low-pressure inlet；The outlet of described second liquid phase cryogen is connected with described second liquid phase cryogen low-pressure inlet by pipeline and choke valve, is used for making liquid phase cryogen decrease temperature and pressure.
Described second main cryogenic heat exchanger is additionally provided with one second outlet of gas phase cryogen and one second gas phase cryogen low-pressure inlet；Described second gas phase cryogen outlet is connected with described second gas phase cryogen low-pressure inlet by pipeline and choke valve, is used for making gas phase cryogen decrease temperature and pressure.
Described first main cryogenic heat exchanger and described second main cryogenic heat exchanger all adopt wrap-round tubular heat exchanger.
Described first compressor and described second compressor adopt one of piston compressor, helical-lobe compressor and centrifugal compressor.
Described choke valve adopts J-T valve.
Due to the fact that and take above technical scheme, it has the advantage that 1, due to the fact that and be provided with the pre-cooling level compression module that pipeline connects, pre-cooling level heat exchange module, deep cooling level compression module and deep cooling level heat exchange module, therefore pre-cooling level compression module can provide power source for pre-cooling level heat exchange module, natural gas and deep cooling cryogen can be carried out pre-cooling by pre-cooling level heat exchange module, deep cooling level compression module can provide power source for deep cooling level heat exchange module, and natural gas can be carried out low-temperature liquefaction by deep cooling level heat exchange module, and then complete natural gas liquefaction work.2, the first of the present invention the main cryogenic heat exchanger and the second main cryogenic heat exchanger are owing to adopting wrap-round tubular heat exchanger, therefore have that heat exchange area is big, heat transfer efficiency is high, uniform fluid distribution is good and the advantage such as thermal stress strong adaptability.3, the liquefaction system of the present invention adopts two-stage independence azeotrope to circulate outer overlapping layout, and system flow is simplified, compact conformation, produces load operation elastic big.4, present invention can apply to the various construction of natural gas fields and utilize occasion, due to can first at continental rise place Prefabricated block, job site be made directly and assembles, and therefore greatly reduces engineering construction difficulty and project investment cost.The present invention is relatively applicable to the floating natural gas liquefaction process units of the single-row production line L NG yield middle-size and small-size continental rise natural gas liquefaction plant more than 1,000,000 tons/year or more than 300,000 tons/year.
Accompanying drawing explanation
Fig. 1 is the overall structure schematic diagram of liquefaction system of the present invention；
Fig. 2 is the modular construction schematic diagram of the present invention；
Fig. 3 is the structural representation of the pre-cooling level compression module of the present invention；
Fig. 4 is the structural representation of the pre-cooling level heat exchange module of the present invention；
Fig. 5 is the structural representation of the deep cooling level compression module of the present invention；
Fig. 6 is the structural representation of the deep cooling level heat exchange module of the present invention.
Detailed description of the invention
Below in conjunction with drawings and Examples, the present invention is described in detail.
As shown in Figure 1 and Figure 2, the present invention includes the pre-cooling level compression module 1, pre-cooling level heat exchange module 2, deep cooling level compression module 3 and the deep cooling level heat exchange module 4 that are connected by pipeline.
As it is shown on figure 3, pre-cooling level compression module 1 includes the surge tank 5, compressor 6, cooler 7, surge tank 8, compressor 9 and the cooler 10 that are sequentially connected with by pipeline.
As shown in Figure 4, pre-cooling level heat exchange module 2 includes a main cryogenic heat exchanger 11, and main cryogenic heat exchanger 11 is provided with natural gas one-level entrance 12, natural gas primary outlet 13, liquid phase cryogen entrance 14, liquid phase cryogen outlet 15, gas phase cryogen entrance 16, gas phase cryogen outlet 17, one liquid phase cryogen low-pressure inlet 18, gas phase cryogen low-pressure inlet 19, pre-cooling cryogen low tension outlet 20, deep cooling cryogen one-level entrance 21, deep cooling cryogen primary outlet 22.Wherein, pre-cooling cryogen low tension outlet 20 is connected with surge tank 5 by pipeline, and liquid phase cryogen entrance 14 is connected by the liquid-phase outlet of pipeline and a gas-liquid separator 23, and gas phase cryogen entrance 16 is connected with the gaseous phase outlet of gas-liquid separator 23.Liquid phase cryogen outlet 15 is connected with liquid phase cryogen low-pressure inlet 18 by pipeline and choke valve.Gas phase cryogen outlet 17 is connected with gas phase cryogen low-pressure inlet 19 by pipeline and choke valve.Natural gas primary outlet 13 is connected by the entrance of pipeline and a gas-liquid separator 26.The outlet of cooler 10 is connected by the entrance of pipeline with gas-liquid separator 23.
