CN107436072B - 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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- CN107436072B CN107436072B CN201710691412.8A CN201710691412A CN107436072B CN 107436072 B CN107436072 B CN 107436072B CN 201710691412 A CN201710691412 A CN 201710691412A CN 107436072 B CN107436072 B CN 107436072B
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- 239000003507 refrigerant Substances 0.000 title claims abstract description 133
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 92
- 239000003345 natural gas Substances 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 34
- 238000005057 refrigeration Methods 0.000 claims abstract description 17
- 239000007791 liquid phase Substances 0.000 claims description 81
- 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 66
- 239000007789 gas Substances 0.000 claims description 48
- 239000012071 phase Substances 0.000 claims description 44
- 230000006835 compression Effects 0.000 claims description 38
- 238000007906 compression Methods 0.000 claims description 38
- 239000001294 propane Substances 0.000 claims description 35
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 34
- 239000005977 Ethylene Substances 0.000 claims description 34
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims description 33
- 239000002826 coolant Substances 0.000 claims description 25
- 238000001816 cooling Methods 0.000 claims description 23
- 239000007788 liquid Substances 0.000 claims description 22
- 238000000926 separation method Methods 0.000 claims description 15
- 239000007792 gaseous phase Substances 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 230000001105 regulatory effect Effects 0.000 claims description 12
- 230000004087 circulation Effects 0.000 claims description 10
- 239000012808 vapor phase Substances 0.000 claims description 10
- 239000013589 supplement Substances 0.000 claims description 8
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 6
- 239000000047 product Substances 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical group CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims 2
- 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
- 230000007423 decrease Effects 0.000 description 2
- 230000006837 decompression Effects 0.000 description 1
- 230000000694 effects Effects 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 refrigeration cycle of hybrid refrigeration liquefaction process, device includes four separators, four throttling sets, two flow control valves, two flow metering devices, one group of plate-fin heat exchanger.Period 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) productions using hybrid refrigeration liquefaction process, and in particular to one kind has refrigerant
The natural gas liquefaction system and natural gas liquefaction of supplementary device.
Background technique
With the growth of Natural Gas Consumption Using, most effective for one of form as natural gas, liquefied natural gas becomes
One of fastest-rising field of energy market.The continuous development of liquefied natural gas industry, exists to natural gas liquefaction and device
More stringent requirements are proposed for energy consumption, investment and efficiency etc..
Currently, the natural gas liquefaction process of comparative maturity mainly has: cascaded refrigeration process, swell refrigeration technique and mixing system
Cold technique.Hybrid refrigeration process therein then compares the favor by medium-sized natural gas liquefaction device, but other opposite refrigeration process
For, hybrid refrigeration process there is mix refrigerant component proportion is more difficult, drive period longer disadvantage by device.Mixing
Component in refrigerant, such as propane, isopentane are to be added in refrigerant compression cycle in liquid form, need and its
Become 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 period is significantly elongated.The present invention proposes a kind of novel refrigerant compensation process and its device, can reduce refrigerant benefit
Difficulty is filled, the period of driving is shortened.
Summary of the invention
The present invention provides a kind of refrigerant compensation process and device for hybrid refrigeration liquefaction process, are used for use
Refrigerant is supplemented in the refrigerant-cycle systems of the natural gas liquefaction device of hybrid refrigeration liquefaction process, driving process can be simplified,
Shorten the period of driving.
A kind of natural gas liquefaction system with refrigerant supplementary device of the present invention comprising first, second,
Three and the 4th separator, the first, second, third and fourth throttling set, 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 level-one 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 throttling device, and the other end of first throttling device is connect with the entrance of the first separator；
The second level liquid phase refrigerant pipeline come from refrigerant compression systems passes through the second heat exchanger channels in heat exchanger group
It is connect with one end of second throttling device, the other end of second throttling device is connect with the entrance of the first separator, the first separation
The gaseous phase outlet and liquid-phase outlet of device are connected to the third 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 connect with the entrance of the second separator, the gaseous phase outlet of the second separator passes through the 5th heat exchanger channels and third in heat exchanger group
One end of throttling set connects, and the other end of third throttling set is connect with the entrance of third separator, the gas of third separator
Mutually outlet and liquid-phase outlet are connected to the third 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 connect with one end of the 4th throttling set, the other end of the 4th throttling set and the 4th separator
Entrance connection, the gaseous phase outlet and liquid-phase outlet of the 4th separator are connected to the third heat exchanger channels in heat exchanger group；Third is changed
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 pipeline；
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 ethylene stocking system measures equipment flowmeter through second flow, connects second flow regulating valve
It is connected to the entrance of the 4th separator afterwards.
