CN101338964B - Natural gas liquefaction device and liquefaction flow path - Google Patents
Natural gas liquefaction device and liquefaction flow path Download PDFInfo
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- CN101338964B CN101338964B CN2008100225118A CN200810022511A CN101338964B CN 101338964 B CN101338964 B CN 101338964B CN 2008100225118 A CN2008100225118 A CN 2008100225118A CN 200810022511 A CN200810022511 A CN 200810022511A CN 101338964 B CN101338964 B CN 101338964B
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 160
- 239000003345 natural gas Substances 0.000 title claims abstract description 80
- 239000007788 liquid Substances 0.000 claims abstract description 52
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 35
- 238000000034 method Methods 0.000 claims abstract description 30
- 230000008569 process Effects 0.000 claims abstract description 26
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 27
- 239000006096 absorbing agent Substances 0.000 claims description 21
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 20
- 239000004215 Carbon black (E152) Substances 0.000 claims description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 10
- 229930195733 hydrocarbon Natural products 0.000 claims description 10
- 150000002430 hydrocarbons Chemical class 0.000 claims description 10
- 239000001569 carbon dioxide Substances 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 5
- 239000003463 adsorbent Substances 0.000 claims description 3
- 230000007420 reactivation Effects 0.000 claims description 3
- 238000005057 refrigeration Methods 0.000 abstract description 18
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000002203 pretreatment Methods 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 17
- 238000005516 engineering process Methods 0.000 description 7
- 239000000446 fuel Substances 0.000 description 5
- 241000196324 Embryophyta Species 0.000 description 3
- 230000018109 developmental process Effects 0.000 description 3
- 239000002283 diesel fuel Substances 0.000 description 3
- 239000003502 gasoline Substances 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 235000019628 coolness Nutrition 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 241000183024 Populus tremula Species 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
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- 239000003921 oil Substances 0.000 description 1
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- 238000003825 pressing Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Images
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
- F25J1/02—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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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 natural gas liquefying plant and a liquefying process thereof. The liquefying plant comprises a pre-treatment system, a liquefying system and a storing system which are mutually connected with each other through pipelines; the natural gas filtered by the pre-treatment system enters into a primary heat exchanger, a first a gas-liquid separator, a cooler and a second gas-liquid separator sequentially, and then is modified into liquefied natural gas. The liquefying system of the plant adopts secondary throttle, which reduces throttling pressure drop, reduces the cold terminal temperature difference of the primary heat exchanger, reduces the loss of refrigeration and increases liquefying rate. The liquefying plant ensures that partial vapor generated in the throttlingtemperature reduction of high-pressure natural gas exchanges heat with a plurality of medium at regions with different temperatures, which fully uses the low-temperature refrigeration of the flashed vapor, greatly reduces the energy consumption of the plant, and increases the liquefying rate. Besides, the liquefying plant is simple in technical process with fewer devices.
Description
Technical field
The present invention relates to the compression and the liquefaction of gas, relate more specifically to by the device and the flow process of swell refrigeration with natural gas liquefaction.
Background technology
Natural gas is a kind of known substitute of fuel such as gasoline and diesel oil.People development of natural gas as an alternative fuel to overcome gasoline and diesel oil and comprise production cost and to use and to have made a lot of effort aspect the various shortcomings such as back discharging.Natural gas known in the art is a kind of fuel that more cleans than other fuel, and is also safer than gasoline or diesel oil, because natural gas can rise in the air and dissipation, rather than sedimentation.In order to be used as alternative fuel, natural gas is converted to compressed natural gas or liquefied natural gas usually, is convenient to store before use and transport.
Current China's economic growth momentum is continuously and healthily still continuing, but for ensureing that economic energy source and power is but extremely in short supply.Under the situation that the international petroleum price raises successively, the energy crisis of China seems serious all the more.The energy resource structure of China is based on coal, and oil, natural gas only account for very little ratio, well below world average level.Along with the continuous growth of country to energy demand, liquefied natural gas product will effectively solve the dual problem of energy supply safety, ecological environmental protection to optimizing the energy resource structure of China, realize that sustainable development economic and society plays a significant role.