As it is shown in figure 5, deep cooling level compression module 3 includes the surge tank 27, compressor 28, cooler 29, surge tank 30, compressor 31 and the cooler 32 that are sequentially connected with by pipeline.
As shown in Figure 6, deep cooling level heat exchange module 4 includes a main cryogenic heat exchanger 33, and main cryogenic heat exchanger 33 is provided with natural gas secondary inlet 34, natural gas secondary exit port 35, liquid phase cryogen entrance 36, liquid phase cryogen outlet 37, gas phase cryogen entrance 38, gas phase cryogen outlet 39, one liquid phase cryogen low-pressure inlet 40, gas phase cryogen low-pressure inlet 41, deep cooling cryogen low tension outlet 42.Wherein, deep cooling cryogen low tension outlet 42 is connected with surge tank 27 by pipeline, and liquid phase cryogen entrance 36 is connected by the liquid-phase outlet of pipeline and a gas-liquid separator 43, and gas phase cryogen entrance 38 is connected with the gaseous phase outlet of gas-liquid separator 43 by pipeline.Liquid phase cryogen outlet 37 is connected with liquid phase cryogen low-pressure inlet 40 by pipeline and choke valve.Gas phase cryogen outlet 39 is connected with gas phase cryogen low-pressure inlet 41 by pipeline and choke valve.Natural gas secondary exit port 35 is by pipeline and choke valve and external connection.Natural gas secondary inlet 34 is connected with the gaseous phase outlet of gas-liquid separator 26 by pipeline.The outlet of cooler 32 is connected with deep cooling cryogen one-level entrance 21 by pipeline.Deep cooling cryogen primary outlet 22 is connected with the entrance of gas-liquid separator 43 by pipeline.
In above-described embodiment, main cryogenic heat exchanger 11 and main cryogenic heat exchanger 33 all adopt wrap-round tubular heat exchanger.
In above-described embodiment, compressor 6, compressor 9, compressor 28 and compressor 31 can adopt piston compressor or helical-lobe compressor or centrifugal compressor.
In above-described embodiment, choke valve adopts J-T valve (Joule-Thomson throttle expansion valve).
The present invention is operationally, enter the low pressure pre-cooling azeotrope in pre-cooling level compression module 1, after the gas-liquid separation of buffered tank 5, compressor 6 one stage of compression, cooler 7 cooling, after buffered tank 8 gas-liquid separation again, compressor 9 two-stage compression, cooler 10 cooling, enter the gas-liquid separator 23 in pre-cooling level heat exchange module 2.Gas-liquid separator 23 separating obtained liquid phase cryogen enters main cryogenic heat exchanger 11 through liquid phase cryogen entrance 14,15 extractions are exported from liquid phase cryogen, after choke valve throttling, blood pressure lowering and cooling, enter main cryogenic heat exchanger 11 shell-side space through liquid phase cryogen low-pressure inlet 18, provide cold for natural gas, deep cooling cryogen, pre-cooling gas phase cryogen.Gas-liquid separator 23 separating obtained gas phase cryogen enters main cryogenic heat exchanger 11 through gas phase cryogen entrance 16,17 extractions are exported from gas phase cryogen, after choke valve throttling, blood pressure lowering and cooling, enter main cryogenic heat exchanger 11 shell-side space through gas phase cryogen low-pressure inlet 19, provide cold for natural gas, deep cooling cryogen；Pre-cooling azeotrope is finally drawn by pre-cooling cryogen low tension outlet 20, enters pre-cooling level compression module 1, completes a pre-cooling cycle.
