CN102636000B - 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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- CN102636000B CN102636000B CN201210064449.5A CN201210064449A CN102636000B CN 102636000 B CN102636000 B CN 102636000B CN 201210064449 A CN201210064449 A CN 201210064449A CN 102636000 B CN102636000 B CN 102636000B
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- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 99
- 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 21
- 230000006835 compression Effects 0.000 claims abstract description 18
- 238000003860 storage Methods 0.000 claims abstract description 9
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 64
- 239000012071 phase Substances 0.000 claims description 34
- 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 18
- 210000000689 upper leg Anatomy 0.000 claims description 16
- 238000005057 refrigeration Methods 0.000 claims description 15
- 239000000203 mixture Substances 0.000 claims description 7
- 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
- 238000004140 cleaning Methods 0.000 claims description 2
- 239000003507 refrigerant Substances 0.000 abstract description 4
- 238000009825 accumulation Methods 0.000 abstract 1
- 238000001816 cooling Methods 0.000 description 5
- 238000005265 energy consumption 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
- 238000005516 engineering process Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 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
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
- F25J1/0002—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
- F25J1/0243—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
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 because its feature of environmental protection becomes the optimisation substance that replaces other fuel, and its application expands the aspects such as generating, automobile use gas, industrial gas, city dweller's use gas, chemical industry use gas gradually to.
Along with the growth of Natural Gas Consumption Using, as natural gas, the most effectively for one of form, the volume of trade of liquefied natural gas has also become one of fastest-rising field of energy market.The development of liquefied natural gas industry, has higher requirement at aspects such as energy consumption, investment and efficiency to natural gas liquefaction and device.
At present, the natural gas liquefaction process of comparative maturity mainly contains: stepwise refrigeration process, swell refrigeration technique and mixed working fluid refrigeration process.Single mixed working fluid refrigeration process wherein is relatively subject to the favor of medium-sized LNG device.
In the natural gas liquefaction of existing single mixed working fluid refrigeration, cryogen compressibility is two-stage compression, and natural gas liquefaction adopts one-level heat exchange.
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 liquor pumps 4,4 ', one platen fin heat exchanger 8 and LNG storage tanks 9, the mixed working fluid being made up of C1～C5 and N2 enters the entrance of compressor after rational proportion, be compressed to 0.6～1MPa through one section, enter one-level cooler and be cooled to 30～40 DEG C, enter again one-level knockout drum and carry out gas-liquid separation, the isolated gas in one-level gas-liquid separation tank top continues to enter two sections of entrances of compressor, be compressed to 1.6～2.5MPa through two sections, the liquid that bottom one-level separates, separation obtains is mixed into secondary coolers with the gas of two sections of compressor outlets after pressurizeing by liquor pump and is cooled to 30～40 DEG C, cooled mixed working fluid enters subsequently secondary knockout drum and carries out gas-liquid separation, liquid after separation by the gas obtaining with this separator top after secondary liquor pump pressurization mix laggard enter plate-fin heat exchanger, after being chilled in advance uniform temperature, this plate-fin heat exchanger is returned in throttling again, for whole heat transfer process provides cold, natural gas enters in LNG storage tank after by plate-fin heat exchanger.
In above-mentioned technique, for ensureing that liquids and gases enter 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 separator bottom liquid exports to plate-fin heat exchanger top cryogen entrance is brought, and must realize by increasing final stage liquor pump.Cryogen and the natural gas heat transfer process in plate-fin heat exchanger is one-level heat exchange, between stream thigh, the optimization of heat transfer temperature difference is subject to certain limitation, and plant energy consumption is higher, and, this kind of flow process easily produces ice chest bottom hydrops, and the varying duty running of device is not had to good 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 mixed working fluid loop, mixed working fluid is followed gas-liquid separation step by step in compression process step by step at it simultaneously, 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 compressed gas phase obtaining and liquid phase mixed working fluid stream stock do not enter the different passage throttling heat exchange of heat exchanger package, relatively traditional handicraft has been saved final stage liquor pump, and adopts multi-stage heat exchanger that the heat exchange curve of hot-fluid thigh and cold flow thigh in whole process is more mated; After the re-heat of backflowing of final stage gas phase after throttling, enter cryogen separator, can effectively avoid 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 liquor pump, 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 complete whole heat transfer process in ice chest system.
