CN107436072A - Natural gas liquefaction system and method with refrigerant supplementary device - Google Patents
Natural gas liquefaction system and method with refrigerant supplementary device Download PDFInfo
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- CN107436072A CN107436072A CN201710691412.8A CN201710691412A CN107436072A CN 107436072 A CN107436072 A CN 107436072A CN 201710691412 A CN201710691412 A CN 201710691412A CN 107436072 A CN107436072 A CN 107436072A
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- heat exchanger
- separator
- refrigerant
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- 239000003507 refrigerant Substances 0.000 title claims abstract description 114
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 88
- 239000003345 natural gas Substances 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 28
- 238000005057 refrigeration Methods 0.000 claims abstract description 21
- 239000007791 liquid phase Substances 0.000 claims description 75
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 70
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 claims description 58
- 239000007789 gas Substances 0.000 claims description 44
- 239000012071 phase Substances 0.000 claims description 39
- 230000006835 compression Effects 0.000 claims description 36
- 238000007906 compression Methods 0.000 claims description 36
- 239000001294 propane Substances 0.000 claims description 35
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 34
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims description 29
- 239000002826 coolant Substances 0.000 claims description 27
- 239000007788 liquid Substances 0.000 claims description 20
- 239000007792 gaseous phase Substances 0.000 claims description 14
- 230000001105 regulatory effect Effects 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 230000004087 circulation Effects 0.000 claims description 10
- 239000013589 supplement Substances 0.000 claims description 9
- 239000003795 chemical substances by application Substances 0.000 claims description 8
- 239000012808 vapor phase Substances 0.000 claims description 8
- 239000005977 Ethylene Substances 0.000 claims description 6
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 6
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 239000000047 product Substances 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims 2
- 230000007423 decrease Effects 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 230000001502 supplementing effect Effects 0.000 abstract 1
- 239000003949 liquefied natural gas Substances 0.000 description 9
- 238000002156 mixing Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 3
- 239000000470 constituent Substances 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- -1 isopropyl alkane Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000007115 recruitment Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Classifications
-
- 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
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
- F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
-
- 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
- F25J1/0047—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
-
- 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
-
- 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
Abstract
The present invention relates to a kind of natural gas liquefaction system and natural gas liquefaction with refrigerant supplementary device, for supplementing refrigerant in using the natural gas liquefaction device kind of refrigeration cycle of hybrid refrigeration liquefaction process, its device includes four separators, four throttling arrangements, two flow control valves, two flow metering devices, one group of plate-fin heat exchanger.Cycle of driving can significantly be shortened using method proposed by the present invention, reduce energy consumption of compressor and heat exchanger cold energy in startup procedure.
Description
Technical field
The present invention relates to the liquefied natural gas (LNG) production using hybrid refrigeration liquefaction process, and in particular to one kind carries refrigerant
The natural gas liquefaction system and natural gas liquefaction of supplementary device.
Background technology
With the growth of Natural Gas Consumption Using, turn into for one of form, liquefied natural gas as natural gas is maximally effective
One of fastest-rising field of energy market.The continuous development of liquefied natural gas industry, exists to natural gas liquefaction and device
Energy consumption, investment and efficiency etc. propose higher requirement.
At present, the natural gas liquefaction process of comparative maturity mainly has：Cascaded refrigeration process, swell refrigeration technique and mixing system
Cold technique.Mixed refrigeration process therein then compares to be favored by medium-sized natural gas liquefaction device, but other relative refrigeration process
For, mixed refrigeration process is more difficult there is mix refrigerant component proportion, device drive the cycle it is longer the shortcomings that.Mixing
Component in refrigerant, such as propane, isopentane, be to be added in liquid form in refrigerant compression cycle, need and its
Turn into gas phase after his light component mixing, can just participate in refrigerant compression.The vaporization of heavy constituent, light, heavy constituent so that device
The driving cycle is significantly elongated.The present invention proposes a kind of new refrigerant compensation process and its device, can reduce refrigerant benefit
Difficulty is filled, shortens the cycle of driving.
The content of the invention
The invention provides a kind of refrigerant compensation process and device for hybrid refrigeration liquefaction process, for use
Refrigerant is supplemented in the refrigerant-cycle systems of the natural gas liquefaction device of hybrid refrigeration liquefaction process, driving flow can be simplified,
Shorten the cycle of driving.