nullEnter the low pressure deep cooling azeotrope in deep cooling level compression module 3，The gas-liquid separation of buffered tank 27、Compressor 28 one stage of compression、After cooler 29 cooling，Buffered tank 30 gas-liquid separation again、Compressor 31 two-stage compression、After cooler 32 cooling，The main cryogenic heat exchanger 11 of pre-cooling level heat exchange module 2 is entered through deep cooling cryogen one-level entrance 21，Draw from deep cooling cryogen primary outlet 22 after being cooled down by pre-cooling refrigerant cycle，Enter the gas-liquid separator 43 in deep cooling level heat exchange module 4，Gas-liquid separator 43 separating obtained liquid phase cryogen enters main cryogenic heat exchanger 33 through liquid phase cryogen entrance 36，37 extractions are exported from liquid phase cryogen，Throttled by choke valve、After blood pressure lowering and cooling，Main cryogenic heat exchanger 33 shell-side space is entered through liquid phase cryogen low-pressure inlet 40，For natural gas、Deep cooling gas phase cryogen provides cold.Gas-liquid separator 43 separating obtained gas phase cryogen enters main cryogenic heat exchanger 33 through gas phase cryogen entrance 38,39 extractions are exported from gas phase cryogen, after choke valve throttling, blood pressure lowering and cooling, enter main cryogenic heat exchanger 33 shell-side space through gas phase cryogen low-pressure inlet 41, provide cold for natural gas liquefaction.Deep cooling azeotrope is finally drawn by deep cooling cryogen low tension outlet 42, enters deep cooling level compression module 3, completes a deep cooling circulation.
Natural gas via natural gas one-level entrance 12 after purified treatment accesses the main cryogenic heat exchanger 11 of pre-cooling level heat exchange module 2, after being cooled down by pre-cooling cryogen, draws from natural gas primary outlet 13, enters gas-liquid separator 26；The separating obtained liquid phase lime set of gas-liquid separator 26 is picked out by bottom and causes the external world, gained gas phase natural gas via natural gas secondary inlet 34 enters the main cryogenic heat exchanger 33 of deep cooling level heat exchange module 4, draw from natural gas secondary exit port 35, by choke valve throttling, blood pressure lowering, the LNG of production is caused extraneous storage.
Below by a specific embodiment, further illustrate the technique effect of the present invention.
Embodiment
Adopt liquefaction system provided by the invention that certain offshore gas field is developed and utilized, first (temperature is 45.0 DEG C to the raw natural gas after purified treatment, pressure is 4.0MPaA) introduce main cryogenic heat exchanger 11 and carry out pre-cooling, it is cooled to-50 DEG C by pre-cooling azeotrope, enter gas-liquid separator 26 and carry out gas-liquid separation, separating obtained lime set is picked out by separator bottom and causes the external world, separating obtained gas phase natural gas enters main cryogenic heat exchanger 33 and carries out low-temperature liquefaction, it is cooled to-153 DEG C by deep cooling azeotrope, throttle through choke valve, it is depressurized to 0.2MPaA, the LNG produced is drawn to extraneous storage.
Carry out the low pressure pre-cooling azeotrope (temperature be 19.0 DEG C, pressure be 0.21MPaA) of autonomous cryogenic heat exchanger 11, it is compressed to 3.5MPaA successively through compressor 6 and compressor 9, the cooled device 7 of high pressure-temperature gas phase azeotrope after compression, cooler 10 are cooled to 25.0 DEG C, main cryogenic heat exchanger 11 is respectively enterd after gas-liquid separator 23 separates, after separating obtained liquid phase pre-cooling cryogen is cooled to-21 DEG C, after choke valve reducing pressure by regulating flow to 0.23MPaA, it is back to main cryogenic heat exchanger 11 shell-side space, provides cold for tube side fluid；After separating obtained gas phase pre-cooling cryogen continues to be cooled to-50 DEG C, main cryogenic heat exchanger 11 shell-side space it is back to after choke valve reducing pressure by regulating flow to 0.24MPaA, cold is provided for tube side fluid, low pressure pre-cooling azeotrope after final heat exchange enters compressor 6 and compresses entrance, completes a pre-cooling cycle.