In azeotrope compressibility, compressor one section outlet connects one-level cooler, one-level cooler is connected with one-level gas-liquid separator again, one-level gas-liquid separator gas phase end connects two sections of compressions, one-level gas-liquid separator bottom liquid phases end connects liquor pump, liquor pump outlet is connected secondary coolers after converging with two sections of compression outlets, and secondary coolers is connected with secondary gas-liquid separator again, and secondary gas-liquid separator top gas phase end is connected with heat exchanger package the first heat exchanger channels; Secondary gas-liquid separator bottom liquid phases end is connected with heat exchanger package the second heat exchanger channels;
In ice chest system, the secondary gas-liquid separator liquid phase end being come by azeotrope compressibility connects one end of first throttle device by the second heat exchanger channels in heat exchanger package, after the 3rd heat exchanger channels of the other end connection heat exchanger package of first throttle device, connect one section of compression; The gas phase end that secondary gas-liquid separator top obtains passes through heat exchanger package the first heat exchanger channels precooling, then is connected with second throttling arrangement one end, and the second throttling arrangement other end connects cryogen separator after connecting heat exchanger package the 4th heat exchanger channels; Natural gas line connects heavy hydrocarbon separator by heat exchanger package the 5th heat exchanger channels, heavy hydrocarbon separator top gas phase end is successively by sending into LNG storage tank after all the other heat exchangers at different levels of heat exchanger package, and heavy hydrocarbon separator bottom liquid phases obtains as liquefied petroleum gas (LPG).
The device of two-period form mixed working fluid compressibility of the present invention, in its azeotrope compressibility, it is cooling rear by one-level gas-liquid separator separates that compressor one section outlet gas enters one-level cooler, gas phase after separation continues to enter two sections of compressions, liquid phase after separation after liquor pump pressurization with two sections of compressions after hot gas converge, after secondary coolers is cooling, enter secondary gas-liquid separator separates, the gas phase after separation enters first heat exchanger channels (gas phase channel) of downstream heat exchanger; The liquid that secondary gas-liquid separator bottom obtains enters respectively the second liquid phase heat exchanger channels of downstream heat exchanger.In ice chest system, the liquid cryogen being come by cryogen compressibility secondary gas-liquid separator bottom enters after heat exchanger package precooling by first throttle device, and this stream thigh after throttling enters cryogen separator middle part; By secondary gas-liquid separator top come gas phase cryogen after heat exchanger package precooling through the second throttling arrangement throttling, this stream thigh after throttling oppositely enters re-heat in heat exchanger package and lead to cryogen separator middle part to uniform temperature, converge with the same cryogen that enters cryogen separator (going out after first throttle device) after above-mentioned cooling throttling, the two is divided into gas-liquid two-phase through cryogen separator, is back to cold is provided in heat exchanger package after the gas-liquid two-phase that goes out cryogen separator converges.First natural gas enters separator and separates after heat exchanger package is cooled to uniform temperature, bottom obtains heavy hydrocarbon component, the gas phase part that top obtains continues to enter all the other heat exchanger heat exchange at different levels of heat exchanger package, is cooled to the LNG obtaining after supercooled state and enters in LNG storage tank and store.