A kind of natural gas liquefaction system with refrigerant supplementary device of the present invention, it includes first, second,
Three and the 4th separator, first, second, third and fourth throttling arrangement, the first and second flow control valves, the first and second streams
Measuring equipment and one group of plate-fin heat exchanger are measured,
Wherein, the one-level liquid phase refrigerant pipeline from refrigerant compression systems is logical by the first heat exchange in heat exchanger group
Road connects one end of first throttle device, and the other end of first throttle device is connected with the entrance of the first separator；
The two level liquid phase refrigerant pipeline come from refrigerant compression systems passes through the second heat exchanger channels in heat exchanger group
It is connected with one end of second throttling device, the other end of second throttling device is connected with the entrance of the first separator, the first separation
The gaseous phase outlet and liquid-phase outlet of device are connected to the 3rd heat exchanger channels in heat exchanger group；
The secondary gas phase refrigerant tubing come from refrigerant compression systems passes through the 4th heat exchanger channels in heat exchanger group
It is connected with the entrance of the second separator, the gaseous phase outlet of the second separator passes through the 5th heat exchanger channels and the 3rd in heat exchanger group
One end connection of throttling arrangement, the other end of the 3rd throttling arrangement are connected with the entrance of the 3rd separator, the gas of the 3rd separator
Mutually outlet and liquid-phase outlet are connected to the 3rd heat exchanger channels in heat exchanger group；The liquid-phase outlet of second separator passes through heat exchanger
The 7th heat exchanger channels in group are connected with one end of the 4th throttling arrangement, the other end of the 4th throttling arrangement and the 4th separator
Entrance connects, and the gaseous phase outlet and liquid-phase outlet of the 4th separator are connected to the 3rd heat exchanger channels in heat exchanger group；3rd changes
The other end of the passage of heat returns to refrigerant compression systems；Purified natural gas pipeline connects the 6th heat exchanger channels of heat exchanger group, so
After be connected to LNG pipelines；
Propane/isopentane pipeline from propane, isopentane stocking system measures equipment flowmeter, connection through first flow
The first separator inlet is connected to after first flow regulating valve；
Ethylene conduit from ethene stocking system measures equipment flowmeter through second flow, connects second flow regulating valve
The entrance of the 4th separator is connected to afterwards.
Further, the refrigerant supplementary device for hybrid refrigeration liquefaction process further comprises that secondary refrigerant compresses
The liquid-phase outlet connection one-level liquid phase refrigerant pipeline of system, wherein one stage of compression, the liquid-phase outlet connection two level of two-stage compression
Liquid phase refrigerant pipeline, and the gaseous phase outlet connection secondary gas phase refrigerant tubing of two-stage compression.
Further, what the gaseous phase outlet of the first separator and liquid-phase outlet were connected to after converging in heat exchanger group the 3rd changes
The passage of heat or the 3rd heat exchanger channels being respectively connecting in heat exchanger group；And/or
The gaseous phase outlet and liquid-phase outlet of 3rd separator be connected to after converging the 3rd heat exchanger channels in heat exchanger group or
The 3rd heat exchanger channels being respectively connecting in heat exchanger group；And/or
The gaseous phase outlet and liquid-phase outlet of 4th separator be connected to after converging the 3rd heat exchanger channels in heat exchanger group or
The 3rd heat exchanger channels being respectively connecting in heat exchanger group.
Further, the other end of the 3rd heat exchanger channels returns to the entrance of the one stage of compression of refrigerant compression systems.
