CN102636000A - Method for refrigerating liquefied natural gas by aid of single mixed working medium and device - Google Patents
Method for refrigerating liquefied natural gas by aid of single mixed working medium and device Download PDFInfo
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- CN102636000A CN102636000A CN2012100644495A CN201210064449A CN102636000A CN 102636000 A CN102636000 A CN 102636000A CN 2012100644495 A CN2012100644495 A CN 2012100644495A CN 201210064449 A CN201210064449 A CN 201210064449A CN 102636000 A CN102636000 A CN 102636000A
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- 238000000034 method Methods 0.000 title claims abstract description 27
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 115
- 239000012530 fluid Substances 0.000 claims abstract description 53
- 239000007789 gas Substances 0.000 claims abstract description 52
- 238000007906 compression Methods 0.000 claims abstract description 22
- 230000006835 compression Effects 0.000 claims abstract description 19
- 238000003860 storage Methods 0.000 claims abstract description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 64
- 239000012071 phase Substances 0.000 claims description 33
- 239000003345 natural gas Substances 0.000 claims description 32
- 239000007791 liquid phase Substances 0.000 claims description 23
- 239000004215 Carbon black (E152) Substances 0.000 claims description 22
- 229930195733 hydrocarbon Natural products 0.000 claims description 22
- 150000002430 hydrocarbons Chemical class 0.000 claims description 22
- 238000000926 separation method Methods 0.000 claims description 17
- 238000005057 refrigeration Methods 0.000 claims description 15
- 210000000689 upper leg Anatomy 0.000 claims description 15
- 239000012808 vapor phase Substances 0.000 claims description 6
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 3
- 239000003507 refrigerant Substances 0.000 abstract description 3
- 238000009825 accumulation Methods 0.000 abstract 1
- 238000001816 cooling Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000003915 liquefied petroleum gas Substances 0.000 description 4
- 241000521257 Hydrops Species 0.000 description 3
- 206010030113 Oedema Diseases 0.000 description 3
- 239000000126 substance Substances 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 244000188472 Ilex paraguariensis Species 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—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
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a method for refrigerating liquefied natural gas by the aid of a single mixed working medium and a device. The device comprises a mixed working medium compressor, a cooler, a gas and liquid separator, a throttling device, a plate-fin heat exchanger group and an LNG (liquefied natural gas) storage tank. In the technological process, mixed refrigerant is compressed and separated step by step, and gas compression power consumption is reduced. Heat exchange curves of cold fluid and hot fluid in a total heat exchange process match with each other better by the aid of multi-stage heat exchange, and flow of the mixed refrigerant is reduced effectively. In addition, the technological process is excellently adaptable to variable-load operation of the device, and liquid accumulation at the bottom of a refrigerating box can be avoided effectively.
Description
Technical field
The present invention relates to be rich in the liquefaction production of hydrocarbon gas, be specifically related to a kind of method and apparatus of single mixed working fluid refrigeration liquefying natural gas.
Background technology
Natural gas is owing to its feature of environmental protection becomes the optimisation substance that replaces other fuel, and its application expands aspects such as generating, automobile usefulness gas, industrial gas, city dweller's usefulness gas, chemical industry usefulness gas gradually to.
Along with the growth of natural gas consumption amount, the most effectively supply with one of form as natural gas, the volume of trade of liquefied natural gas has also become one of fastest-rising field of energy market.The continuous development of liquefied natural gas industry is then had higher requirement at aspects such as energy consumption, investment and efficient to natural gas liquefaction and device.
At present, the natural gas liquefaction process of comparative maturity mainly contains: stepwise refrigeration process, swell refrigeration technology and mixed working fluid refrigeration process.Single mixed working fluid refrigeration process wherein then relatively receives the favor of medium-sized LNG device.
In the natural gas liquefaction of existing single mixed working fluid refrigeration, the cryogen compressibility is the secondary compression, and the one-level heat exchange is adopted in natural gas liquefaction.