For the ease of more clearly understanding 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 comprises two-period form mixed working fluid compressor, respectively the First cooler that is connected with first paragraph and the second segment of described two-period form mixed working fluid compressor and second cooler, respectively the First gas-liquid separator that is connected with described First cooler and second cooler and second gas-liquid separator and the liquor pump being connected with the First in the middle of described two gas-liquid separators
Wherein ice chest system comprises:
One group of plate-fin heat exchanger group, it comprises at least six heat exchanger channels: first, second, third, fourth, the 5th and the 6th heat exchanger channels, the input of described the second heat exchanger channels and the first heat exchanger channels is connected with liquid phase end and the gas phase end of second gas-liquid separator in described azeotrope compressibility respectively via two pipelines, and the output of the 3rd heat exchanger channels is connected to the first compression section via pipeline;
The First throttling arrangement being connected with the output of the second heat exchanger channels of described plate-fin heat exchanger group;
Second throttling arrangement being connected with the output of the first heat exchanger channels and the input of the 4th heat exchanger channels of described plate-fin heat exchanger group;
With
Input, the output of the 4th heat exchanger channels and the cryogen separator that First throttling arrangement is connected with the 3rd heat exchanger channels of described plate-fin heat exchanger group;
With the independent heat exchanger channels natural gas heavy hydrocarbon separator that the 5th heat exchanger channels is connected of described plate-fin heat exchanger group,
Wherein the gas phase end of the First gas-liquid separator in two gas-liquid separators is connected with the 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 described two coolers after converging via the outlet conduit of liquor pump and the second compression section, and the gas phase end of second gas-liquid separator is connected with the input that liquid phase end is the first heat exchanger channels and the second heat exchanger channels with two heat exchanger channels of described one group of plate-fin heat exchanger group respectively, wherein after above-mentioned First throttling arrangement, connect cryogen separator, the top gas phase end of cryogen separator and bottom liquid phases end converge the input of rear connection the 3rd heat exchanger channels, the output of the 3rd heat exchanger channels is connected with the first paragraph of two-period form mixed working fluid compressor, after connecting the 4th heat exchanger channels input, above-mentioned the second throttling arrangement is connected to cryogen separator, the above-mentioned independent heat exchanger channels of crossing heat exchanger package for delivery of the device for cleaning pipeline of purified natural gas is that the 5th heat exchanger channels is connected to heavy hydrocarbon separator, the top gas phase end of heavy hydrocarbon separator is connected to LNG tank after the 6th heat exchanger channels by a heat exchanger channels of heat exchanger package successively.
Optionally, the top gas phase end of heavy hydrocarbon separator successively by after the 6th heat exchanger channels of heat exchanger package further other the 7th heat exchanger channels by heat exchanger package be connected to LNG tank.
The technological process of the method that adopts single mixed working fluid to freeze to carry out liquefied natural gas is as follows:
Natural gas circulation:
First raw natural gas after purification enters plate-fin heat exchanger group and carries out precooling, after being cooled to-30 DEG C～-80 DEG C, enter heavy hydrocarbon separator and carry out gas-liquid separation, continued to enter 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 therein-130 DEG C～-166 DEG C, the liquefied natural gas obtaining is sent in LNG storage tank and is stored.
Azeotrope circulation:
By C1～C5 and N
2the mixed working fluid of composition, is selected from C1, C2, C3, C4 and C5 alkane and N
2in four kinds, five kinds or six kinds, they are according to arbitrary volume ratio or according to the volume ratio being approximately equal to, enter the entrance of compressor, be compressed to 0.6～1.8MPaA through one section, enter one-level cooler and be cooled to 30 DEG C～40 DEG C, enter again one-level gas-liquid separator and carry out gas-liquid separation, the isolated gas in one-level gas-liquid separator top continues to enter two sections of entrances of compressor, be compressed to 1.2～5.4MPaA through two sections, the isolated liquid of one-level gas-liquid separator bottom liquid phases end is after liquor pump is forced into 1.2～5.4MPaA and two sections compression outlet hot gas and converges, enter again secondary coolers and be cooled to 30 DEG C～40 DEG C, cooled mixed working fluid enters subsequently secondary gas-liquid separator and carries out gas-liquid separation, the first heat exchanger channels that secondary gas-liquid separator top gas enters main heat exchanger group subsequently participates in heat exchange, the second heat exchanger channels that the isolated liquid in secondary gas-liquid separator bottom enters main heat exchanger group participates in heat exchange,
First the liquid of drawing from mixed working fluid compressibility secondary gas-liquid separator bottom enter the second heat exchanger channels of heat exchanger package, be chilled in advance therein approximately-30 DEG C～-80 DEG C, after first throttle valve throttling to 0.2～0.8MPaA, enter cryogen separator middle part, vapor phase stream thigh by the isolated mixed working fluid in secondary gas-liquid separator top is cooled to-135 DEG C～-169 DEG C by the gas phase channel of heat exchanger package, after second choke valve throttling to 0.2～0.8MPaA, oppositely enter again heat exchanger package and provide cold for heat exchanger, re-heat enters cryogen separator middle part to drawing heat exchanger package after-30 DEG C～-80 DEG C, with the bottom liquid phases of secondary gas-liquid separator through cooling, the stream thigh that enters equally cryogen separator after throttling converges, enter cryogen separator, after the gas-liquid two-phase that goes out cryogen separator converges, be back to cold is provided in heat exchanger package.Further, after being back to after the gas-liquid two-phase that goes out cryogen separator converges and providing cold in heat exchanger package, turn back to a section of compressor as azeotrope.