The invention further relates to the natural gas liquefaction using said system, its technological process are as follows：
Raw natural gas after purification enters plate-fin heat exchanger group, cold that absorption refrigeration agent discharges carry out precooling,
Liquefaction, and -130 DEG C~-162 DEG C are finally cooled to, further such as -135~-155 DEG C, obtain LNG product；
Mix refrigerant (including the C1~C5 and N2 of arbitrary proportion or be made up of the C1~C5 and N2 of arbitrary proportion) is through mixed
Close coolant compressor supercharging, obtained one-level liquid phase refrigerant, two level liquid phase refrigerant, secondary gas phase refrigerant；
The one-level liquid phase refrigerant initially enters the first heat exchanger channels of heat exchanger group, is cooled to about 0 DEG C in advance wherein
~-30 DEG C, preferably -5~-20 DEG C, throttled through first throttle valve to 0.25~0.8MPaA, the is entered after preferably 0.4-0.7MPa
One separator, the gas phase isolated by the first separator and liquid phase enter the 3rd heat exchanger channels of heat exchanger group after converging, with from
The mixed refrigerant stream stock that heat exchanger group rear stage heat exchanger returns converges, and provides cold for heat exchanger group, is then back to mixing
Coolant compressor entrance is pressurized；
By refrigerant compression systems Lai two level liquid phase refrigerant be cooled to 0 DEG C in advance by the heat exchanger channels of heat exchanger group second
~-30 DEG C, preferably -5~-20 DEG C, then throttled through second throttle to 0.25~0.8MPaA, after preferably 0.4-0.7MPa, also enter
Enter the first separator and carry out gas-liquid distribution；
By refrigerant compression systems Lai fourth heat exchanger channels of the secondary gas phase refrigerant through heat exchanger group, be cooled to 0 DEG C
~-30 DEG C, preferably -5~-20 DEG C, subsequently into the second separator liquid separation, the gas phase isolated goes out from the top of the second separator
The 5th heat exchanger channels for mouthful entering heat exchanger group are cooled to -30 DEG C~-100 DEG C, preferably -40~-90 DEG C, and further such as -50
~-80 DEG C, then throttled through the 3rd choke valve 3 to 0.25~0.8MPaA, enter the 3rd separator after preferably 0.4-0.7MPa,
The gas phase isolated by the 3rd separator enters the 3rd heat exchanger channels of heat exchanger group after converging with liquid phase, provided for heat exchanger group
Cold, finally return that coolant compressor entrance is pressurized；The liquid phase that second separator is isolated goes out from the bottom of the second separator
The 7th heat exchanger channels that mouth enters heat exchanger group are cooled to -135 DEG C~-165 DEG C, preferably -140~-155 DEG C, then through the 4th
Choke valve throttles to 0.25~0.8MPaA, enters the 4th separator after preferably 0.4-0.7MPa, is isolated by the 4th separator
Gas phase enters the 3rd heat exchanger channels of heat exchanger group after converging with liquid phase, cold is provided for heat exchanger group；
The propane come from propane, isopentane stocking system is supplemented to after flowmeter measures by first flow regulating valve
On the inlet duct of first separator, predominantly liquid phase may carry a small amount of tolerance, be distributed into the first separator gas-liquid
Afterwards, together into plate-fin heat exchanger group；
The ethene come from ethene stocking system is supplemented to the 4th separation after flowmeter measures, by second flow regulating valve
Also it is mainly liquid phase on the inlet duct of device, caused tolerance during possible carrying pipe is defeated, into the 4th separator gas-liquid point
After as one sees fit, together into plate-fin heat exchanger group.
Further, drive to supplement methane and nitrogen gas refrigerant successively initial stage in natural gas liquefaction device, make refrigerant pressure
Circulation is formed between contracting machine and plate-fin heat exchanger group, is then slowly added to propane, isopentane successively, in the first separator
Propane, isopentane vaporize under the drive of swiftly flowing vapor phase refrigerant from bottom to top of the 3rd heat exchanger channels, together return to system
Refrigerant compressor entrance；After declining (such as dropping to -100~-70 DEG C) Deng plate-fin heat exchanger group entirety warm area, now second
Alkene is added to the 4th separator from ethene stocking system through second flowmeter, second flow regulating valve, the second in the 4th separator
Alkene vaporizes under the drive of swiftly flowing vapor phase refrigerant from bottom to top of the heat exchanger channels of heat exchanger group the 3rd, together returns to refrigeration
Agent suction port of compressor.Driving is dropped in order to avoid plate-fin heat exchanger group local temperature is poly-, produced not by this approach make-up ethylene initial stage
Potential safety hazard.
Further, drive to be added to methane and nitrogen gas refrigerant successively initial stage in natural gas liquefaction device, make refrigerant
Circulation is formed between compressor and plate-fin heat exchanger group, propane, isopentane is then added to successively, is then added to successively again
Methane and nitrogen gas refrigerant, propane, isopentane are then added to successively, repeat one or more circulations, such as 2-5 circulation.
Component is supplemented successively from light to heavy, and magnitude of recruitment, flow velocity depend on the scale of specific natural gas liquefaction device, are not especially to limit
, it can be determined by site operation personnel, supplement speed speed simply influences the time of driving；Typically it is added to several times, supplement one
Meeting youngster's light component, then the heavy constituents such as propane, isopentane are mended, light component is then mended again；Until each component refrigerant is full of in system,
So that final each group distribution ratio is：N2:5mol%-25mol%, C1:10mol%-25mol%, C2:30mol%-
55mol%, C3:10mol%-25mol%, C5:10mol%-25mol%, the total mole number based on all gas.