Existing technology: as shown in Figure 1; The device of its use comprises 21,22, two gas- liquid separators 31,32 of 1, two cooler of a motor-driven two-period form mixed working fluid compressor; Two liquid pump 4,4 ', one platen fin heat exchangers 8 and a LNG storage tank 9; The mixed working fluid of being made up of C1～C5 and N2 is through getting into the inlet of compressor behind the rational proportion; Be compressed to 0.6～1MPa through one section; Get into the one-level cooler and be cooled to 30～40 ℃; Get into the one-level knockout drum again and carry out gas-liquid separation, the isolated gas in one-level knockout drum top continues to get into two sections inlets of compressor, is compressed to 1.6～2.5MPa through two sections; One-level is separated the bottom and is separated the liquid that the obtains gas through liquid pump pressurization back and two sections compressor outlets and be mixed into secondary coolers and be cooled to 30～40 ℃; Cooled mixed working fluid gets into the secondary knockout drum subsequently and carries out gas-liquid separation, and the liquid after the separation mixes the laggard plate-fin heat exchanger of going into through secondary liquid pump pressurization back and gas that this separator top obtains, and this plate-fin heat exchanger is returned in throttling again after precooling to the uniform temperature; For whole heat transfer process provides cold, natural gas is through getting in the LNG storage tank behind the plate-fin heat exchanger.
In above-mentioned technology; For guaranteeing that liquids and gases get into same plate-fin heat exchanger passage and participate in heat exchange; The liquid of final stage gas-liquid separator bottom must pressurize to overcome the head of liquid that difference in height that the separator bottom liquid exports to plate-fin heat exchanger top cryogen inlet is brought, and must realize through increasing final stage liquid pump.Cryogen and the natural gas heat transfer process in plate-fin heat exchanger is the one-level heat exchange; The optimization of heat transfer temperature difference receives certain limitation between the stream thigh, and plant energy consumption is higher, and; This kind flow process is easy to generate ice chest bottom hydrops, and the varying duty running of installing is not had excellent adaptability.
Summary of the invention
The invention provides a kind of method and apparatus that adopts single mixed working fluid refrigeration liquefying natural gas.This invention adopts single mixed working fluid refrigeration to make natural gas liquefaction.
The present invention adopts single mixed working fluid to freeze to come the method and apparatus of liquefied natural gas, and it is divided into natural gas circulation and mixed working fluid kind of refrigeration cycle.In the mixed working fluid loop, mixed working fluid is followed gas-liquid separation step by step in the compression process step by step simultaneously at it, and one-level is compressed isolated liquid phase stream thigh and do not participated in follow-up compression process, has effectively reduced postorder gas compression power consumption; The gas phase that obtains through compression flows the different passage throttling heat exchange that stock does not get into heat exchanger package with liquid-phase mixing working medium; Relatively traditional handicraft has been saved final stage liquid pump, and adopts multi-stage heat exchanger to make that the heat exchange curve of hot-fluid thigh and cold flow thigh more matees in the whole process; The final stage gas phase gets into the cryogen separator after the re-heat of backflowing after the throttling, can effectively avoid the ice chest hydrops.
The present invention relates to adopt the device of single mixed working fluid refrigeration liquefying natural gas; It comprises azeotrope compressibility and ice chest system; Wherein the compressibility of mix refrigerant adopts two-period form mixed working fluid compressor compresses; Comprise a two-period form mixed working fluid compressor, two coolers, two gas-liquid separators and a liquid pump, the ice chest system comprises one group of plate-fin heat exchanger group (secondary heat exchange), two gas-liquid separators (comprising a heavy hydrocarbon separator and a cryogen separator) and two throttling arrangements; Mixed working fluid and natural gas are accomplished whole heat transfer process in the ice chest system.
In the azeotrope compressibility; The compressor one section outlet connects the one-level cooler, and the one-level cooler is connected with the one-level gas-liquid separator again, and one-level gas-liquid separator gas phase end connects two sections compressions; One-level gas-liquid separator bottom liquid phases end connects the liquid pump; The liquid pump discharge be connected secondary coolers after two sections compression outlets converge, secondary coolers is connected with the secondary gas-liquid separator again, secondary gas-liquid separator top gas phase end is connected with heat exchanger package first heat exchanger channels; Secondary gas-liquid separator bottom liquid phases end is connected with heat exchanger package second heat exchanger channels;
In the ice chest system; The secondary gas-liquid separator liquid phase end that is come by the azeotrope compressibility connects an end of first throttle device through second heat exchanger channels in the heat exchanger package, and the other end of first throttle device connects one section compression after connecting the 3rd heat exchanger channels of heat exchanger package; The gas phase end that secondary gas-liquid separator top obtains is connected with second throttling arrangement, one end through the heat exchanger package first heat exchanger channels precooling again, and the second throttling arrangement other end connects the cryogen separator after connecting heat exchanger package the 4th heat exchanger channels; Natural gas line connects the heavy hydrocarbon separator through heat exchanger package the 5th heat exchanger channels, and through sending into the LNG storage tank behind all the other heat exchangers at different levels of heat exchanger package, heavy hydrocarbon separator bottom liquid phases obtains as liquefied petroleum gas (LPG) heavy hydrocarbon separator top gas phase end successively.