It further, further comprise secondary refrigerant compression for the refrigerant supplementary device of hybrid refrigeration liquefaction process
System, wherein the liquid-phase outlet of one stage of compression connects level-one liquid phase refrigerant pipeline, and the liquid-phase outlet of two-stage compression connects second level
The gaseous phase outlet of liquid phase refrigerant pipeline and two-stage compression connects secondary gas phase refrigerant tubing.
Further, the third that the gaseous phase outlet of the first separator and liquid-phase outlet are connected in heat exchanger group after converging is changed
The passage of heat or the third heat exchanger channels being respectively connected in heat exchanger group；And/or
The gaseous phase outlet and liquid-phase outlet of third separator be connected to after converging third heat exchanger channels in heat exchanger group or
The third heat exchanger channels being respectively connected in heat exchanger group；And/or
The gaseous phase outlet and liquid-phase outlet of 4th separator be connected to after converging third heat exchanger channels in heat exchanger group or
The third heat exchanger channels being respectively connected in heat exchanger group.
Further, the other end of third 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 for using above system, process flow is as follows:
Purified raw natural gas enters plate-fin heat exchanger group, absorb the cooling capacity that refrigerant releases be pre-chilled,
Liquefaction, and -130 DEG C~-162 DEG C are finally cooled to, further such as -135~-155 DEG C, obtain LNG product；
Mix refrigerant (C1~C5 and N2 or be made of the C1~C5 and N2 of arbitrary proportion) including arbitrary proportion is through mixed
Close coolant compressor pressurization, obtained level-one liquid phase refrigerant, second level liquid phase refrigerant, secondary gas phase refrigerant；
The level-one 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 throttle through first throttle valve to 0.25~0.8MPaA, and the is entered after preferably 0.4-0.7MPa
One separator, the gas phase isolated by the first separator and liquid phase enter the third 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 cooling capacity for heat exchanger group, then returns to mixing
The pressurization of coolant compressor entrance；
By refrigerant compression systems Lai second level liquid phase refrigerant be cooled to 0 DEG C in advance by the second heat exchanger channels of heat exchanger group
~-30 DEG C, preferably -5~-20 DEG C, then throttle through second throttle to 0.25~0.8MPaA, after preferably 0.4-0.7MPa, also into
Enter the first separator and 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 top of the gas phase isolated from the second separator goes out
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
It~-80 DEG C, then throttles through third throttle valve 3 to 0.25~0.8MPaA, third separator is entered after preferably 0.4-0.7MPa,
The gas phase and liquid phase isolated by third separator enter the third heat exchanger channels of heat exchanger group after converging, provide for heat exchanger group
Cooling capacity finally returns that coolant compressor entrance is pressurized；The bottom of the liquid phase that second separator is isolated from the second separator goes out
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
Throttle valve throttles to 0.25~0.8MPaA, and the 4th separator is entered after preferably 0.4-0.7MPa, is isolated by the 4th separator
Gas phase and liquid phase enter the third heat exchanger channels of heat exchanger group after converging, provide cooling capacity for heat exchanger group；
From the next propane of propane, isopentane stocking system, isopentane after flowmeter measures, by first flow regulating valve
It is supplemented on the inlet duct of the first separator, predominantly liquid phase, a small amount of tolerance may be carried, into the first separator gas-liquid
After distribution, enter plate-fin heat exchanger group together；
The ethylene come from ethylene stocking system is supplemented to the 4th separation after flowmeter measures, by second flow regulating valve
Mainly also it is liquid phase on the inlet duct of device, the defeated tolerance generated in the process of pipe may be carried, into the 4th separator gas-liquid point
After as one sees fit, enter plate-fin heat exchanger group together.