" enforcement of West-east Gas " extra large gas disembarkation " engineerings such as " Liquefied Natural Gas Import ", China more and more payes attention to the development of liquefied natural gas industry along with China.As the gas user of one of gas downstream main users, it is very big with gas load fluctuation amount, faces the pressure of source of the gas peak regulation every day.Therefore, each gas enterprise all need throw huge fund and build some peak regulation facilities.At present, the process route of natural gas liquefaction device mainly contains three kinds of stepwise refrigeration process, mixed refrigeration process and swell refrigeration technologies.The required cold of its natural gas liquefaction of stepwise refrigeration process and mixed refrigeration process all is that the kind of refrigeration cycle by cold-producing medium provides, and swell refrigeration technology then is to utilize the pressure of raw natural gas externally to do work required cold is provided.
At present, the natural gas liquefaction technology that a lot of swell refrigerations are arranged both at home and abroad, as U.S. Pat 6023942, US6209350, US6449982, US6378330 etc., but the disclosed technology of these patents all comes with some shortcomings, and is less compliant in city gas receiving gate station or voltage regulating station and uses.For example U.S. Pat 6023942 and US6209350, the natural gas liquefaction flow process of its announcement is complicated, and the investment that needs is also very big; U.S. Pat 6449982 needs the external world to provide cold to cool off unstripped gas in the process of natural gas liquefaction, and operating cost is higher; Cold in the gas deliquescence process that U.S. Pat 6378330 discloses does not make full use of, and has reduced the liquefied fraction of device.
Summary of the invention
The objective of the invention is to solve above-mentioned technical problem, thereby a kind of energy-efficient natural gas liquefaction device and liquefaction flow path that the high-pressure natural gas energy reduces plant energy consumption that make full use of is provided.
Purpose of the present invention is achieved through the following technical solutions:
A kind of natural gas liquefaction device, comprise by the interconnective pretreatment system of pipeline, liquefaction system and stocking system, raw natural gas enters stocking system in order after changing into liquefied natural gas behind pretreatment system and the liquefaction system, described liquefaction system comprises main heat exchanger and the subcooler that is used for heat exchange, be used for first gas-liquid separator and second gas-liquid separator that liquefied natural gas is separated and a decompressor; Enter main heat exchanger in order through the natural gas after the pretreatment system filtration, first gas-liquid separator, subcooler changes into liquefied natural gas behind second gas-liquid separator; The pipeline connection of described decompressor and pretreatment system, its pipeline passes main heat exchanger again, and provides cold for main heat exchanger; Be connected with the first throttle valve on the pipeline between the described main heat exchanger and first gas-liquid separator; Be connected with second choke valve on the pipeline between the described subcooler and second gas-liquid separator.
Further, the flashed vapour that produces in described first gas-liquid separator and second gas-liquid separator enters low-pressure pipe network through behind subcooler and the main heat exchanger in order, and described flashed vapour provides cold for subcooler and main heat exchanger.
Again further, through pressure pipe net in entering behind natural gas process main heat exchanger after the described decompressor expansion and the pretreatment system.
Further, described pretreatment system comprises first absorber of the water, heavy hydrocarbon and the benzene that are used for removing raw natural gas and is used to remove second absorber of carbon dioxide.Natural gas liquefaction device also comprises the heating furnace of the adsorbent reactivation that is used for making first absorber and second absorber, is connected with the pressurized end pipeline of described decompressor.
The present invention has also disclosed the liquefaction flow path of above-mentioned natural gas liquefaction device, may further comprise the steps:
Raw natural gas removes water, heavy hydrocarbon and benzene through first absorber of pretreatment system, and wherein a part enters second absorber again and removes carbon dioxide;
Remove the natural gas behind the carbon dioxide, lower the temperature, natural gas is liquefied fully through behind the main heat exchanger; Only remove the natural gas of water, heavy hydrocarbon and benzene, after cooling behind the main heat exchanger, enter decompressor and expand, for main heat exchanger provides cold;
After the step-down of natural gas after liquefaction process first throttle valve, enter into first gas-liquid separator more fully, this moment, the top of first gas-liquid separator can produce 38% flashed vapour, and the bottom is a liquefied natural gas;
It is cold excessively that liquefied natural gas carries out the degree of depth through described subcooler again;
The degree of depth is crossed liquefied natural gas after cold after the second choke valve step-down, enters into second gas-liquid separator again, and this moment, the top of second gas-liquid separator can produce flashed vapour, and the liquefied natural gas of bottom then enters stocking system.