The device of two-period form mixed working fluid compressibility according to the invention; In its azeotrope compressibility; Compressor one section outlet gas gets into one-level cooler cooling back through the one-level gas-liquid separator separates, and the gas phase after the separation continues to get into two sections compressions, and the hot gas of the liquid phase after the separation after liquid pump pressurization back and two sections compressions converges; After the secondary coolers cooling, get into the secondary gas-liquid separator separates, the gas phase after the separation gets into first heat exchanger channels (gas phase channel) of downstream heat exchanger; The liquid that secondary gas-liquid separator bottom obtains gets into the second liquid phase heat exchanger channels of downstream heat exchanger respectively.In the ice chest system, the liquid cryogen that bottom cryogen compressibility secondary gas-liquid separator, comes passes through the first throttle device after getting into the heat exchanger package precooling, and this stream thigh after the throttling gets into cryogen separator middle part; The gas phase cryogen that comes by secondary gas-liquid separator top through the heat exchanger package precooling after the second throttling arrangement throttling; This stream after the throttling burst reverse entering leads to cryogen separator middle part after re-heat to the uniform temperature in the heat exchanger package; Converge with the cryogen of the same entering cryogen separator of (after going out the first throttle device) after the above-mentioned cooling throttling; The two is divided into gas-liquid two-phase through the cryogen separator, and being back to after the gas-liquid two-phase that goes out the cryogen separator converges provides cold in the heat exchanger package.Natural gas gets into separator separates after at first being cooled to uniform temperature through heat exchanger package; The bottom obtains the heavy hydrocarbon component; The gas phase that the top obtains partly continues to get into all the other heat exchanger heat exchange at different levels of heat exchanger package, is cooled in the LNG entering LNG storage tank that obtains after the supercooled state to store.
For the ease of more being expressly understood the present invention, the technical scheme of device of the present invention is summarized as follows:
Adopt the device of single mixed working fluid refrigeration liquefying natural gas, this device comprises azeotrope compressibility and ice chest system,
Wherein this compressibility comprise two-period form mixed working fluid compressor, first cooler being connected with second section with first section of said two-period form mixed working fluid compressor respectively and second cooler, first gas-liquid separator being connected with second cooler with said first cooler respectively and second gas-liquid separator with said two gas-liquid separators in the middle of first liquid pump that is connected
Wherein the ice chest system comprises:
One group of plate-fin heat exchanger group; It comprises at least six heat exchanger channels: the 5th and the 6th heat exchanger channels first, second, third, fourth; The input of said second heat exchanger channels and first heat exchanger channels via two pipelines respectively with said azeotrope compressibility in the liquid phase end of second gas-liquid separator be connected with the gas phase end and the output of the 3rd heat exchanger channels is connected to first compression section via pipeline;
First throttling arrangement that is connected with the output of second heat exchanger channels of said plate-fin heat exchanger group;
Second throttling arrangement that is connected with the input of the output of first heat exchanger channels of said plate-fin heat exchanger group and the 4th heat exchanger channels;
With
The cryogen separator that is connected with first throttling arrangement with the output of the input of the 3rd heat exchanger channels of said plate-fin heat exchanger group, the 4th heat exchanger channels;
With an independent heat exchanger channels of said plate-fin heat exchanger group is the natural gas heavy hydrocarbon separator that the 5th heat exchanger channels is connected,
Wherein the gas phase end of first gas-liquid separator in two gas-liquid separators is connected with second compression section of two-period form mixed working fluid compressor; The liquid phase end of first gas-liquid separator is connected to second cooler in said two coolers after converging via the outlet conduit of the liquid pump and second compression section, the gas phase end of second gas-liquid separator and liquid phase end respectively with two heat exchanger channels of said one group of plate-fin heat exchanger group promptly the input of first heat exchanger channels and second heat exchanger channels be connected; Connect the cryogen separator behind wherein above-mentioned first throttling arrangement; The top gas phase end and the bottom liquid phases end of cryogen separator converges the input that the back is connected the 3rd heat exchanger channels; First section of the output of the 3rd heat exchanger channels and two-period form mixed working fluid compressor is connected; Above-mentioned second throttling arrangement is connected to the cryogen separator after connecting the 4th heat exchanger channels input; The above-mentioned independent heat exchanger channels of the pipeline that is used to carry purified natural gas through heat exchanger package i.e. the 5th heat exchanger channels is connected to the heavy hydrocarbon separator, and the top gas phase end of heavy hydrocarbon separator promptly is connected to LNG tank behind the 6th heat exchanger channels through a heat exchanger channels of heat exchanger package successively.