Advantages of the present invention：
1. during ethene, propane, isopentane etc. to be directly added to the cryogen liquid separation tank for storing liquid phase originally, more former supplement
To coolant compressor entrance, and the compensation process that each component vaporizes need to be compared, flow is more simple, can save driving week
Phase.
2. it is to eliminate each component by liquid phase by another advantage that each refrigerant component is directly added to cryogen liquid separation tank
It is changed into vapour phase, is then changed into the process of liquid phase again, the compression power consumption of coolant compressor, and plate-fin heat exchanger can be saved
In cold.
Brief description of the drawings
Fig. 1 is process chart of the present invention.
Embodiment
Further illustrate below in conjunction with the accompanying drawings：
As shown in figure 1, the refrigerant supplementary device of the present invention for hybrid refrigeration liquefaction process, including four points
From device, four throttling arrangements, two flow control valves, two flow metering devices, one group of plate-fin heat exchanger.
By refrigerant compression systems Lai one-level liquid phase refrigerant pipeline pass through the first heat exchanger channels in heat exchanger group E1
One end of first throttle device 1 is connected, the other end of first throttle device 1 is connected with the first separator V1 entrance；By freezing
The two level liquid phase refrigerant pipeline that agent compressibility comes passes through the second heat exchanger channels in heat exchanger group E1 and second throttling device 2
One end connection, the other end of second throttling device 2 is connected with the first separator V1 entrance, the first separator V1 gas phase and
Liquid-phase outlet is connected to the 3rd heat exchanger channels in heat exchanger group E1；By refrigerant compression systems Lai secondary gas phase refrigerant pipe
Road is connected by the 4th heat exchanger channels in heat exchanger group E1 with the second separator V2 entrance, and the second separator V2 gas phase goes out
Mouthful be connected by the 5th heat exchanger channels in heat exchanger group E1 with one end of the 3rd throttling arrangement 3, the 3rd throttling arrangement 3 it is another
End is connected with the 3rd separator V3 entrance, and the 3rd separator V3 gas phase and liquid-phase outlet are connected to the in heat exchanger group E1
Three heat exchanger channels；Second separator V2 liquid-phase outlet passes through the 7th heat exchanger channels and the 4th throttling arrangement in heat exchanger group E1
4 one end connection, the other end of the 4th throttling arrangement 4 are connected with the 4th separator V4 entrance, the 4th separator V4 gas phase
And liquid-phase outlet is connected to the 3rd heat exchanger channels in heat exchanger group E1；The other end of 3rd heat exchanger channels returns to refrigerant compression
System；Purified natural gas pipeline connection heat exchanger group E1 the 6th heat exchanger channels, are then attached to LNG pipelines；
Propane/isopentane pipeline from propane, isopentane stocking system measures equipment flowmeter F1 through first flow, even
The first separator V1 entrances are connected to after connecing first flow regulating valve 5；
Ethylene conduit from ethene stocking system measures equipment flowmeter F2, connection second flow regulation through second flow
The 4th separator V4 entrance is connected to after valve 6.
