CN101413749A - Method and apparatus for single-stage mixing cryogen refrigerating cycle liquefied natural gas - Google Patents
Method and apparatus for single-stage mixing cryogen refrigerating cycle liquefied natural gas Download PDFInfo
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- CN101413749A CN101413749A CNA2008101476236A CN200810147623A CN101413749A CN 101413749 A CN101413749 A CN 101413749A CN A2008101476236 A CNA2008101476236 A CN A2008101476236A CN 200810147623 A CN200810147623 A CN 200810147623A CN 101413749 A CN101413749 A CN 101413749A
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- azeotrope
- natural gas
- ice chest
- heat exchanger
- gas
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- 238000000034 method Methods 0.000 title claims abstract description 49
- 239000003949 liquefied natural gas Substances 0.000 title claims description 37
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 150
- 239000003345 natural gas Substances 0.000 claims abstract description 71
- 239000007788 liquid Substances 0.000 claims abstract description 39
- 239000007789 gas Substances 0.000 claims abstract description 22
- 230000005514 two-phase flow Effects 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 12
- 238000001816 cooling Methods 0.000 claims description 39
- 239000004215 Carbon black (E152) Substances 0.000 claims description 22
- 229930195733 hydrocarbon Natural products 0.000 claims description 22
- 150000002430 hydrocarbons Chemical class 0.000 claims description 22
- 230000007306 turnover Effects 0.000 claims description 8
- 238000007789 sealing Methods 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 5
- 230000008859 change Effects 0.000 claims description 3
- 230000008569 process Effects 0.000 abstract description 18
- 238000005057 refrigeration Methods 0.000 abstract description 11
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 230000009467 reduction Effects 0.000 abstract description 2
- 239000003507 refrigerant Substances 0.000 abstract 5
- 230000006835 compression Effects 0.000 description 8
- 238000007906 compression Methods 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 235000019628 coolness Nutrition 0.000 description 3
- 230000006837 decompression Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000003245 coal Substances 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
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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
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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
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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
- F25J1/0212—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
- F25J1/02—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
- F25J1/0258—Construction and layout of liquefaction equipments, e.g. valves, machines vertical layout of the equipments within in the cold box
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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"
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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.
- F25J1/0296—Removal of the heat of compression, e.g. within an inter- or afterstage-cooler against an ambient heat sink
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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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
Abstract
The invention discloses a method for liquefying natural gas by the refrigeration cycle of a single stage mixed refrigerant, which comprises the following steps: raw natural gas passes through a heat exchanger in an ice chest to exchange heat with the mixed refrigerant, and is cooled and liquefied; wherein, in sequence, the mixed refrigerant is first pressurized by a compressor, cooled by a cooler, directly enters the heat exchanger to be precooled without gas-liquid separation, goes out of the heat exchanger for depressurization and temperature reduction and then returns to the heat exchanger to exchange the heat of the natural gas and liquefy the natural gas, as well as is vaporized to gaseous mixed refrigerant and returns to the compressor for the next cycle; by reducing the outlet pressure of the compressor, or boosting the position of the outlet cooler of the compressor or using a way that the mixed refrigerant goes in and out of the ice chest both from the lower part, the method solves the problem of two phase flow of gas and liquid; can reduce the investment of the equipment such as a gas-liquid separator, a pump and the like, simplify the cycle process and operation control and reduce the manufacture cost as well. The invention also discloses a device applied to the method.
Description
Technical field
The invention belongs to the liquefaction technology field of natural gas, coal bed gas or other methane-rich gas, particularly a kind of method of single-stage mixing cryogen refrigerating cycle liquefied natural gas and device.
Background technology
The main component of natural gas, coal bed gas is a methane, at normal temperatures, can't only depend on pressurization that it is liquefied.Need to adopt natural gas liquefaction process that it is liquefied, is LNG (liquefied natural gas) such as the methane under normal pressure-162 ℃ of liquefaction, its volume only is 1/625 of an original gaseous state, its density be under the standard state more than 600 times of methane, water 45%, volume energy density is 72% of a gasoline.Because the convenience of the burning quality of its cleaning and use so be the industry and the domestic fuel of high-quality, very helps again carrying and storing simultaneously.