Further, the flashed vapour that comes out from first gas-liquid separator and second gas-liquid separator separates is through behind the described subcooler, converges through behind the main heat exchanger to enter into low-pressure pipe network.
Again further, the natural gas after entering decompressor and expanding returns in the main heat exchanger after the re-heat, enters the pressurized end supercharging of decompressor again, pressure pipe net in entering after the cooling.
Further, the natural gas after the liquefaction is through behind the first throttle valve fully, and its pressure is reduced to 20 kilograms from every cubic centimetre 50 kilograms; The degree of depth is crossed liquefied natural gas after cold through second choke valve, and its pressure is reduced to 4 kilograms from every cubic centimetre 20 kilograms.
Again further, liquefied natural gas carries out the temperature that the degree of depth crosses after cold through described subcooler and can reduce 7-8 degree centigrade.
Beneficial effect of the present invention is mainly reflected in:
(1) device adopts the circulation of natural gas swell refrigeration, compare with the azeotrope kind of refrigeration cycle with the stepwise kind of refrigeration cycle, flow process has been saved the required expense of the various refrigerants of production, transportation and storage, has also saved complicated refrigeration process, device operates fairly simple, and the starting fluid is fast.
(2) adopt second throttle in the device liquefaction system, reduce choke pressure and fall, the main heat exchanger cold-end temperature difference is reduced, reduce loss of refrigeration capacity, improve liquefied fraction.
(3) in heat exchanger, throttling working medium was carried out cold, make natural gas before throttling, be in supercooled state.
(4) the part flashed vapour that device will produce in the high-pressure natural gas throttling temperature-fall period reasonably, different temperatures interval with multiple medium heat exchange, made full use of the low temperature cold of these flashed vapours, greatly reduce plant energy consumption, improve liquefied fraction.
(5) the natural band of gas of low temperature liquid is pressed and is stored the raising that is beneficial to the device liquefied fraction.
(6) the device technique flow process is simple, and number of devices is few.
(7) moving number of devices is few, has reduced construction investment and operation maintenance expense.
(8) adopt efficient plate-fin heat exchanger, the heat exchange efficiency height, the plant area area is little.
(9) moisture in the unstripped gas, heavy hydrocarbon and sour gas utilize adsorption method of separation.Purification by molecular sieve can guarantee moisture in the unstripped gas less than 1ppm, and the content of CO2 is less than 50ppm.Adopt active carbon purifying, can guarantee that aromatic hydrocarbon content in the unstripped gas is less than 10ppm.Adsorption method of separation not only satisfies the requirement of follow-up chilling process, also makes the purification process of unstripped gas oversimplify.
(10) purification system adopts two group of three tower operation, also reduces regeneration tolerance when guaranteeing the heating furnace continuous operation, thereby improves liquefied fraction.
Description of drawings
Below in conjunction with accompanying drawing technical solution of the present invention is described further:
Fig. 1: the schematic flow sheet of natural gas liquefaction device of the present invention.
Wherein:
1 pretreatment system, 2 liquefaction systems, 3 stocking systems
Pressure pipe net 5 raw natural gas pipe networks 6 low-pressure pipe networks in 4
7 heating furnaces, 11 first absorbers, 12 second absorbers
21 main heat exchanges, 22 subcoolers, 23 first gas-liquid separators
24 second gas-liquid separators, 25 first throttle valves, 26 second choke valves
27 decompressors, 28 pressurized ends, 29 expanding ends
The specific embodiment
Principle of the present invention is the pressure energy that makes full use of natural gas voltage regulating station natural gas self in the pressure regulation process, and use swell refrigeration technology is made liquefied natural gas with a part of natural gas liquefaction in the pipe network and stored.
As shown in Figure 1, natural gas liquefaction device of the present invention comprises by the interconnective pretreatment system 1 of pipeline, liquefaction system 2 and stocking system 3.Described pretreatment system 1 comprises first absorber 11 of the water, heavy hydrocarbon and the benzene that are used for removing raw natural gas and is used to remove second absorber 12 of carbon dioxide.Raw natural gas enters stocking system 3 in order after changing into liquefied natural gas behind pretreatment system 1 and the liquefaction system 2.