Further, methane and nitrogen gas refrigerant are successively supplemented at natural gas liquefaction device driving initial stage, makes refrigerant pressure
Circulation is formed between contracting machine and plate-fin heat exchanger group, is then slowly successively added to propane, isopentane, in the first separator
Propane, isopentane vaporize under third the heat exchanger channels from bottom to top drive of swiftly flowing vapor phase refrigerant, return to system together
Refrigerant compressor entrance；After equal plate-fin heat exchangers group entirety warm area decline (such as dropping to -100~-70 DEG C), second at this time
Alkene is added to the 4th separator through second flowmeter, second flow regulating valve from ethylene stocking system, the second in the 4th separator
Alkene vaporizes under the drive of swiftly flowing vapor phase refrigerant from bottom to top of heat exchanger group third heat exchanger channels, returns to refrigeration together
Agent suction port of compressor.Driving initial stage does not pass through this approach make-up ethylene, in case the poly- drop of plate-fin heat exchanger group local temperature, generates
Security risk.
Further, it is successively added to methane and nitrogen gas refrigerant at natural gas liquefaction device driving initial stage, makes refrigerant
Circulation is formed between compressor and plate-fin heat exchanger group, is then successively added to propane, isopentane, is then successively added to again
Methane and nitrogen gas refrigerant are then successively added to propane, isopentane, repeat one or more circulations, such as 2-5 circulation.
Component is successively supplemented from light to heavy, and it is not especially to limit that magnitude of recruitment, flow velocity, which depend on the scale of specific natural gas liquefaction device,
, it can be determined by site operation personnel, supplement speed speed only influences the time of driving；It is generally 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 are as follows: 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:
It is stored in the cryogen liquid separation tank of liquid phase originally 1. ethylene, propane, isopentane etc. are directly added to, more former supplement
To coolant compressor entrance, and the compensation process that each component vaporizes need to be compared, process is more simple, can save driving week
Phase.
2. being to eliminate each component by liquid phase by another advantage that each refrigerant component is directly added to cryogen liquid separation tank
Become vapour phase, then become the process of liquid phase again, the compression power consumption and plate-fin heat exchanger of coolant compressor can be saved
In cooling capacity.
Detailed description of the invention
Fig. 1 is process flow chart of the present invention.
Specific embodiment
It further illustrates with reference to the accompanying drawing:
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 sets, two flow control valves, two flow metering devices, one group of plate-fin heat exchanger.
By refrigerant compression systems Lai level-one liquid phase refrigerant pipeline pass through the first heat exchanger channels in heat exchanger group E1
One end of first throttling device 1 is connected, the other end of first throttling device 1 is connect with the entrance of the first separator V1；By freezing
The second level liquid phase refrigerant pipeline that agent compressibility comes passes through the second heat exchanger channels and second throttling device 2 in heat exchanger group E1
One end connection, the other end of second throttling device 2 connect with the entrance of the first separator V1, the gas phase of the first separator V1 and
Liquid-phase outlet is connected to the third heat exchanger channels in heat exchanger group E1；By refrigerant compression systems Lai secondary gas phase refrigerant pipe
Road is connect by the 4th heat exchanger channels in heat exchanger group E1 with the entrance of the second separator V2, and the gas phase of the second separator V2 goes out
Mouthful connect by the 5th heat exchanger channels in heat exchanger group E1 with one end of third throttling set 3, third throttling set 3 it is another
End is connect with the entrance of third separator V3, and the gas phase and liquid-phase outlet of third separator V3 is connected to the in heat exchanger group E1
Three heat exchanger channels；The liquid-phase outlet of second separator V2 passes through the 7th heat exchanger channels and the 4th throttling set in heat exchanger group E1
4 one end connection, the other end of the 4th throttling set 4 are connect with the entrance of the 4th separator V4, the gas phase of the 4th separator V4
And liquid-phase outlet is connected to the third heat exchanger channels in heat exchanger group E1；The other end of third heat exchanger channels returns to refrigerant compression
System；Purified natural gas pipeline connects the 6th heat exchanger channels of heat exchanger group E1, is then attached to LNG pipeline；
Propane/isopentane pipeline from propane, isopentane stocking system measures equipment flowmeter F1 through first flow, even
The first separator V1 entrance is connected to after connecing first flow regulating valve 5；
Ethylene conduit from ethylene stocking system measures equipment flowmeter F2 through second flow, and connection second flow is adjusted
The entrance of the 4th separator V4 is connected to after valve 6.