It is as follows for the refrigerant compensation process of hybrid refrigeration liquefaction process, its technological process：
As shown in Figure 1, the raw natural gas after purification enters plate-fin heat exchanger group E1, and absorption refrigeration agent discharges
Cold carries out precooling, liquefaction, and is finally cooled to -130 DEG C~-162 DEG C, obtains LNG product；
Mix refrigerant is made up of C1~C5 and N2, and blended coolant compressor is pressurized, obtained one-level liquid phase system
Cryogen, two level liquid phase refrigerant, secondary gas phase refrigerant respectively enter plate-fin heat exchanger group E1 and participate in heat exchange；
By refrigerant compression systems Lai one-level liquid phase refrigerant initially enter heat exchanger group E1 the first heat exchanger channels,
Wherein it is cooled to about 0 DEG C~-30 DEG C in advance, the first separator V1 is entered after first throttle valve 1 throttles to 0.25~0.8MPaA,
The gas phase isolated by the first separator V1 enters heat exchanger group E1 the 3rd heat exchanger channels after converging with liquid phase, and from heat exchanger
The mixed refrigerant stream stock that group E1 rear stages heat exchanger returns converges, and cold is provided for heat exchanger group E1, is then back to mixing system
Refrigerant compressor entrance is pressurized；By refrigerant compression systems Lai two level liquid phase refrigerant exchanged heat by heat exchanger group E1 second it is logical
Road is cooled to 0 DEG C~-30 DEG C in advance, then is throttled through second throttle 2 to 0.25~0.8MPaA, also enters into the first separator V1
Promoting the circulation of qi liquid distributes；By refrigerant compression systems Lai fourth heat exchanger channels of the secondary gas phase refrigerant through heat exchanger group E1, cooling
To 0 DEG C~-30 DEG C, subsequently into the second separator V2 liquid separations, the gas phase isolated is entered from the second separator V2 top exit
The 5th heat exchanger channels for entering heat exchanger group E1 are cooled to -30 DEG C~-100 DEG C, then throttle to 0.25 through the 3rd choke valve 3~
Enter the 3rd separator V3 after 0.8MPaA, the gas phase isolated by the 3rd separator V3 enters heat exchanger group after converging with liquid phase
E1 the 3rd heat exchanger channels, cold is provided for heat exchanger group E1, finally return that coolant compressor entrance is pressurized；Second separator
The liquid phase that V2 is isolated is cooled to -135 from the second separator V2 outlet at bottom into heat exchanger group E1 the 7th heat exchanger channels
DEG C~-165 DEG C, the 4th separator V4 is then entered after the 4th choke valve 4 throttles to 0.25~0.8MPaA, by the 4th separation
The gas phase that device V4 is isolated enters heat exchanger group E1 the 3rd heat exchanger channels after converging with liquid phase, provided for heat exchanger group E1 cold
Amount；
From the propane that propane, isopentane stocking system come after flowmeter F1 meterings, supplemented by first flow regulating valve 5
To the first separator V1 inlet duct, predominantly liquid phase may carry a small amount of tolerance, into the first separator V1 gas-liquids
After distribution, together into plate-fin heat exchanger group E1；
From the ethene that ethene stocking system comes after flowmeter F2 meterings, the 4th is supplemented to by second flow regulating valve 6
Also it is mainly liquid phase on separator V4 inlet duct, caused tolerance during possible carrying pipe is defeated, into the 4th separator
After V4 gas-liquids point are taken the circumstances into consideration, together into plate-fin heat exchanger group E1.
Device drives to supplement refrigerant initial stage, is added to the light components such as methane, nitrogen to coolant compressor entrance first,
Make to form circulation between coolant compressor and plate-fin heat exchanger group E1, be then slowly added to propane, isopentane, first point
Vaporized from the propane in device V1, isopentane under the drive of swiftly flowing vapor phase refrigerant from bottom to top of the 3rd heat exchanger channels,
Together return to coolant compressor entrance；After declining Deng plate-fin heat exchanger group E1 entirety warm area, now ethene stores up from ethene
Deposit system is added to the 4th separator V4 through flowmeter, flow control valve, and the ethene in the 4th separator V4 is in heat exchanger group E1
Vaporized under the drive of swiftly flowing vapor phase refrigerant from bottom to top of 3rd heat exchanger channels, together return to coolant compressor and enter
Mouthful.Driving is dropped in order to avoid plate-fin heat exchanger group E1 local temperatures are poly- not by this approach make-up ethylene, it is hidden to produce safety initial stage
Suffer from.