Described liquefaction system 2 comprises main heat exchanger 21 and the subcooler 22 that is used for heat exchange, is used for first gas-liquid separator 23 and second gas-liquid separator 24 that liquefied natural gas is separated and a decompressor 27.Enter main heat exchanger 21, the first gas-liquid separators 23 in order through the natural gas after pretreatment system 1 filtration, change into liquefied natural gas behind subcooler 22, the second gas-liquid separators 24.Main heat exchanger 21 of the present invention and subcooler 22 all adopt plate-fin heat exchanger, and with respect to traditional shell-and-tube heat exchanger, the advantage of plate-fin heat exchanger is small and light, and control the temperature difference at an easy rate, and the temperature difference is more little, and energy consumption will be low more, and its efficient also can increase.
The pipeline of described decompressor 27 passes main heat exchanger 21.Before entering decompressor 27, the pressure of natural gas is 50 kilograms every cubic centimetre, is reduced to 10 kilograms every cubic centimetre after expanding through expanding end 29.After natural gas after the described decompressor 27 of process expands enters into main heat exchanger 21, for main heat exchanger 21 provides cold, after the re-heat, enter pressurized end 28 superchargings of decompressor 27 again, pressure pipe net 4 in entering after the cooling.
After natural gas after filtering through pretreatment system 1 enters main heat exchanger 21, with expand after the natural gas heat exchange, make the natural gas cooling after the filtration, finally reach subzero 85 degrees centigrade, this moment, natural gas reached liquid phase, was liquefied fully.
Further, be connected with first throttle valve 25 on the pipeline between the described main heat exchanger 21 and first gas-liquid separator 23; Be connected with second choke valve 26 on the pipeline between the described subcooler 22 and second gas-liquid separator 24.
Through 25 step-downs of first throttle valve, its pressure is reduced to 20 kilograms from every cubic centimetre 50 kilograms through the natural gas after main heat exchanger 21 liquefaction; Enter into first gas-liquid separator 23 again, this moment, the top of first gas-liquid separator 23 can produce 38% flashed vapour, and the bottom is a liquefied natural gas; It is cold excessively that the liquefied natural gas of bottom carries out the degree of depth through described subcooler 22 again, and temperature reduces 7-8 degree centigrade; The degree of depth is crossed liquefied natural gas after cold through 26 step-downs of second choke valve, and its pressure is reduced to 4 kilograms from every cubic centimetre 20 kilograms; Enter into second gas-liquid separator 24 again, this moment, the top of second gas-liquid separator 24 can produce flashed vapour, and the liquefied natural gas of bottom then enters stocking system 3.
The flashed vapour that produces in described first gas-liquid separator 23 through a choke valve step-down after, converge in order through entering low-pressure pipe network 6 behind subcooler 22 and the main heat exchanger 21 with the flashed vapour that produces in second gas-liquid separator 24, described flashed vapour further provides cold for subcooler 22 and main heat exchanger 21.Described flashed vapour also can be used as the regeneration gas of molecular sieve.
The preferred embodiments of the present invention also comprise the heating furnace 7 of the adsorbent reactivation that is used for making first absorber 11 and second absorber 12, are connected with pressurized end 28 pipelines of described decompressor 27.Heating furnace 7 can be heated to 280 degrees centigrade, thereby makes molecular sieve and active carbon holomorphosis in the absorber.
The preferred embodiments of the present invention are utilized Aspen and two kinds of flowsheeting softwares of HYSYS, adopt the cubic form state equation that this device flow process is carried out analog computation, guarantee the accurately feasible of device technique.