Randomly, the top gas phase end of heavy hydrocarbon separator successively through behind the 6th heat exchanger channels of heat exchanger package further other the 7th heat exchanger channels through heat exchanger package be connected to LNG tank.
The technological process of the method that adopts single mixed working fluid to freeze to come liquefied natural gas is following:
The natural gas circulation:
Raw natural gas after the purification at first gets into the plate-fin heat exchanger group and carries out precooling; Get into the heavy hydrocarbon separator after being cooled to-30 ℃～-80 ℃ and carry out gas-liquid separation; Continue to get into all the other heat exchangers at different levels of heat exchanger package by the isolated vapor phase stream thigh in heavy hydrocarbon separator top; And being cooled to-130 ℃～-166 ℃ therein, the liquefied natural gas that obtains is sent in the LNG storage tank and is stored.
The azeotrope circulation:
By C1～C5 and N
2The mixed working fluid of forming promptly is selected from C1, C2, C3, C4 and C5 alkane and N
2In four kinds, five kinds or six kinds; They are according to the arbitrary volume ratio or according to the volume ratio that approximately is equal to; Get into the inlet of compressor, warp is compressed to 0.6～1.8MPaA for one section, gets into the one-level cooler and is cooled to 30 ℃～40 ℃; Get into the one-level gas-liquid separator again and carry out gas-liquid separation; The isolated gas in one-level gas-liquid separator top continues to get into two sections inlets of compressor, is compressed to 1.2～5.4MPaA through two sections, and the isolated liquid of one-level gas-liquid separator bottom liquid phases end is after the liquid pump is forced into 1.2～5.4MPaA and two sections compressions and exports hot gas and converge; Get into secondary coolers again and be cooled to 30 ℃～40 ℃; Cooled mixed working fluid gets into the secondary gas-liquid separator subsequently and carries out gas-liquid separation, and secondary gas-liquid separator top gas gets into first heat exchanger channels of main heat exchanger group subsequently and participates in heat exchange, and the isolated liquid in secondary gas-liquid separator bottom gets into second heat exchanger channels of main heat exchanger group and participates in heat exchange;
The liquid of drawing from mixed working fluid compressibility secondary gas-liquid separator bottom at first gets into second heat exchanger channels of heat exchanger package; Therein by-30 ℃～-80 ℃ extremely approximately of precoolings; Behind first throttle valve throttling to 0.2～0.8MPaA, get into cryogen separator middle part; Be cooled to-135 ℃～-169 ℃ by the vapor phase stream thigh of the isolated mixed working fluid in the secondary gas-liquid separator top gas phase channel through heat exchanger package; Reverse entering heat exchanger package is that heat exchanger provides cold behind second choke valve throttling to 0.2～0.8MPaA again; Re-heat is drawn heat exchanger package entering cryogen separator middle part after-30 ℃～-80 ℃; Converge with the bottom liquid phases of the secondary gas-liquid separator same stream thigh that gets into the cryogen separator after cooling, throttling, get into the cryogen separator, being back to after the gas-liquid two-phase that goes out the cryogen separator converges provides cold in the heat exchanger package.Further, being back to after the gas-liquid two-phase that goes out the cryogen separator converges provides in the heat exchanger package after the cold, turns back to a section of compressor as azeotrope.
Here, pressure unit MPaA is a MPa, absolute pressure.
Method of the present invention and the employed device of this method have fully been described here.
Advantage of the present invention:
1. the varying duty running to device has excellent adaptability, and the final stage gas phase gets into the cryogen separator after the re-heat of backflowing after the throttling, can effectively avoid the ice chest hydrops, thereby guarantee when running on the lower load, and product energy consumption and nominal situation energy consumption are approaching.
2. adopt two-period form azeotrope compressor in the inventive method, azeotrope has been compressed and separation step by step step by step, reduced the power consumption of gas compression.
3. one-level gas-liquid separator bottom liquid stream thigh is not participated in follow-up compression process, has reduced the influence degree of the fluctuation of azeotrope proportioning to the compressor bank operating condition to a certain extent, makes whole device be easier to operation.