Common natural gas liquefaction cooling flow has tandem type kind of refrigeration cycle, azeotrope kind of refrigeration cycle and expander kind of refrigeration cycle at present.Though tandem type kind of refrigeration cycle unit energy consumption is minimum, energy-saving effect is best, the flow process complexity, and operation control is complicated, and equipment is many, and investment is maximum, is applicable to the Large LNG system; Expander kind of refrigeration cycle flow process is simple, regulates flexibly, is easy to the start-stop car, and easy operating is invested lowlyer, but specific energy consumption height is applicable to small-sized LNG system.The azeotrope kind of refrigeration cycle is to adopt azeotrope to carry out compression throttling refrigeration, and its flow process complexity, number of devices, control complexity, investment, specific energy consumption be then between between the two, mainly is applicable to big-and-middle-sized LNG system.At present the flow process of azeotrope kind of refrigeration cycle is after improving, because number of devices minimizing, process simplification, energy consumption is very low, control is simpler, can be suitable for the LNG system of various scales.Especially by the PRICO Refrigeration Technique of U.S. BVPI exploitation, it need not multistage separatory repeatedly mixes after the throttling and returns compressor, has simplified flow process to a certain extent, has reduced number of devices and investment.But its cooler is positioned on the ground, and after the azeotrope after the compressed machine compression enters cooler, thereby partial liquefaction (in the pipeline after cooler) produces gas-liquid two-phase in cooler; In order to solve the problem of azeotrope biphase gas and liquid flow, this technology still is provided with gas-liquid separator gas-liquid is separated behind cooler, isolated liquid cryogen is entered ice chest again with after being pumped to the ice chest porch and the isolated gas cryogen of separator mixing, this method has still increased number of devices (as separator, pump etc.) and control point, its circulation process and operation control etc. are still comparatively complicated, the increase of number of devices also causes the increase of input cost, thereby causes the increase of whole process of production cost.
Summary of the invention
Main purpose of the present invention provides a kind of method that need not to carry out azeotrope gas-liquid separation and the single-stage mixing cryogen refrigerating cycle liquefied natural gas that mixes, and minimizing equipment drops into, and simplifies circulation process and operation control, reduces production costs.Simultaneously, the present invention also provides a kind of device that is used for the method for above-mentioned single-stage mixing cryogen refrigerating cycle liquefied natural gas.
The technical solution adopted for the present invention to solve the technical problems is:
A kind of method of single-stage mixing cryogen refrigerating cycle liquefied natural gas, with raw natural gas by the heat exchanger in the ice chest, with the azeotrope heat exchange in the heat exchanger, raw natural gas is cooled to-135～-160 ℃ of liquefaction becomes LNG, sends to storage again after the step-down of natural gas choke valve; Wherein: azeotrope needs compressed successively machine supercharging earlier, cooler cooling, do not carry out gas-liquid separation then, directly enter heat exchanger precooling in the ice chest, go out heat exchanger again, lower the temperature through the step-down of azeotrope choke valve, return the heat exchanger in the ice chest, in heat exchanger, make it liquefaction with the raw natural gas heat exchange, and when the natural gas liquefaction cold is provided, make and self be vaporized into the gaseous state azeotrope, the gaseous state azeotrope then returns compressor and enters next circulation; Wherein, after the compressed machine supercharging of azeotrope, the cooler cooling, still can be owing to partial liquefaction produces gas-liquid two-phase, in order to realize not increasing equipment such as separator and pump and solve the gas-liquid two-phase flow problem, can adopt in the technical solution of the present invention following three kinds of methods any one or multiple:
(1), reduce compressor delivery pressure to 0.8～2.0MPa, to change two-phase volume ratio in the biphase gas and liquid flow, making the gas-liquid two-phase volume ratio is 0.0001～0.01; Promptly make the azeotrope can steady flow in pipeline by increasing in the two phase flow gas-liquid volume ratio;
(2), the position of raising the compressor outlet cooler makes it to be higher than the position of ice chest, not only make compressor outlet to the pipeline of cooler inlet two phase flow not occur, simultaneously can flow to ice chest smoothly, not need to increase equipment such as gas-liquid separator and pump through the cooled gas-liquid two-phase of cooler;
(3), the mode that the employing of natural gas turnover ice chest goes out on advancing down, azeotrope turnover ice chest goes out under adopting and advancing down; Rely on the pressure of natural gas and azeotrope self, send into smoothly in the ice chest, also can solve the gas-liquid two-phase flow problem.