Introduce liquefaction flow path of the present invention below, may further comprise the steps:
Raw natural gas is exported from raw natural gas pipe network 5, enters pretreatment system 1;
First absorber 11 through pretreatment system 1 removes water, heavy hydrocarbon and benzene, and wherein a part enters second absorber 12 again and removes carbon dioxide;
Remove the natural gas behind the carbon dioxide,, natural gas is liquefied fully through main heat exchanger 21 back coolings; Only remove the natural gas of water, heavy hydrocarbon and benzene, after main heat exchanger 21 back coolings, enter decompressor 27 and expand, for main heat exchanger 21 provides cold;
After 25 step-downs of natural gas after liquefaction process first throttle valve, enter into first gas-liquid separator 23 more fully, this moment, the top of first gas-liquid separator 23 can produce 38% flashed vapour, and the bottom is a liquefied natural gas;
It is cold excessively that liquefied natural gas carries out the degree of depth through described subcooler 22 again;
The degree of depth is crossed liquefied natural gas after cold after 26 step-downs of second choke valve, enters into second gas-liquid separator 24 again, and this moment, the top of second gas-liquid separator 24 can produce flashed vapour, and the liquefied natural gas of bottom then enters stocking system 3.
The flashed vapour of separating from first gas-liquid separator 23 and second gas-liquid separator 24 is through behind the described subcooler 22, converges through behind the main heat exchanger 21 to enter into low-pressure pipe network 6.
After natural gas after the described decompressor 27 of process expands enters into main heat exchanger 21, for main heat exchanger 21 provides cold, after the re-heat, enter pressurized end 28 superchargings of decompressor 27 again, pressure pipe net 4 in entering after the cooling.This device adopts open circuit expander refrigeration flow process, liquefied fraction about 10%, so the natural gas that do not liquefy of major part enter after pressing in reducing in pressure pipe net 4.
Owing to adopt the design of energy-conserving and environment-protective, normal operation is consumption of power power supply not substantially, and gas-liquid realizes zero-emission substantially, adopts the natural gas liquefaction flow process of this technology to have the very large market competitiveness certainly.
The present invention still has multiple concrete embodiment, and all employings are equal to replacement or equivalent transformation and all technical schemes of forming, all drop within the scope of protection of present invention.
Claims (10)
1. natural gas liquefaction device, comprise by the interconnective pretreatment system of pipeline (1), liquefaction system (2) and stocking system (3), raw natural gas passes through in order and changes into liquefied natural gas behind pretreatment system (1) and the liquefaction system (2) and enter stocking system (3), it is characterized in that: described liquefaction system (2) comprises main heat exchanger (21) and the subcooler (22) that is used for heat exchange, be used for first gas-liquid separator (23) and second gas-liquid separator (24) that liquefied natural gas is separated and a decompressor (27); Natural gas after filtering through pretreatment system (1) enters main heat exchanger (21), first gas-liquid separator (23), subcooler (22), second gas-liquid separator in order and changes into liquefied natural gas after (24); The pipeline connection of described decompressor (27) and pretreatment system (1), the pipeline of described decompressor (27) passes main heat exchanger (21), and provides cold for main heat exchanger (21); Be connected with first throttle valve (25) on the pipeline between described main heat exchanger (21) and first gas-liquid separator (23); Be connected with second choke valve (26) on the pipeline between described subcooler (22) and second gas-liquid separator (24).
2. natural gas liquefaction device according to claim 1, it is characterized in that: enter low-pressure pipe network (6) after the flashed vapour that produces in described first gas-liquid separator (23) and second gas-liquid separator (24) passes through subcooler (22) and main heat exchanger (21) in order, described flashed vapour is that subcooler (22) and main heat exchanger (21) provide cold.
3. natural gas liquefaction device according to claim 2 is characterized in that: pressure pipe net (4) in entering behind natural gas process main heat exchanger (21) after expanding through described decompressor (27) and the pretreatment system (1).
4. natural gas liquefaction device according to claim 1 is characterized in that: described pretreatment system (1) comprises first absorber (11) of the water, heavy hydrocarbon and the benzene that are used for removing raw natural gas and is used to remove second absorber (12) of carbon dioxide.
5. natural gas liquefaction device according to claim 4 is characterized in that: also comprise the heating furnace (7) of the adsorbent reactivation that is used for making first absorber (11) and second absorber (12), be connected with pressurized end (28) pipeline of described decompressor (27).