4. adopt the secondary heat exchange to make the cold fluid of whole heat transfer process and the heat exchange curve of hot fluid more mate, effectively reduced the flow of azeotrope.
Description of drawings
Fig. 1 is a kind of structure chart of prior art;
Fig. 2 is the device allocation plan of mixed working fluid refrigeration system according to the invention.
Wherein: 1 two-period form mixed working fluid compressor, 6 heavy hydrocarbon separators, 7 cryogen separators, 21,22 coolers, 31,32 gas-liquid separators, 4,4 ' liquid pump, 8 plate-fin heat exchangers, 9 LNG storage tanks, 51,52 choke valves.
The specific embodiment
Further specify below in conjunction with accompanying drawing:
The natural gas circulation:
As shown in Figure 2; Raw natural gas after the purification at first gets into precooling in plate-fin main heat exchanger group 8 the 5th heat exchanger channels; Get in the heavy hydrocarbon separator 6 after being cooled to-30 ℃～-80 ℃ and carry out gas-liquid separation, continue to get into all the other heat exchangers at different levels (the 6th heat exchanger channels) of main heat exchanger group 8 by the isolated vapor phase stream thigh in heavy hydrocarbon separator 6 tops, and after being cooled to-130 ℃～-166 ℃ therein; Send into storage in the LNG storage tank 9, heavy hydrocarbon separator bottom liquid phases is liquefied petroleum gas (LPG).
The azeotrope circulation:
By C1～C5 and N
2The mixed working fluid of forming promptly is selected from C1, C2, C3, C4 and C5 alkane and N
2In four kinds, five kinds or six kinds; They are according to the arbitrary volume ratio or according to the volume ratio that approximately is equal to; Get into the inlet of compressor 1, warp is compressed to 0.6～1.8MPaA for one section, gets into one-level cooler 21 and is cooled to 30 ℃～40 ℃; Get into one-level gas-liquid separator 31 again and carry out gas-liquid separation; The isolated gas in one-level gas-liquid separator 31 tops continues to get into two sections inlets of compressor, is compressed to 1.2～5.4MPaA through two sections, and the isolated liquid of one-level gas-liquid separator 31 bottom liquid phases ends is after liquid pump 4 is forced into 1.2～5.4MPaA and two sections compressions and exports hot gas and converge; Get into secondary coolers 22 again and be cooled to 30 ℃～40 ℃; Cooled mixed working fluid gets into secondary gas-liquid separator 32 subsequently and carries out gas-liquid separation, and secondary gas-liquid separator 32 top gas get into first heat exchanger channels of main heat exchanger group 8 subsequently and participate in heat exchange, and the isolated liquid in secondary gas-liquid separator 32 bottoms gets into second heat exchanger channels of main heat exchanger group 8 and participates in heat exchange;
The liquid of drawing from mixed working fluid compressibility secondary gas-liquid separator 32 bottoms at first gets into second heat exchanger channels of heat exchanger package, by-30 ℃～-80 ℃ extremely approximately of precoolings, behind choke valve 51 throttlings to 0.2～0.8MPaA, gets into cryogen separator 7 therein; Be cooled to-135 ℃～-169 ℃ by the vapor phase stream thigh of the isolated mixed working fluid in the secondary gas-liquid separator 32 tops gas phase channel (first heat exchanger channels) through heat exchanger package 8; Behind choke valve 52 throttlings to 0.2～0.8MPaA, oppositely get into heat exchanger package 8 the 4th heat exchanger channels again; Re-heat is drawn heat exchanger package entering cryogen separator 7 middle parts after-30 ℃～-80 ℃; The stream thigh that after cooling, throttling, produces with the liquid phase of secondary gas-liquid separator 32 converges; The top gas phase that goes out the cryogen separator provides in heat exchanger package the 3rd heat exchanger channels after the cold with being back to after bottom liquid phases two is converged mutually, turns back to a section of compressor as azeotrope.