Embodiment 1
As shown in Figure 1, the raw natural gas after purification enters plate-fin heat exchanger group E1, and absorption refrigeration agent discharges
Cold carries out precooling, liquefaction, and is finally cooled to -141 DEG C, obtains LNG product；
Mix refrigerant is by C1~C5 and N2Composition, and blended coolant compressor is pressurized, obtained one-level liquid phase system
Cryogen, two level liquid phase refrigerant, secondary gas phase refrigerant respectively enter plate-fin heat exchanger group E1 and participate in heat exchange；
By refrigerant compression systems Lai one-level liquid phase refrigerant initially enter heat exchanger group E1 the first heat exchanger channels,
Wherein it is cooled to about -15 DEG C in advance, the first separator V1 is entered after first throttle valve 1 throttles to 0.5MPaA, by the first separator
The gas phase that V1 is isolated enters heat exchanger group E1 the 3rd heat exchanger channels after converging with liquid phase, with being changed from heat exchanger group E1 rear stages
The mixed refrigerant stream stock that hot device returns converges, and provides cold for heat exchanger group E1, is then back to mix refrigerant compressor and enters
Mouth supercharging；By refrigerant compression systems Lai two level liquid phase refrigerant be cooled to -18 in advance by heat exchanger group the second heat exchanger channels of E1
DEG C, then throttled through second throttle 2 to 0.5MPaA, also carry out gas-liquid distribution into the first separator V1；By refrigerant compression
Fourth heat exchanger channels of the secondary gas phase refrigerant through heat exchanger group E1 that system is come, are cooled to -16 DEG C, subsequently into the second separation
Device V2 liquid separations, the gas phase isolated cool down from the second separator V2 top exit into heat exchanger group E1 the 5th heat exchanger channels
To -60 DEG C, the 3rd separator V3 is then entered after the 3rd choke valve 3 throttles to 0.5MPaA, is isolated by the 3rd separator V3
Gas phase and liquid phase converge after enter heat exchanger group E1 the 3rd heat exchanger channels, provide cold for heat exchanger group E1, finally return that
Coolant compressor entrance is pressurized；The liquid phase that second separator V2 is isolated enters heat exchange from the second separator V2 outlet at bottom
Device group E1 the 7th heat exchanger channels are cooled to -145 DEG C, and the 4th point is then entered after the 4th choke valve 4 throttles to about 0.5MPaA
From device V4, the gas phase isolated by the 4th separator V4 enters heat exchanger group E1 the 3rd heat exchanger channels after converging with liquid phase, be
Heat exchanger group E1 provides cold；
From the propane that propane, isopentane stocking system come after flowmeter F1 meterings, supplemented by first flow regulating valve 5
To the first separator V1 inlet duct, predominantly liquid phase may carry a small amount of tolerance, into the first separator V1 gas-liquids
After distribution, together into plate-fin heat exchanger group E1；
From the ethene that ethene stocking system comes after flowmeter F2 meterings, the 4th is supplemented to by second flow regulating valve 6
Also it is mainly liquid phase on separator V4 inlet duct, caused tolerance during possible carrying pipe is defeated, into the 4th separator
After V4 gas-liquids point are taken the circumstances into consideration, together into plate-fin heat exchanger group E1.
Device drives to supplement refrigerant initial stage, is added to methane, nitrogen light component to coolant compressor entrance first, makes
Circulation is formed between coolant compressor and plate-fin heat exchanger group E1, is then slowly added to propane, isopentane, the first separation
Propane, isopentane in device V1 vaporize under the drive of swiftly flowing vapor phase refrigerant from bottom to top of the 3rd heat exchanger channels, and one
With return coolant compressor entrance；After dropping to about -85 DEG C Deng plate-fin heat exchanger group E1 entirety warm areas, now ethene from
Ethene stocking system is added to the 4th separator V4 through flowmeter, flow control valve, and the ethene in the 4th separator V4 is exchanging heat
Vaporized under the heat exchanger channels drives of swiftly flowing vapor phase refrigerant from bottom to top of device group E1 the 3rd, together return to refrigerant compression
Machine entrance.Finally make it that refrigerant each group distribution ratio is：N2:10mol%, C1:20mol%, C2:40mol%, C3:
15mol%, C5:15mol%, the total mole number based on all gas.
Comparative example 1
Carry out similar to Example 1ly, simply propane, isopentane, the arbitrary way of ethene are different.From coolant compressor
After one-level or two-stage compression, a hot gas line is drawn, propane, isopentane, ethene pass through propane replenishment system, isopropyl alkane respectively
Replenishment system and ethene replenishment system supplement so far hot gas line, by hot gas by after propane, isopentane, ethene heating and gasifying, mend
It is charged to coolant compressor entrance.Compared with Example 1, the hot gas decompression of foregoing extraction is back to coolant compressor entrance,
And be introduced into ice chest and play the due effect of refrigerant, the power of coolant compressor appropriate section is then wasted.Due to supplement
The all gas phases of propane, isopentane, ethene entered, into ice chest after need expend cold liquefaction, be directly added to liquid with embodiment 1
Compare, also make the increase of coolant compressor energy consumption.