Azeotrope can be selected in the prior art azeotrope commonly used in the natural gas liquefaction for use, as by N2 be selected from C
1To C
5The azeotrope formed of various ingredients such as hydrocarbon.
In the method for above-mentioned single-stage mixing cryogen refrigerating cycle liquefied natural gas:
After the compressed machine supercharging of azeotrope, its pressure can increase to 0.8～2.0MPa, and temperature is 80～150 ℃, becomes HTHP azeotrope gas;
HTHP azeotrope gas is after the cooler cooling, and its temperature can be cooled to 25～50 ℃;
Enter heat exchanger precooling in the ice chest (be chilled to liquid azeotrope heat exchange and reach the precooling purpose) through supercharging, cooled azeotrope and, become the low temperature liquid azeotrope to-145～-160 ℃ with throttling; Going out heat exchanger again, being cooled to pressure through azeotrope choke valve throttling expansion step-down is that 0.2～0.5MPa, temperature are-148～-163 ℃;
Liquid azeotrope after the step-down cooling makes the raw natural gas temperature reduce to-135～-160 ℃ and liquefy with the raw natural gas heat exchange in heat exchanger, also make simultaneously from compressor and cooler and compress the azeotrope precooling that has just entered after the cooling, the heat temperature that self then absorbs the two is elevated to normal temperature and is vaporized into the gaseous state azeotrope, the gaseous state azeotrope returns compressor by the pipeline cooling box, carries out the circulation of following one-period.
Be used for the device of the method for above-mentioned single-stage mixing cryogen refrigerating cycle liquefied natural gas, it consists of:
Mainly comprise cooling cycle system and natural gas liquefaction system, cooling cycle system mainly (can be positioned at ice chest by compressor, cooler, ice chest (wherein capital equipment is a heat exchanger), azeotrope choke valve, it is outer also can be positioned at ice chest) etc. be connected to form the cooling cycle system of (behind cooler outlet, not needing to be provided with gas-liquid separator and pump an etc.) sealing by pipeline; Ice chest wherein (comprising heat exchanger wherein etc.) also connects into natural gas liquefaction system by natural gas inlet and outlet piping and natural gas choke valve etc.(in the time of need before liquid, removing heavy hydrocarbon as in the natural gas pretreatment system, not removing heavy hydrocarbon) in case of necessity in advance, natural gas liquefaction system can also comprise the heavy hydrocarbon separator;
Wherein, gas-liquid separator and pump etc. are not set and solution gas-liquid two-phase flow problem after being implemented in cooler, said apparatus can adopt one of following proposal:
(1) cooler of compressor outlet, its position can be raised to the position that is higher than ice chest, not only make compressor outlet in the gas deliquescence process to the pipeline of ice chest import two phase flow not occur, simultaneously can flow to ice chest smoothly, not need to increase equipment such as gas-liquid separator and pump through the cooled gas-liquid two-phase of cooler;
(2) can adopt down the connected mode that outes for the pipeline of natural gas turnover ice chest,, adopt the mode that goes out under advancing down to be connected with ice chest simultaneously for the pipeline of azeotrope turnover ice chest; Rely on the pressure of natural gas and azeotrope self, pass in and out ice chest smoothly, also can solve the gas-liquid two-phase flow problem.
Compared with prior art, the invention has the beneficial effects as follows:
The method of single-stage mixing cryogen refrigerating cycle liquefied natural gas provided by the invention need not to carry out the azeotrope gas-liquid separation and mix, and can reduce equipment inputs such as gas-liquid separator and pump, and simplifies circulation process and operation control, reduces production costs simultaneously.