Claims (4)
1. adopt the device of single mixed working fluid refrigeration liquefying natural gas, this device comprises azeotrope compressibility and ice chest system,
Wherein this compressibility comprise two-period form mixed working fluid compressor, first cooler being connected with second section with first section of said two-period form mixed working fluid compressor respectively and second cooler, first gas-liquid separator being connected with second cooler with said first cooler respectively and second gas-liquid separator with said two gas-liquid separators in the middle of first liquid pump that is connected
Wherein the ice chest system comprises:
One group of plate-fin heat exchanger group; It comprises at least six heat exchanger channels: the 5th and the 6th heat exchanger channels first, second, third, fourth; The input of said second heat exchanger channels and first heat exchanger channels via two pipelines respectively with said azeotrope compressibility in the liquid phase end of second gas-liquid separator be connected with the gas phase end and the output of the 3rd heat exchanger channels is connected to first compression section via pipeline;
First throttling arrangement that is connected with the output of second heat exchanger channels of said plate-fin heat exchanger group;
Second throttling arrangement that is connected with the input of the output of first heat exchanger channels of said plate-fin heat exchanger group and the 4th heat exchanger channels;
With
The cryogen separator that is connected with first throttling arrangement with the output of the input of the 3rd heat exchanger channels of said plate-fin heat exchanger group, the 4th heat exchanger channels;
With an independent heat exchanger channels of said plate-fin heat exchanger group is the natural gas heavy hydrocarbon separator that the 5th heat exchanger channels is connected,
Wherein the gas phase end of first gas-liquid separator in two gas-liquid separators is connected with second compression section of two-period form mixed working fluid compressor; The liquid phase end of first gas-liquid separator is connected to second cooler in said two coolers after converging via the outlet conduit of the liquid pump and second compression section, the gas phase end of second gas-liquid separator and liquid phase end respectively with two heat exchanger channels of said one group of plate-fin heat exchanger group promptly the input of first heat exchanger channels and second heat exchanger channels be connected; Connect the cryogen separator behind wherein above-mentioned first throttling arrangement; The top gas phase end and the bottom liquid phases end of cryogen separator converges the input that the back is connected the 3rd heat exchanger channels; First section of the output of the 3rd heat exchanger channels and two-period form mixed working fluid compressor is connected; Above-mentioned second throttling arrangement is connected to the cryogen separator after connecting the 4th heat exchanger channels input; The above-mentioned independent heat exchanger channels of the pipeline that is used to carry purified natural gas through heat exchanger package i.e. the 5th heat exchanger channels is connected to the heavy hydrocarbon separator, and the top gas phase end of heavy hydrocarbon separator promptly is connected to LNG tank behind the 6th heat exchanger channels through a heat exchanger channels of heat exchanger package successively.
2. the device of the single mixed working fluid refrigeration liquefying of employing according to claim 1 natural gas is characterised in that:
The top gas phase end of heavy hydrocarbon separator successively through behind the 6th heat exchanger channels of heat exchanger package further other the 7th heat exchanger channels through heat exchanger package be connected to LNG tank.
3. adopt single mixed working fluid to freeze and come the method for liquefied natural gas, it is characterized in that: this method comprises natural gas circulation and azeotrope circulation:
The natural gas circulation:
Raw natural gas after the purification at first gets into the plate-fin heat exchanger group and carries out precooling; Get into the heavy hydrocarbon separator after being cooled to-30 ℃～-80 ℃ and carry out gas-liquid separation; Continue to get into all the other heat exchangers at different levels of heat exchanger package by the isolated vapor phase stream thigh in heavy hydrocarbon separator top; And being cooled to-130 ℃～-166 ℃ therein, the liquefied natural gas that obtains is sent in the LNG storage tank and is stored;
The azeotrope circulation:
By C1～C5 and N
2The mixed working fluid of forming gets into the inlet of compressor; Be compressed to 0.6～1.8MPaA through one section; Get into the one-level cooler and be cooled to 30 ℃～40 ℃; Get into the one-level gas-liquid separator again and carry out gas-liquid separation; The isolated gas in one-level gas-liquid separator top continues to get into two sections inlets of compressor, is compressed to 1.2～5.4MPaA through two sections, and the isolated liquid of one-level gas-liquid separator bottom liquid phases end is after the liquid pump is forced into 1.2～5.4MPaA and two sections compressions and exports hot gas and converge; Get into secondary coolers again and be cooled to 30 ℃～40 ℃; Cooled mixed working fluid gets into the secondary gas-liquid separator subsequently and carries out gas-liquid separation, and secondary gas-liquid separator top gas gets into first heat exchanger channels of main heat exchanger group subsequently and participates in heat exchange, and the isolated liquid in secondary gas-liquid separator bottom gets into second heat exchanger channels of main heat exchanger group and participates in heat exchange;
The liquid of drawing from mixed working fluid compressibility secondary gas-liquid separator bottom at first gets into second heat exchanger channels of heat exchanger package; Therein by-30 ℃～-80 ℃ extremely approximately of precoolings; Behind first throttle valve throttling to 0.2～0.8MPaA, get into cryogen separator middle part; By the vapor phase stream thigh of the isolated mixed working fluid in the secondary gas-liquid separator top gas phase channel through heat exchanger package promptly first heat exchanger channels be cooled to-135 ℃～-169 ℃; Reverse entering heat exchanger package the 4th heat exchanger channels is that heat exchanger provides cold behind second choke valve throttling to 0.2～0.8MPaA again; Re-heat is drawn heat exchanger package after-30 ℃～-80 ℃ and is also got into cryogen separator middle part; Converge with the stream thigh that goes out the same entering cryogen separator behind the first throttle valve, be back to after the gas-liquid two-phase that goes out the cryogen separator converges in heat exchanger package the 3rd heat exchanger channels, turn back to a section of compressor as azeotrope then to heat exchanger package provides cold.