For the refrigerant compensation process of hybrid refrigeration liquefaction process, process flow is as follows:
As shown in Fig. 1, purified raw natural gas enters plate-fin heat exchanger group E1, absorbs what refrigerant released
Cooling capacity is pre-chilled, is liquefied, and is finally cooled to -130 DEG C~-162 DEG C, obtains LNG product；
Mix refrigerant is made of C1~C5 and N2, and through mix refrigerant compressor boost, obtained level-one liquid phase system
Cryogen, second 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 level-one liquid phase refrigerant initially enter the first heat exchanger channels of heat exchanger group E1, In
Wherein it is cooled to about 0 DEG C~-30 DEG C in advance, enters the first separator V1 after the throttling to 0.25~0.8MPaA of first throttle valve 1,
The gas phase isolated by the first separator V1 and liquid phase enter the third heat exchanger channels of heat exchanger group E1 after converging, and from heat exchanger
The mixed refrigerant stream stock that group E1 rear stage heat exchanger returns converges, and provides cooling capacity for heat exchanger group E1, then returns to mixing system
The pressurization of refrigerant compressor entrance；By refrigerant compression systems Lai second level liquid phase refrigerant it is logical by the heat exchange of heat exchanger group E1 second
Road is cooled to 0 DEG C~-30 DEG C in advance, then after the throttling to 0.25~0.8MPaA of second throttle 2, also enter the first separator V1 into
The distribution of promoting the circulation of qi liquid；By refrigerant compression systems Lai fourth heat exchanger channels of the secondary gas phase refrigerant through heat exchanger group E1, it is cooling
To 0 DEG C~-30 DEG C, subsequently into the second separator V2 liquid separation, the gas phase isolated from the top exit of the second separator V2 into
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 third throttle valve 3~
Enter third separator V3 after 0.8MPaA, the gas phase isolated by third separator V3 and liquid phase enter heat exchanger group after converging
The third heat exchanger channels of E1 provide cooling capacity for heat exchanger group E1, finally return that coolant compressor entrance is pressurized；Second separator
The 7th heat exchanger channels that the outlet at bottom of the liquid phase that V2 is isolated from the second separator V2 enter heat exchanger group E1 are cooled to -135
DEG C~-165 DEG C, then enter the 4th separator V4 after the 4th throttle valve 4 throttles to 0.25~0.8MPaA, by the 4th separation
The gas phase and liquid phase that device V4 is isolated enter the third heat exchanger channels of heat exchanger group E1 after converging, provide for heat exchanger group E1 cold
Amount；
From the next propane of propane, isopentane stocking system, isopentane after flowmeter F1 metering, adjusted by first flow
Valve 5 is supplemented on the inlet duct of the first separator V1, predominantly liquid phase, may carry a small amount of tolerance, into the first separation
After the distribution of device V1 gas-liquid, enter plate-fin heat exchanger group E1 together；
The ethylene come from ethylene stocking system is supplemented to the 4th by second flow regulating valve 6 after flowmeter F2 metering
Mainly also it is liquid phase on the inlet duct of separator V4, the defeated tolerance generated in the process of pipe may be carried, into the 4th separator
After V4 gas-liquid point is taken the circumstances into consideration, enter plate-fin heat exchanger group E1 together.
Device driving initial stage supplements refrigerant, 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, is then slowly added to propane, isopentane, first point
It is vaporized under third the heat exchanger channels from bottom to top drive of swiftly flowing vapor phase refrigerant from propane, the isopentane in device V1,
Coolant compressor entrance is returned together；After equal plate-fin heat exchangers group E1 entirety warm area decline, ethylene is stored up from ethylene at this time
Deposit system is added to the 4th separator V4 through flowmeter, flow control valve, and the ethylene in the 4th separator V4 is in heat exchanger group E1
It is vaporized under the drive of swiftly flowing vapor phase refrigerant from bottom to top of third heat exchanger channels, returns to coolant compressor together and enter
Mouthful.Driving initial stage does not pass through this approach make-up ethylene, in case the poly- drop of plate-fin heat exchanger group E1 local temperature, it is hidden to generate safety
Suffer from.