Description of drawings
Fig. 1 is the principle schematic of the method for the present invention's (not with heavy hydrocarbon separation module) single-stage mixing cryogen refrigerating cycle liquefied natural gas, also as the schematic flow sheet of the method for embodiment 1 single-stage mixing cryogen refrigerating cycle liquefied natural gas.
Fig. 2 has the principle schematic of method of the single-stage mixing cryogen refrigerating cycle liquefied natural gas of heavy hydrocarbon separation module for the present invention, also as the schematic flow sheet of the method for embodiment 2 single-stage mixing cryogen refrigerating cycle liquefied natural gas.
Fig. 3 is the schematic flow sheet of the method for the present invention's (not with heavy hydrocarbon separation module) embodiment 3 single-stage mixing cryogen refrigerating cycle liquefied natural gas.
In Fig. 1～3, the 11st, removed the natural gas of impurity, the 12nd, LNG (liquefied natural gas), the 13rd, heavy hydrocarbon; The 21st, the azeotrope gas of HTHP, the 22nd, cooled azeotrope, the 23rd, the azeotrope that is liquefied, the 24th, the azeotrope of low-temp low-pressure, the 25th, come from the azeotrope of ice chest; The 31st, heat exchanger, the 311st, precool heat exchanger device, the 312nd, main cold heat exchanger, the 32nd, compressor, the 33rd, cooler, the 34th, azeotrope choke valve, the 35th, natural gas choke valve, the 36th, heavy hydrocarbon separator.
The specific embodiment
The present invention is described in further detail below in conjunction with the specific embodiment.
But this should be interpreted as that the scope of the above-mentioned theme of the present invention only limits to following embodiment.
Among following each embodiment, the device that the method for single-stage mixing cryogen refrigerating cycle liquefied natural gas adopted includes the cooling cycle system and the natural gas liquefaction system of the sealing that is connected to form by pipeline by compressor 32, cooler 33, heat exchanger 31 and azeotrope choke valve 34, natural gas choke valve 35 etc.
Azeotrope is by N
2Be selected from C
1To C
5The azeotrope formed of various ingredients such as hydrocarbon.
Embodiment 1
Schematic diagram as shown in Figure 1 for the device (not being with the heavy hydrocarbon separation module) that present embodiment adopts, mainly comprise cooling cycle system and natural gas liquefaction system, cooling cycle system is connected to form the cooling cycle system of a sealing by pipeline by compressor 32, cooler 33, ice chest (wherein capital equipment is a heat exchanger 31), azeotrope choke valve 34 (being positioned at ice chest) etc.; Heat exchanger 31 in its ice chest, go back and natural gas choke valve 35 etc. connects into natural gas liquefaction system by the natural gas inlet and outlet piping; The position of cooler 33 is at ice chest top (outside the ice chest).
The azeotrope that adopts is by 5% N
2, 35% CH
4, 26% C
2H
4, 16% C
3H
8, 18% C
5H
12Form.