6. liquefaction flow path that uses the described natural gas liquefaction device of claim 1 is characterized in that: may further comprise the steps,
Raw natural gas removes water, heavy hydrocarbon and benzene through first absorber (11) of pretreatment system (1), and wherein a part enters second absorber (12) again and removes carbon dioxide;
Remove the natural gas behind the carbon dioxide,, natural gas is liquefied fully through the cooling of main heat exchanger (21) back; Only remove the natural gas of water, heavy hydrocarbon and benzene, after the cooling of main heat exchanger (21) back, enter decompressor (27) and expand, for main heat exchanger (21) provides cold;
After the step-down of natural gas after liquefaction process first throttle valve (25), enter into first gas-liquid separator (23) more fully, the top of first gas-liquid separator this moment (23) can produce flashed vapour, and the bottom is a liquefied natural gas;
It is cold excessively that liquefied natural gas carries out the degree of depth through described subcooler (22) again;
The degree of depth is crossed liquefied natural gas after cold after second choke valve (26) step-down, enters into second gas-liquid separator (24) again, and the top of second gas-liquid separator this moment (24) can produce flashed vapour, and the liquefied natural gas of bottom then enters stocking system (3).
7. liquefaction flow path according to claim 6, it is characterized in that: the flashed vapour of separating from first gas-liquid separator (23) and second gas-liquid separator (24) through described subcooler (22) after, converge through entering into low-pressure pipe network (6) behind the main heat exchanger (21).
8. liquefaction flow path according to claim 6, it is characterized in that: the natural gas after entering decompressor (27) and expanding returns in the main heat exchanger (21) after the re-heat, enter pressurized end (28) supercharging of decompressor (27) again, through pressure pipe net (4) in entering after pretreatment system (1) cooling.
9. liquefaction flow path according to claim 6 is characterized in that: fully the natural gas after the liquefaction through first throttle valve (25) after, its pressure is reduced to 20 kilograms from every cubic centimetre 50 kilograms; The degree of depth is crossed liquefied natural gas after cold through second choke valve (26), and its pressure is reduced to 4 kilograms from every cubic centimetre 20 kilograms.
10. liquefaction flow path according to claim 6 is characterized in that: liquefied natural gas carries out the temperature that the degree of depth crosses after cold through described subcooler (22) can reduce 7-8 degree centigrade.
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| CN101787314B (en) * | 2010-04-01 | 2013-04-17 | 中国石油大学(华东) | Process for compact natural gas liquefying and floating production |
| CN102660341B (en) * | 2012-04-27 | 2014-05-07 | 新地能源工程技术有限公司 | Process and device utilizing pressure of natural gas to partially liquefy natural gas |
| CN103031170A (en) * | 2012-12-14 | 2013-04-10 | 贵州盘江煤层气开发利用有限责任公司 | Production method for concentrating low-concentration gas to prepare LNG (liquefied natural gas) |
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| EP3030338A1 (en) * | 2013-08-06 | 2016-06-15 | Dow Global Technologies LLC | Method comprising a microwave heating system for regenerating adsorbent media used for extracting natural gas liquids from natural gas |
| CN104515362B (en) * | 2013-09-30 | 2017-02-15 | 神华集团有限责任公司 | Method for producing liquid carbon dioxide |
| CN103712414B (en) * | 2013-12-31 | 2018-08-17 | 苏州制氧机有限责任公司 | A kind of natural gas liquefaction device and its liquefaction process |
| CN103712413B (en) * | 2013-12-31 | 2018-08-17 | 苏州制氧机有限责任公司 | A kind of natural gas liquefaction device |
| CN104864682B (en) * | 2015-05-29 | 2018-01-16 | 新奥科技发展有限公司 | A kind of natural gas pipe network pressure energy recoverying and utilizing method and system |
| CN107847851B (en) * | 2015-09-02 | 2021-05-18 | 埃克森美孚上游研究公司 | Swing adsorption process and system using demethanizer overhead stream as purge gas |
| CN106052303A (en) * | 2016-06-07 | 2016-10-26 | 成都赛普瑞兴科技有限公司 | Efficient expansion refrigeration methane-rich gas liquefaction method and device |
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Address after: Wuzhong District Mudu town Suzhou city Jiangsu province 215101 Spring Road No. 31 Patentee after: SUZHOU OXYGEN PLANT CO., LTD. Address before: Wuzhong District Mudu town Suzhou city Jiangsu province 215101 Spring Road No. 31 Patentee before: Suzhou Oxygen Plant Co., Ltd. |