Embodiment 1
As shown in Fig. 1, purified raw natural gas enters plate-fin heat exchanger group E1, absorbs what refrigerant released
Cooling capacity is pre-chilled, is liquefied, and is finally cooled to -141 DEG C, obtains LNG product；
Mix refrigerant is by C1~C5 and N2It forms, and through mix refrigerant compressor boost, obtained level-one liquid phase system
Cryogen, second 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 level-one liquid phase refrigerant initially enter the first heat exchanger channels of heat exchanger group E1, In
Wherein it is cooled to about -15 DEG C in advance, enters the first separator V1 after the throttling to 0.5MPaA of first throttle valve 1, by the first separator
The gas phase and liquid phase that V1 is isolated enter the third heat exchanger channels of heat exchanger group E1 after converging, change with from heat exchanger group E1 rear stage
The mixed refrigerant stream stock that hot device returns converges, and provides cooling capacity for heat exchanger group E1, then returns to mix refrigerant compressor and enters
Mouth pressurization；By refrigerant compression systems Lai second level liquid phase refrigerant be cooled to -18 in advance by the second heat exchanger channels of heat exchanger group E1
DEG C, then after the throttling to 0.5MPaA of second throttle 2, also enter the first separator V1 and carry out gas-liquid distribution；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 separation, the 5th heat exchanger channels that the top exit of the gas phase isolated from the second separator V2 enter heat exchanger group E1 are cooling
To -60 DEG C, then enters third separator V3 after third throttle valve 3 throttles to 0.5MPaA, isolated by third separator V3
Gas phase and liquid phase converge after enter heat exchanger group E1 third heat exchanger channels, provide cooling capacity for heat exchanger group E1, finally return that
The pressurization of coolant compressor entrance；The outlet at bottom of the liquid phase that second separator V2 is isolated from the second separator V2 enter heat exchange
The 7th heat exchanger channels of device group E1 are cooled to -145 DEG C, then enter the 4th point after the 4th throttle valve 4 throttles to about 0.5MPaA
From device V4, the gas phase isolated by the 4th separator V4 enters the third heat exchanger channels of heat exchanger group E1 after converging with liquid phase, is
Heat exchanger group E1 provides cooling capacity；
From the next propane of propane, isopentane stocking system, isopentane after flowmeter F1 metering, adjusted by first flow
Valve 5 is supplemented on the inlet duct of the first separator V1, predominantly liquid phase, may carry a small amount of tolerance, into the first separation
After the distribution of device V1 gas-liquid, enter plate-fin heat exchanger group E1 together；
The ethylene come from ethylene stocking system is supplemented to the 4th by second flow regulating valve 6 after flowmeter F2 metering
Mainly also it is liquid phase on the inlet duct of separator V4, the defeated tolerance generated in the process of pipe may be carried, into the 4th separator
After V4 gas-liquid point is taken the circumstances into consideration, enter plate-fin heat exchanger group E1 together.
Device driving initial stage supplements refrigerant, 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 third the heat exchanger channels from bottom to top drive of swiftly flowing vapor phase refrigerant, and one
With return coolant compressor entrance；Equal plate-fin heat exchangers group E1 entirety warm area drops to after about -85 DEG C, at this time ethylene from
Ethylene stocking system is added to the 4th separator V4 through flowmeter, flow control valve, and the ethylene in the 4th separator V4 is exchanging heat
It is vaporized under the drive of swiftly flowing vapor phase refrigerant from bottom to top of device group E1 third heat exchanger channels, returns to refrigerant compression together
Machine entrance.Finally make refrigerant each group distribution ratio are as follows: N2:10mol%, C1:20mol%, C2:40mol%, C3:
15mol%, C5:15mol%, the total mole number based on all gas.
Comparative example 1
It carries out similar to Example 1ly, only propane, isopentane, the arbitrary way of ethylene are different.From coolant compressor
After level-one or two-stage compression, a hot gas line is drawn, propane, isopentane, ethylene pass through propane replenishment system, isopropyl alkane respectively
So far hot gas line is mended by hot gas by after propane, isopentane, ethylene heating and gasifying for replenishment system and ethylene replenishment system supplement
It is charged to coolant compressor entrance.Compared with Example 1, the hot gas decompression of aforementioned extraction is back to coolant compressor entrance,
And do not enter ice chest and play the due effect of refrigerant, the power of coolant compressor corresponding portion is then wasted.Due to supplement
The all gas phases of propane, isopentane, ethylene entered, into ice chest after need expend cooling capacity liquefaction, be directly added to liquid with embodiment 1
It compares, also increases coolant compressor energy consumption.