The method of present embodiment single-stage mixing cryogen refrigerating cycle liquefied natural gas comprises following key step (its flow process is as shown in Figure 1):
A, the azeotrope 25 that comes from ice chest are pressurized to 1.6Mpa by compressor 32, and temperature is about 140 ℃, becomes the azeotrope gas 21 of HTHP;
The azeotrope gas 21 of b, HTHP is cooled to 40 ℃ by cooler 33, gets cooled azeotrope 22, then cooled azeotrope 22 is sent to the ice chest inlet; By raising cooler 33 positions, it is arranged in the ice chest top, two phase flow does not appear in the pipeline that makes compressor 32 be exported to cooler 33 imports, only in entering the mouth than short duct, cooler 33 to ice chest occurs, and herein in the pipeline gas-liquid two-phase all flow downward, to the not influence that distributes of ice chest inlet gas-liquid;
C, cooled azeotrope 22 is entered heat exchanger 31 in the ice chest further be cooled to approximately-145 ℃ and liquefy, become the azeotrope 23 that is liquefied;
D, the azeotrope 23 that is liquefied are cooled to-148 ℃ by azeotrope choke valve 34 decompression 0.3Mpa, become the azeotrope 24 of low-temp low-pressure, return heat exchanger 31 then cold is provided, raw natural gas 11 and the azeotrope 22 that just enters ice chest after cooler 33 coolings are cooled off; After azeotrope 24 had absorbed the heat of this two fluid streams, its temperature was increased to normal temperature and is gasificated into gaseous state azeotrope 25, and cooling box returns compressor 32 and enters next circulation then;
E, about 40 ℃ of natural gas 11 temperature of impurity, the about 2.3Mpa of pressure have been removed through pretreatment system; By the heat exchanger in the ice chest 31, with azeotrope 24 heat exchange that are liquefied, being cooled to-146 ℃ of liquefaction of pact becomes LNG 12, delivers to the LNG storage tank after natural gas choke valve 35 is depressurized to 0.5Mpa.
Embodiment 2
Schematic diagram as shown in Figure 2 for the device (having the heavy hydrocarbon separation module) that present embodiment adopts, mainly comprise cooling cycle system and natural gas liquefaction system, cooling cycle system is connected to form the cooling cycle system of a sealing by pipeline by compressor 32, cooler 33, ice chest (wherein capital equipment is a heat exchanger, comprises precool heat exchanger device 311 and main cold heat exchanger 312), azeotrope choke valve 34 (being positioned at ice chest) etc.; Precool heat exchanger device 311 in its ice chest and main cold heat exchanger 312 are gone back and heavy hydrocarbon separator 36, natural gas choke valve 35 etc. connect into natural gas liquefaction system by the natural gas inlet and outlet piping.
The azeotrope that adopts is by 5% N
2, 35% CH
4, 26% C
2H
4, 16% C
3H
8, 18% C
5H
12Form.
The method of present embodiment single-stage mixing cryogen refrigerating cycle liquefied natural gas comprises following key step (its flow process is as shown in Figure 2):
A, the azeotrope 25 that comes from ice chest are pressurized to 1.3Mpa by compressor 32, and temperature is about 137 ℃, becomes the azeotrope gas 21 of HTHP;
The azeotrope gas 21 of b, HTHP is cooled to 38 ℃ by cooler 33, gets cooled azeotrope 22, then cooled azeotrope 22 is sent to the ice chest inlet; In order to prevent that two phase flow from flowing in ducted instability, having adopted the reduction compressor delivery pressure among this embodiment is that 1.3Mpa is to change the method for two-phase volume ratio in the liquid-gas two-phase flow, this moment, its value was 0.00615, can make azeotrope steady flow in pipeline;
C, cooled azeotrope 22 is entered precool heat exchanger device 311 and main cold heat exchanger 312 in the ice chest successively, further be cooled to approximately-146 ℃ and liquefy, become the azeotrope 23 that is liquefied;
D, the azeotrope 23 that is liquefied is cooled to-148 ℃ by azeotrope choke valve 35 decompression 0.3Mpa, become the azeotrope 24 of low-temp low-pressure, return heat exchanger then and pass through main cold heat exchanger 312 and precool heat exchanger device 311 successively, cold is provided, azeotrope to natural gas after separating through heavy hydrocarbon and the precooling of process precool heat exchanger device in main heat exchanger 312 cools off, in the precool heat exchanger device, raw natural gas 11 and the azeotrope 22 that just enters ice chest after cooler 33 coolings are cooled off, temperature was increased to normal temperature and is gasificated into gaseous state azeotrope 25 after azeotrope 24 absorbed heat, and cooling box returns compressor 32 and enters next circulation then;
E, removed the natural gas 11 of other impurity through pretreatment system, temperature is about 40 ℃, the about 2.5Mpa of pressure.By precool heat exchanger device 311 precoolings in the ice chest, heavy hydrocarbon separator 36 separate remove heavy hydrocarbon 13, and 312 coolings of main cold heat exchanger after, be cooled to approximately that-146 ℃ of liquefaction become LNG12, after being depressurized to 0.5Mpa, deliver to the LNG storage tank.