Claims (8)
1. a kind of natural gas liquefaction system with refrigerant supplementary device, it includes first, second, third and fourth separation
Device, first, second, third and fourth throttling arrangement, the first and second flow control valves, the first and second flow metering devices,
And one group of plate-fin heat exchanger,
Wherein, the one-level liquid phase refrigerant pipeline from refrigerant compression systems is connected by the first heat exchanger channels in heat exchanger group
One end of first throttle device is connect, the other end of first throttle device is connected with the entrance of the first separator；
Pass through the second heat exchanger channels in heat exchanger group and the from the two level liquid phase refrigerant pipeline that refrigerant compression systems are come
One end connection of two throttling arrangements, the other end of second throttling device are connected with the entrance of the first separator, the first separator
Gaseous phase outlet and liquid-phase outlet are connected to the 3rd heat exchanger channels in heat exchanger group；
Pass through the 4th heat exchanger channels in heat exchanger group and the from the secondary gas phase refrigerant tubing that refrigerant compression systems are come
The entrance connection of two separators, the gaseous phase outlet of the second separator are throttled by the 5th heat exchanger channels in heat exchanger group and the 3rd
One end connection of device, the other end of the 3rd throttling arrangement are connected with the entrance of the 3rd separator, and the gas phase of the 3rd separator goes out
Mouth and liquid-phase outlet are connected to the 3rd heat exchanger channels in heat exchanger group；The liquid-phase outlet of second separator passes through in heat exchanger group
The 7th heat exchanger channels be connected with one end of the 4th throttling arrangement, the other end of the 4th throttling arrangement and the entrance of the 4th separator
Connection, the gaseous phase outlet and liquid-phase outlet of the 4th separator are connected to the 3rd heat exchanger channels in heat exchanger group；3rd heat exchange is logical
The other end in road returns to refrigerant compression systems；Purified natural gas pipeline connects the 6th heat exchanger channels of heat exchanger group, Ran Houlian
It is connected to LNG pipelines；
Propane/isopentane pipeline from propane, isopentane stocking system measures equipment flowmeter, connection first through first flow
The first separator inlet is connected to after flow control valve；
Ethylene conduit from ethene stocking system measures equipment flowmeter through second flow, connects after connecting second flow regulating valve
It is connected to the entrance of the 4th separator.
2. natural gas liquefaction system according to claim 1, it is characterised in that the refrigeration for hybrid refrigeration liquefaction process
Agent supplementary device further comprises the liquid-phase outlet connection one-level liquid phase refrigeration of secondary refrigerant compressibility, wherein one stage of compression
Agent pipeline, the liquid-phase outlet connection two level liquid phase refrigerant pipeline of two-stage compression, and the gaseous phase outlet connection two of two-stage compression
Level vapor phase refrigerant pipeline.
3. natural gas liquefaction system according to claim 1 or 2, it is characterised in that the gaseous phase outlet of the first separator and
Liquid-phase outlet the 3rd heat exchanger channels being connected to after converging in heat exchanger group or the 3rd heat exchange being respectively connecting in heat exchanger group
Passage；And/or
The gaseous phase outlet and liquid-phase outlet of 3rd separator are connected to the 3rd heat exchanger channels or difference in heat exchanger group after converging
The 3rd heat exchanger channels being connected in heat exchanger group；And/or
The gaseous phase outlet and liquid-phase outlet of 4th separator are connected to the 3rd heat exchanger channels or difference in heat exchanger group after converging
The 3rd heat exchanger channels being connected in heat exchanger group.
4. according to the natural gas liquefaction system any one of claim 1-3, it is characterised in that the 3rd heat exchanger channels it is another
One end returns to the entrance of the one stage of compression of refrigerant compression systems.