Claims (9)
1. a kind of natural gas liquefaction system with refrigerant supplementary device comprising the first, second, third and fourth separation
Device, the first, second, third and fourth throttling set, the first and second flow control valves, the first and second flow metering devices,
And one group of plate-fin heat exchanger,
Wherein, the level-one liquid phase refrigerant pipeline from refrigerant compression systems is connected by the first heat exchanger channels in heat exchanger group
One end of first throttling device is connect, the other end of first throttling device is connect with the entrance of the first separator；
The second level liquid phase refrigerant pipeline come from refrigerant compression systems passes through the second heat exchanger channels in heat exchanger group and the
One end of two throttling sets connects, and the other end of second throttling device is connect with the entrance of the first separator, the first separator
Gaseous phase outlet and liquid-phase outlet are connected to the third 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 and the
The entrance of two separators connects, and the gaseous phase outlet of the second separator is throttled by the 5th heat exchanger channels in heat exchanger group with third
One end of device connects, and the other end of third throttling set is connect with the entrance of third separator, and the gas phase of third separator goes out
Mouth and liquid-phase outlet are connected to the third 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 connect with one end of the 4th throttling set, the other end of the 4th throttling set and the entrance of the 4th separator
Connection, the gaseous phase outlet and liquid-phase outlet of the 4th separator are connected to the third heat exchanger channels in heat exchanger group；Third 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, then connects
It is connected to LNG pipeline；
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 ethylene 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, which is characterized in that the refrigeration for hybrid refrigeration liquefaction process
Agent supplementary device further comprises secondary refrigerant compressibility, wherein the liquid-phase outlet connection level-one liquid phase refrigeration of one stage of compression
Agent pipeline, the gaseous phase outlet connection two of the liquid-phase outlet connection second level liquid phase refrigerant pipeline and two-stage compression of two-stage compression
Grade vapor phase refrigerant pipeline.
3. natural gas liquefaction system according to claim 1 or 2, which is characterized in that the gaseous phase outlet of the first separator and
The third heat exchanger channels or the third heat exchange being respectively connected in heat exchanger group that liquid-phase outlet is connected in heat exchanger group after converging
Channel；And/or
The gaseous phase outlet and liquid-phase outlet of third separator are connected to third heat exchanger channels or difference in heat exchanger group after converging
The third 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 third heat exchanger channels or difference in heat exchanger group after converging
The third heat exchanger channels being connected in heat exchanger group.
4. natural gas liquefaction system according to claim 2, which is characterized in that the other end of third heat exchanger channels returns to system
The entrance of the one stage of compression of cryogen compressibility.
5. a kind of natural gas liquefaction, this method comprises:
Purified raw natural gas enters plate-fin heat exchanger group, absorbs the cooling capacity that refrigerant releases and is pre-chilled, is liquefied,
And -130 DEG C~-162 DEG C are finally cooled to, obtain LNG product；
Mix refrigerant is through mix refrigerant compressor boost, obtained level-one liquid phase refrigerant, second level liquid phase refrigerant, second level
Vapor phase refrigerant；
The level-one liquid phase refrigerant initially enters the first heat exchanger channels of heat exchanger group, is cooled to 0 DEG C~-30 in advance wherein
DEG C, the first separator is entered after first throttle valve throttles to 0.25~0.8MPaA, the gas phase isolated by the first separator with
Liquid phase enters the third heat exchanger channels of heat exchanger group after converging, with the mix refrigerant returned from heat exchanger group rear stage heat exchanger
Stream stock converges, and provides cooling capacity for heat exchanger group, then returns to the pressurization of mix refrigerant suction port of compressor；
By refrigerant compression systems Lai second level liquid phase refrigerant be cooled to 0 DEG C~-30 in advance by the second heat exchanger channels of heat exchanger group
DEG C, then throttle through second throttle to 0.25~0.8MPaA, also enter the first separator and 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, subsequently into the second separator liquid separation, the top exit of the gas phase isolated from the second separator enters the of heat exchanger group
Five heat exchanger channels are cooled to -30 DEG C~-100 DEG C, then enter third after third throttle valve 3 throttles to 0.25~0.8MPaA
Separator, the gas phase isolated by third separator and liquid phase enter the third heat exchanger channels of heat exchanger group after converging, for heat exchange
Device group provides cooling capacity, finally returns that coolant compressor entrance is pressurized；The liquid phase that second separator is isolated is from the second separator
Outlet at bottom enter the 7th heat exchanger channels of heat exchanger group and be cooled to -135 DEG C~-165 DEG C, then throttle through the 4th throttle valve
Enter the 4th separator after to 0.25~0.8MPaA, the gas phase isolated by the 4th separator and liquid phase enter heat exchange after converging
The third heat exchanger channels of device group provide cooling capacity for heat exchanger group；
From the next propane of propane, isopentane stocking system, isopentane after flowmeter measures, supplemented by first flow regulating valve
To the inlet duct of the first separator, into after the distribution of the first separator gas-liquid, enter plate-fin heat exchanger group together；
The ethylene come from ethylene stocking system is supplemented to the 4th separator by second flow regulating valve after flowmeter measures
On inlet duct, into after the distribution of the 4th separator gas-liquid, enter plate-fin heat exchanger group together.