Embodiment 3
Schematic diagram as shown in Figure 3 for the device (not being with the heavy hydrocarbon separation module) that present embodiment adopts, mainly comprise cooling cycle system and natural gas liquefaction system, cooling cycle system is connected to form the cooling cycle system of a sealing by pipeline by compressor 32, cooler 33, ice chest (wherein capital equipment is a heat exchanger 31), azeotrope choke valve 34 (being positioned at ice chest) etc.; Heat exchanger 31 in its ice chest, go back and natural gas choke valve 35 etc. connects into natural gas liquefaction system by the natural gas inlet and outlet piping; Wherein, the connected mode that goes out on advancing under the pipeline of natural gas turnover ice chest adopts, the mode that the pipeline that supplies azeotrope to pass in and out ice chest simultaneously goes out under adopting and advancing down is connected with ice chest.
The azeotrope that adopts is by 8% N
2, 30% CH
4, 28% C
2H
4, 16% C
3H
8, 18% C
5H
12Form.
The method of present embodiment single-stage mixing cryogen refrigerating cycle liquefied natural gas comprises following key step (its flow process is as shown in Figure 3):
A, the azeotrope 25 that comes from ice chest are pressurized to 2.0Mpa by compressor 32, and temperature is about 150 ℃, becomes the azeotrope gas 21 of HTHP;
The azeotrope gas 21 of b, HTHP is cooled to 38 ℃ by cooler 33, gets cooled azeotrope 22, then cooled azeotrope 22 is sent to the ice chest inlet; In order to prevent that two phase flow from flowing in ducted instability, azeotrope turnover ice chest adopts the mode of advancing down to go out down, enter from the ice chest bottom, after heat exchanger 31 precoolings, be cooled to-148 ℃ through 34 decompressions of azeotrope choke valve again, become the azeotrope 24 of low-temp low-pressure, returning heat exchanger 31 then provides cold that raw natural gas 11 is cooled off; Azeotrope 24 absorbs heat and is gasificated into gaseous state azeotrope 25, and gaseous state azeotrope 25 still comes out from the ice chest bottom, returns compressor 32 and enters next circulation;
C, removed the raw natural gas 11 of impurity through pretreatment system, temperature is about 40 ℃, the about 2.0Mpa of pressure; By the heat exchanger in the ice chest 31, with azeotrope 24 heat exchange that are liquefied, being cooled to-146 ℃ of liquefaction of pact becomes LNG 12, delivers to the LNG storage tank after natural gas choke valve 35 is depressurized to 0.5Mpa.
On key foundation of the present invention, can also take different temperature, pressure operation parameter according to the master-plan of system and the composition of unstripped gas.
Because therefore the inevitable loss of cold-producing medium in kind of refrigeration cycle need regularly replenish; Under normal start-stop car or accident condition, need charge into or discharge azeotrope, necessary therefrom separation, married operation do not influence the expression of feature of the present invention.
Can the cooling of one-level compression one-level in the compression cooling procedure, also can multistage cooling of multiple compressors multi-stage compression or the multistage cooling of a compressor multi-stage compression.The one-level compression is reduced investment outlay, and multi-stage compression is energy-saving and cost-reducing.No matter adopt which kind of compact model, as long as the operation that there is not shunting in the cold-producing medium circulation, mixes does not then influence feature representation of the present invention.
Remove water, sour gas and mercury in the raw natural gas.Heavy hydrocarbon can remove by molecular sieve in pretreatment system, perhaps by independently making the heavy hydrocarbon condensation and separated removing after the chilldown system cooling; Also can not establish independently chilldown system, and remove heavy hydrocarbon by the cooling of the forecooler in the ice chest.When adopting the latter, heavy hydrocarbon separates from the natural gas streamline, and therefore not shunting or mixing of azeotrope do not influence feature representation of the present invention.