(temperature is 0 DEG C to the low pressure deep cooling azeotrope of next autonomous cryogenic heat exchanger 33, pressure is 0.24MPaA), successively through compressor 28, compressor 31 is compressed to 4.0MPaA, the cooled device 29 of high pressure-temperature gas phase azeotrope after compression, cooler 32 is cooled to 25.0 DEG C, enter main cryogenic heat exchanger 11 and carry out pre-cooling, after being cooled to-50 DEG C by pre-cooling azeotrope, main cryogenic heat exchanger 33 is respectively enterd after gas-liquid separator 43 separates, after separating obtained liquid phase deep cooling cryogen is cooled to-110 DEG C, main cryogenic heat exchanger 33 shell-side space it is back to after choke valve reducing pressure by regulating flow to 0.28MPaA, cold is provided for tube side fluid.After separating obtained gas phase deep cooling cryogen continues to be cooled to-153 DEG C, main cryogenic heat exchanger 33 shell-side space it is back to after choke valve reducing pressure by regulating flow to 0.30MPaA, thering is provided cold for tube side fluid, the deep cooling azeotrope after final heat exchange enters compressor 28 and compresses entrance, completes a deep cooling circulation.
Wherein, the feed gas molar after process consists of: 1.0% nitrogen+97.0% methane+2.0% ethane；The molar constituent of the pre-cooling azeotrope adopted is: 48.32% ethane+16.43% propane+35.25% isopentane；The molar constituent of the deep cooling azeotrope adopted is: 4.43 nitrogen %+48.60% methane+37.26% ethane+9.72% propane.
The various embodiments described above are merely to illustrate the present invention, and wherein the structure of each parts, connected mode etc. all can be varied from, every equivalents carried out on the basis of technical solution of the present invention and improvement, all should not get rid of outside protection scope of the present invention.
Claims (8)
1. the two refrigerants based on wrap-round tubular heat exchanger circulates natural gas liquefaction system, it is characterised in that: it includes the pre-cooling level compression module, pre-cooling level heat exchange module, deep cooling level compression module and the deep cooling level heat exchange module that are connected by pipeline；
Described pre-cooling level compression module includes the first surge tank, the first compressor and the first cooler that least one set is sequentially connected with by pipeline；
Described pre-cooling level heat exchange module includes one first main cryogenic heat exchanger, and described first main cryogenic heat exchanger is provided with a natural gas one-level entrance, a natural gas primary outlet, one first liquid phase cryogen entrance, one first gas phase cryogen entrance, a pre-cooling cryogen low tension outlet, a deep cooling cryogen one-level entrance and a deep cooling cryogen primary outlet；Described pre-cooling cryogen low tension outlet is connected with described first surge tank by pipeline, and described first liquid phase cryogen entrance and described first gas phase cryogen entrance are connected with one first gas-liquid separator respectively；Described natural gas primary outlet is connected by pipeline and one second gas-liquid separator；The outlet of described first cooler is connected with described first gas-liquid separator by pipeline；
Described deep cooling level compression module includes the second surge tank, the second compressor and the second cooler that least one set is sequentially connected with by pipeline；
Described deep cooling level heat exchange module includes one second main cryogenic heat exchanger, and described second main cryogenic heat exchanger is provided with a natural gas secondary inlet, a natural gas secondary exit port, a second liquid phase cryogen entrance, one second gas phase cryogen entrance and a deep cooling cryogen low tension outlet；Described deep cooling cryogen low tension outlet is connected with described second surge tank by pipeline, and described second liquid phase cryogen entrance and described second gas phase cryogen entrance are connected with one the 3rd gas-liquid separator respectively；Described natural gas secondary exit port is by pipeline and choke valve and external connection；Described natural gas secondary inlet is connected with described second gas-liquid separator by pipeline；The outlet of described second cooler is connected with described deep cooling cryogen one-level entrance by pipeline；Described deep cooling cryogen primary outlet is connected with described 3rd gas-liquid separator by pipeline.