6. natural gas liquefaction according to claim 5, which is characterized in that purified raw natural gas enters plate wing
Formula heat exchanger group absorbs the cooling capacity that refrigerant releases and is pre-chilled, is liquefied, and is finally cooled to -135~-155 DEG C, obtains
LNG product；
Mix refrigerant is through mix refrigerant compressor boost, obtained level-one liquid phase refrigerant, second level liquid phase refrigerant, second level
Vapor phase refrigerant；
The level-one liquid phase refrigerant initially enters the first heat exchanger channels of heat exchanger group, is cooled to -5~-20 DEG C in advance wherein,
Enter the first separator after first throttle valve throttles to 0.4-0.7MPa, the gas phase and liquid phase isolated by the first separator are converged
The third heat exchanger channels for entering heat exchanger group after conjunction converge with the mixed refrigerant stream stock returned from heat exchanger group rear stage heat exchanger
It closes, provides cooling capacity for heat exchanger group, then return to the pressurization of mix refrigerant suction port of compressor；
By refrigerant compression systems Lai second level liquid phase refrigerant be cooled to -5~-20 in advance by the second heat exchanger channels of heat exchanger group
DEG C, then throttle through second throttle to 0.4-0.7MPa, also enter the first separator and 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 -5~-20
DEG C, subsequently into the second separator liquid separation, the top exit of the gas phase isolated from the second separator enters the of heat exchanger group
Five heat exchanger channels are cooled to -50~-80 DEG C, then enter third separator after third throttle valve 3 throttles to 0.4-0.7MPa,
The gas phase and liquid phase isolated by third separator enter the third heat exchanger channels of heat exchanger group after converging, provide for heat exchanger group
Cooling capacity finally returns that coolant compressor entrance is pressurized；The bottom of the liquid phase that second separator is isolated from the second separator goes out
The 7th heat exchanger channels that mouth enters heat exchanger group are cooled to -140~-155 DEG C, then throttle through the 4th throttle valve to 0.4-
Enter the 4th separator after 0.7MPa, the gas phase isolated by the 4th separator and liquid phase enter the third of heat exchanger group after converging
Heat exchanger channels provide cooling capacity for heat exchanger group.
7. natural gas liquefaction according to claim 5 or 6, which is characterized in that drive just in natural gas liquefaction device
Phase is successively added to methane and nitrogen gas refrigerant, makes to form circulation between coolant compressor and plate-fin heat exchanger group, then
It is successively added to propane, isopentane, the propane, isopentane in the first separator are in third heat exchanger channels flow at high speed from bottom to top
Vapor phase refrigerant drive under vaporize, together return coolant compressor entrance；Under equal plate-fin heat exchangers group entirety warm area
After being down within the scope of -100 DEG C~-70 DEG C, ethylene is from ethylene stocking system through second flowmeter, second flow regulating valve at this time
It is added to the 4th separator, the ethylene in the 4th separator is in heat exchanger group third heat exchanger channels swiftly flowing gas from bottom to top
It is vaporized under the drive of phase refrigerant, returns to coolant compressor entrance together；Driving initial stage does not pass through this approach make-up ethylene, with
Exempt from the poly- drop of plate-fin heat exchanger group local temperature, generates security risk.
8. natural gas liquefaction according to claim 5 or 6, which is characterized in that drive just in natural gas liquefaction device
Phase is successively added to methane and nitrogen gas refrigerant, makes to form circulation between coolant compressor and plate-fin heat exchanger group, then
It is successively added to propane, isopentane, is then successively added to methane and nitrogen gas refrigerant again, is then successively added to propane, different
Pentane repeats one or more circulations.
9. natural gas liquefaction according to claim 5 or 6, which is characterized in that successively supplement methane, nitrogen, propane,
Isopentane, ethylene, so that final each group distribution ratio are as follows: 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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