If the nitrogenous height of raw natural gas and need denitrogenation then also can increase the denitrogenation module on the natural gas streamline.Lock out operation in the denitrification process betides on the natural gas streamline, and azeotrope is shunting or mixing not, does not therefore also influence feature representation of the present invention.
Claims (4)
1. the method for a single-stage mixing cryogen refrigerating cycle liquefied natural gas, with raw natural gas by the heat exchanger in the ice chest, with the azeotrope heat exchange in the heat exchanger, raw natural gas is cooled to-135～-160 ℃ of liquefaction becomes LNG, sends to storage again after the step-down of natural gas choke valve; Wherein: azeotrope compressed successively machine supercharging earlier, cooler cooling, do not carry out gas-liquid separation then, directly enter heat exchanger precooling in the ice chest, go out heat exchanger again, lower the temperature through the step-down of azeotrope choke valve, return the heat exchanger in the ice chest, in heat exchanger, make it liquefaction with the raw natural gas heat exchange, and when the natural gas liquefaction cold is provided, make and self be vaporized into the gaseous state azeotrope, the gaseous state azeotrope then returns compressor and enters next circulation; Wherein, in order to solve the gas-liquid two-phase flow problem, adopt following three kinds of methods any one or multiple:
(1), reduce compressor delivery pressure to 0.8～2.0MPa, to change two-phase volume ratio in the biphase gas and liquid flow, making the gas-liquid two-phase volume ratio is 0.0001～0.01;
(2), the position of raising the compressor outlet cooler makes it to be higher than the position of ice chest;
(3), the mode that the employing of natural gas turnover ice chest goes out on advancing down, azeotrope turnover ice chest goes out under adopting and advancing down.
2. the method for single-stage mixing cryogen refrigerating cycle liquefied natural gas according to claim 1 is characterized in that: in the method for described single-stage mixing cryogen refrigerating cycle liquefied natural gas:
After the compressed machine supercharging of azeotrope, its pressure increases to 0.8～2.0MPa, and temperature is 80～150 ℃, becomes HTHP azeotrope gas;
HTHP azeotrope gas is after the cooler cooling, and its temperature is cooled to 25～50 ℃;
The heat exchanger that enters in the ice chest through supercharging, cooled azeotrope is chilled to-145～-160 ℃ in advance, becomes the low temperature liquid azeotrope; Going out heat exchanger again, being cooled to pressure through azeotrope choke valve throttling expansion step-down is that 0.2～0.5MPa, temperature are-148～-163 ℃;
Liquid azeotrope after the step-down cooling makes the raw natural gas temperature reduce to-135～-160 ℃ and liquefy with the raw natural gas heat exchange in heat exchanger, also make simultaneously from compressor and cooler and compress the azeotrope precooling that has just entered after the cooling, the heat temperature that self then absorbs the two is elevated to normal temperature and is vaporized into the gaseous state azeotrope, the gaseous state azeotrope returns compressor by the pipeline cooling box, carries out the circulation of following one-period.
3. device that is used for the method for the described single-stage mixing cryogen refrigerating cycle liquefied natural gas of claim 1, it consists of:
Mainly comprise cooling cycle system and natural gas liquefaction system, cooling cycle system mainly is connected to form the cooling cycle system of sealing by compressor, cooler, ice chest, azeotrope choke valve by pipeline, and capital equipment is a heat exchanger in the ice chest; Described ice chest also connects into natural gas liquefaction system by natural gas inlet and outlet piping and natural gas choke valve;
Wherein, in order to solve the gas-liquid two-phase flow problem, described device also adopts one of following proposal:
(1) cooler of compressor outlet, its position is raised to the position that is higher than ice chest;
(2) connected mode that goes out on advancing under the pipeline that supplies natural gas to pass in and out ice chest adopts supplies azeotrope to pass in and out the pipeline of ice chest simultaneously, and the mode that employing goes out under advancing down is connected with ice chest.
4. device according to claim 3 is characterized in that: also comprise the heavy hydrocarbon separator in the described natural gas liquefaction system.
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