2. a kind of two refrigerants based on wrap-round tubular heat exchanger circulates natural gas liquefaction system as claimed in claim 1, it is characterised in that: described first main cryogenic heat exchanger is additionally provided with one first outlet of liquid phase cryogen and one first liquid phase cryogen low-pressure inlet；Described first liquid phase cryogen outlet is connected with described first liquid phase cryogen low-pressure inlet by pipeline and choke valve, is used for making liquid phase cryogen decrease temperature and pressure.
3. a kind of two refrigerants based on wrap-round tubular heat exchanger circulates natural gas liquefaction system as claimed in claim 1, it is characterised in that: described first main cryogenic heat exchanger is additionally provided with one first outlet of gas phase cryogen and one first gas phase cryogen low-pressure inlet；Described first gas phase cryogen outlet is connected with described first gas phase cryogen low-pressure inlet by pipeline and choke valve, is used for making gas phase cryogen decrease temperature and pressure.
4. a kind of two refrigerants based on wrap-round tubular heat exchanger circulates natural gas liquefaction system as claimed in claim 1, it is characterised in that: described second main cryogenic heat exchanger is additionally provided with the outlet of second liquid phase cryogen and a second liquid phase cryogen low-pressure inlet；The outlet of described second liquid phase cryogen is connected with described second liquid phase cryogen low-pressure inlet by pipeline and choke valve, is used for making liquid phase cryogen decrease temperature and pressure.
5. a kind of two refrigerants based on wrap-round tubular heat exchanger circulates natural gas liquefaction system as claimed in claim 1, it is characterised in that: described second main cryogenic heat exchanger is additionally provided with one second outlet of gas phase cryogen and one second gas phase cryogen low-pressure inlet；Described second gas phase cryogen outlet is connected with described second gas phase cryogen low-pressure inlet by pipeline and choke valve, is used for making gas phase cryogen decrease temperature and pressure.
6. a kind of two refrigerants based on wrap-round tubular heat exchanger circulates natural gas liquefaction system as claimed in claim 1, it is characterised in that: described first main cryogenic heat exchanger and described second main cryogenic heat exchanger all adopt wrap-round tubular heat exchanger.
7. a kind of two refrigerants based on wrap-round tubular heat exchanger circulates natural gas liquefaction system as claimed in claim 1, it is characterised in that: described first compressor and described second compressor adopt one of piston compressor, helical-lobe compressor and centrifugal compressor.
8. a kind of two refrigerants based on wrap-round tubular heat exchanger circulates natural gas liquefaction system as claimed in claim 1, it is characterised in that: described choke valve adopts J-T valve.
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| CN108775770A (en) * | 2018-05-30 | 2018-11-09 | 科霖恩新能源科技（江苏）有限公司 | A kind of brazing plate type heat exchanger natural gas liquefaction system using mixed-refrigerant cycle |
| CN110044131A (en) * | 2019-05-06 | 2019-07-23 | 郑州轻工业学院 | A kind of multi-stage compression propane pre-cooling natural gas liquefaction system and its liquifying method |
| CN110411145A (en) * | 2018-04-27 | 2019-11-05 | 气体产品与化学公司 | For using the improved method and system of the cooling hydrocarbon stream of vapor phase refrigerant |
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| CN115371355A (en) * | 2022-08-16 | 2022-11-22 | 中海石油气电集团有限责任公司 | Natural gas liquefaction system and method suitable for standard modularization |
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Address after: 100010 Chaoyangmen North Street, Dongcheng District, Dongcheng District, Beijing Applicant after: China Offshore Oil Group Co., Ltd. Applicant after: CNOOC Gas & Power Group Address before: 100010 Chaoyangmen North Street, Dongcheng District, Dongcheng District, Beijing Applicant before: China National Offshore Oil Corporation Applicant before: CNOOC Gas & Power Group |
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Application publication date: 20160720 |