4. the single mixed working fluid of employing according to claim 3 freezes and comes the method for liquefied natural gas, it is characterized in that, by C1～C5 and N
2The mixed working fluid of forming is for being selected from C1, C2, C3, C4 and C5 alkane and N
2In four kinds, five kinds or six kinds, each is according to the arbitrary volume ratio or according to the volume ratio that approximately is equal to.
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210064449.5A CN102636000B (en) | 2012-03-13 | 2012-03-13 | Method for refrigerating liquefied natural gas by aid of single mixed working medium and device |
| CA2864482A CA2864482C (en) | 2012-03-13 | 2012-09-13 | Method and system for liquefying natural gas using single mixed refrigerant and refrigeration medium |
| US14/381,675 US20150013378A1 (en) | 2012-03-13 | 2012-09-13 | Apparatus And Method For Liquefying Natural Gas By Refrigerating Single Mixed Working Medium |
| PCT/CN2012/081340 WO2013135037A1 (en) | 2012-03-13 | 2012-09-13 | Apparatus and method for liquefying natural gas by refrigerating single mixed working medium |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210064449.5A CN102636000B (en) | 2012-03-13 | 2012-03-13 | Method for refrigerating liquefied natural gas by aid of single mixed working medium and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102636000A true CN102636000A (en) | 2012-08-15 |
| CN102636000B CN102636000B (en) | 2014-07-23 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210064449.5A Active CN102636000B (en) | 2012-03-13 | 2012-03-13 | Method for refrigerating liquefied natural gas by aid of single mixed working medium and device |
Country Status (4)
| Country | Link |
|---|---|
| US (1) | US20150013378A1 (en) |
| CN (1) | CN102636000B (en) |
| CA (1) | CA2864482C (en) |
| WO (1) | WO2013135037A1 (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013071789A1 (en) * | 2011-11-18 | 2013-05-23 | 新地能源工程技术有限公司 | Device and method for liquefying natural gas using single mixed working medium as refrigeration medium |
| WO2013135037A1 (en) * | 2012-03-13 | 2013-09-19 | 新地能源工程技术有限公司 | Apparatus and method for liquefying natural gas by refrigerating single mixed working medium |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6298688B1 (en) * | 1999-10-12 | 2001-10-09 | Air Products And Chemicals, Inc. | Process for nitrogen liquefaction |
| US6308531B1 (en) * | 1999-10-12 | 2001-10-30 | Air Products And Chemicals, Inc. | Hybrid cycle for the production of liquefied natural gas |
| US6347531B1 (en) * | 1999-10-12 | 2002-02-19 | Air Products And Chemicals, Inc. | Single mixed refrigerant gas liquefaction process |
| CN101644527A (en) * | 2009-08-26 | 2010-02-10 | 四川空分设备(集团)有限责任公司 | Refrigeration system and liquefaction system for liquefaction process of natural gas |
| CN101893367A (en) * | 2010-08-13 | 2010-11-24 | 唐建峰 | Method for liquefying natural gas by using mixed coolant |
| CN101967413A (en) * | 2010-06-07 | 2011-02-09 | 杭州福斯达实业集团有限公司 | Method and device for liquefying natural gas via refrigeration of single mixed refrigerant |
| CN202494271U (en) * | 2012-03-13 | 2012-10-17 | 新地能源工程技术有限公司 | Device for liquefying natural gas through refrigeration of single mixed working medium |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3808826A (en) * | 1970-09-28 | 1974-05-07 | Phillips Petroleum Co | Refrigeration process |
| EP0723125B1 (en) * | 1994-12-09 | 2001-10-24 | Kabushiki Kaisha Kobe Seiko Sho | Gas liquefying method and plant |
| DE10209799A1 (en) * | 2002-03-06 | 2003-09-25 | Linde Ag | Process for liquefying a hydrocarbon-rich stream |