5. a kind of natural gas liquefaction, this method include：
Raw natural gas after purification enters plate-fin heat exchanger group, and the cold that absorption refrigeration agent discharges carries out precooling, liquefaction,
And -130 DEG C~-162 DEG C are finally cooled to, further such as -135~-155 DEG C, obtain LNG product；
The blended coolant compressor supercharging of mix refrigerant, obtained one-level liquid phase refrigerant, two level liquid phase refrigerant, two level
Vapor phase refrigerant；
The one-level liquid phase refrigerant initially enters the first heat exchanger channels of heat exchanger group, is cooled to about 0 DEG C~-30 in advance wherein
DEG C, preferably -5~-20 DEG C, throttled through first throttle valve to 0.25~0.8MPaA, the first separation is entered after preferably 0.4-0.7MPa
Device, the gas phase isolated by the first separator and liquid phase enter the 3rd heat exchanger channels of heat exchanger group after converging, and from heat exchanger
The mixed refrigerant stream stock that group rear stage heat exchanger returns converges, and provides cold for heat exchanger group, is then back to mix refrigerant
Suction port of compressor is pressurized；
By refrigerant compression systems Lai two level liquid phase refrigerant be cooled to 0 DEG C~-30 in advance by the heat exchanger channels of heat exchanger group second
DEG C, preferably -5~-20 DEG C, then throttled through second throttle to 0.25~0.8MPaA, after preferably 0.4-0.7MPa, also into
One separator carries out gas-liquid distribution；
By refrigerant compression systems Lai fourth heat exchanger channels of the secondary gas phase refrigerant through heat exchanger group, be cooled to 0 DEG C~-30
DEG C, preferably -5~-20 DEG C, subsequently into the second separator liquid separation, the gas phase isolated is entered from the top exit of the second separator
The 5th heat exchanger channels for entering heat exchanger group are cooled to -30 DEG C~-100 DEG C, preferably -40~-90 DEG C, and further such as -50~-80
DEG C, then throttled through the 3rd choke valve 3 to 0.25~0.8MPaA, enter the 3rd separator after preferably 0.4-0.7MPa, by the 3rd
The gas phase that separator is isolated enters the 3rd heat exchanger channels of heat exchanger group after converging with liquid phase, cold is provided for heat exchanger group,
Finally return that coolant compressor entrance is pressurized；The liquid phase that second separator is isolated enters from the outlet at bottom of the second separator
7th heat exchanger channels of heat exchanger group are cooled to -135 DEG C~-165 DEG C, preferably -140~-155 DEG C, then through the 4th choke valve
Throttling enters the 4th separator to 0.25~0.8MPaA after preferably 0.4-0.7MPa, the gas phase isolated by the 4th separator and
Liquid phase enters the 3rd heat exchanger channels of heat exchanger group after converging, cold is provided for heat exchanger group；
The propane come from propane, isopentane stocking system is supplemented to first after flowmeter measures by first flow regulating valve
On the inlet duct of separator, predominantly liquid phase may carry a small amount of tolerance, after being distributed into the first separator gas-liquid, one
It is same to enter plate-fin heat exchanger group；
The ethene come from ethene stocking system is supplemented to the 4th separator after flowmeter measures by second flow regulating valve
Also it is mainly liquid phase on inlet duct, caused tolerance during possible carrying pipe is defeated, takes the circumstances into consideration into the 4th separator gas-liquid point
Afterwards, together into plate-fin heat exchanger group.
6. natural gas liquefaction according to claim 5, it is characterised in that natural gas liquefaction device drive initial stage according to
It is secondary to be added to methane and nitrogen gas refrigerant, make to form circulation between coolant compressor and plate-fin heat exchanger group, then successively
It is added to propane, isopentane, the propane, isopentane in the first separator are in the 3rd heat exchanger channels swiftly flowing gas from bottom to top
Vaporized under the drive of phase refrigerant, together return to coolant compressor entrance；Decline (example Deng plate-fin heat exchanger group entirety warm area
Such as drop to -100~-70 DEG C) after, now ethene is mended from ethene stocking system through second flowmeter, second flow regulating valve
It is filled with the 4th separator, the ethene in the 4th separator is in the heat exchanger channels of heat exchanger group the 3rd swiftly flowing gas phase from bottom to top
Vaporized under the drive of refrigerant, together return to coolant compressor entrance.Driving initial stage not by this approach make-up ethylene, in order to avoid
The poly- drop of plate-fin heat exchanger group local temperature, produces potential safety hazard.
7. the natural gas liquefaction according to claim 5 or 6, it is characterised in that driven just in natural gas liquefaction device
Phase is added to methane and nitrogen gas refrigerant successively, makes to form circulation between coolant compressor and plate-fin heat exchanger group, then
Propane, isopentane are added to successively, is then added to methane and nitrogen gas refrigerant successively again, are then added to propane, different successively
Pentane, repeat one or more circulations.
8. the natural gas liquefaction according to claim 5 or 6, it is characterised in that successively supplement methane, nitrogen, propane,
Isopentane, ethene so that finally each group distribution ratio is：N2:5mol%-25mol%, C1:10mol%-25mol%, C2:
30mol%-55mol%, C3:10mol%-25mol%, C5:10mol%-25mol%, the total moles based on all gas
Number.
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