| CN201762300U (en) * | 2010-06-07 | 2011-03-16 | 杭州福斯达实业集团有限公司 | Device using single-mixed refrigerant refrigeration to liquefy natural gas |
| CN102636000B (en) * | 2012-03-13 | 2014-07-23 | 新地能源工程技术有限公司 | Method for refrigerating liquefied natural gas by aid of single mixed working medium and device |
-
2012
- 2012-03-13 CN CN201210064449.5A patent/CN102636000B/en active Active
- 2012-09-13 US US14/381,675 patent/US20150013378A1/en not_active Abandoned
- 2012-09-13 WO PCT/CN2012/081340 patent/WO2013135037A1/en active Application Filing
- 2012-09-13 CA CA2864482A patent/CA2864482C/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6298688B1 (en) * | 1999-10-12 | 2001-10-09 | Air Products And Chemicals, Inc. | Process for nitrogen liquefaction |
| US6308531B1 (en) * | 1999-10-12 | 2001-10-30 | Air Products And Chemicals, Inc. | Hybrid cycle for the production of liquefied natural gas |
| US6347531B1 (en) * | 1999-10-12 | 2002-02-19 | Air Products And Chemicals, Inc. | Single mixed refrigerant gas liquefaction process |
| CN101644527A (en) * | 2009-08-26 | 2010-02-10 | 四川空分设备(集团)有限责任公司 | Refrigeration system and liquefaction system for liquefaction process of natural gas |
| CN101967413A (en) * | 2010-06-07 | 2011-02-09 | 杭州福斯达实业集团有限公司 | Method and device for liquefying natural gas via refrigeration of single mixed refrigerant |
| CN101893367A (en) * | 2010-08-13 | 2010-11-24 | 唐建峰 | Method for liquefying natural gas by using mixed coolant |
| CN202494271U (en) * | 2012-03-13 | 2012-10-17 | 新地能源工程技术有限公司 | Device for liquefying natural gas through refrigeration of single mixed working medium |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013071789A1 (en) * | 2011-11-18 | 2013-05-23 | 新地能源工程技术有限公司 | Device and method for liquefying natural gas using single mixed working medium as refrigeration medium |
| WO2013135037A1 (en) * | 2012-03-13 | 2013-09-19 | 新地能源工程技术有限公司 | Apparatus and method for liquefying natural gas by refrigerating single mixed working medium |
| CN103697659A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of high methane gas |
| CN103697661A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of coke oven gas |
| CN103697659B (en) * | 2013-12-23 | 2015-11-18 | 中空能源设备有限公司 | The device and method of liquefied natural gas and rich hydrogen production is produced from high methane gas |
| CN104089463B (en) * | 2014-07-16 | 2017-11-17 | 北京安珂罗工程技术有限公司 | A kind of method and system of azeotrope gas-liquid separating throttling refrigeration |
| CN104089463A (en) * | 2014-07-16 | 2014-10-08 | 北京安珂罗工程技术有限公司 | Mixed refrigerant gas-liquid separating type throttling and refrigerating method and system |
| CN106642986A (en) * | 2016-07-15 | 2017-05-10 | 上海利策科技股份有限公司 | Natural gas liquefaction device used for offshore platform |
| CN106766669A (en) * | 2016-11-29 | 2017-05-31 | 重庆耐德工业股份有限公司 | A kind of hydrocarbon removal process and its system for high-pressure jet natural gas liquefaction |
| CN110268214A (en) * | 2016-12-22 | 2019-09-20 | 前苏伊士环能集团 | Device and method for liquefied natural gas and the ship including the equipment |
| CN110537064A (en) * | 2016-12-22 | 2019-12-03 | 前苏伊士环能集团 | Device and method for liquefied natural gas and the ship including the equipment |
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| CN110257118B (en) * | 2019-07-19 | 2024-04-26 | 中冶焦耐(大连)工程技术有限公司 | LNG pipeline precooling method and NG cold air generating device |
Also Published As
| Publication number | Publication date |
|---|---|
| CA2864482A1 (en) | 2013-09-19 |
| WO2013135037A1 (en) | 2013-09-19 |
| CN102636000B (en) | 2014-07-23 |
| CA2864482C (en) | 2016-11-08 |
| US20150013378A1 (en) | 2015-01-15 |
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