Here, pressure unit MPaA is MPa, absolute pressure.
The device that method of the present invention and the method are used has fully been described here.
Advantage of the present invention:
1. the running of the varying duty of pair device has good adaptability, after the re-heat of backflowing of final stage gas phase after throttling, enters cryogen separator, can effectively avoid ice chest hydrops, thereby ensure in the time of running on the lower load, and product energy consumption and nominal situation energy consumption approach.
2. in the inventive method, adopt two-period form azeotrope compressor, azeotrope has been compressed step by step and separate step by step, reduced the power consumption of gas compression.
3. one-level gas-liquid separator bottom liquid stream thigh does not participate in follow-up compression process, and the influence degree of the fluctuation that has reduced to a certain extent azeotrope proportioning to compressor bank operating condition makes whole device be easier to operation.
4. adopt secondary heat exchange that the cold fluid of whole heat transfer process and the heat exchange curve of hot fluid are more mated, effectively reduced the flow of azeotrope.
Brief description of the drawings
Fig. 1 is a kind of structure chart of prior art;
Fig. 2 is the device allocation plan of Refrigeration Cycle Using Refrigerant Mixture of the present 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 ' liquor pump, 8 plate-fin heat exchangers, 9 LNG storage tanks, 51,52 choke valves.
Detailed description of the invention
Further illustrate below in conjunction with accompanying drawing:
Natural gas circulation:
As shown in Figure 2, first raw natural gas after purification enters precooling in plate-fin main heat exchanger group 8 the 5th heat exchanger channels, after being cooled to-30 DEG C～-80 DEG C, enter and in heavy hydrocarbon separator 6, carry out gas-liquid separation, continued to enter all the other heat exchangers at different levels (the 6th heat exchanger channels) of main heat exchanger group 8 by the heavy hydrocarbon separator 6 isolated vapor phase stream thighs in top, and be cooled to therein after-130 DEG C～-166 DEG C, send in LNG storage tank 9 and store, heavy hydrocarbon separator bottom liquid phases is liquefied petroleum gas (LPG).
Azeotrope circulation:
By C1～C5 and N
2the mixed working fluid of composition, is selected from C1, C2, C3, C4 and C5 alkane and N
2in four kinds, five kinds or six kinds, they are according to arbitrary volume ratio or according to the volume ratio being approximately equal to, enter the entrance of compressor 1, be compressed to 0.6～1.8MPaA through one section, enter one-level cooler 21 and be cooled to 30 DEG C～40 DEG C, enter again one-level gas-liquid separator 31 and carry out gas-liquid separation, the one-level gas-liquid separator 31 isolated gases in top continue to enter two sections of entrances of compressor, be compressed to 1.2～5.4MPaA through two sections, the isolated liquid of one-level gas-liquid separator 31 bottom liquid phases end is after liquor pump 4 is forced into 1.2～5.4MPaA and two sections compression outlet hot gas and converges, enter again secondary coolers 22 and be cooled to 30 DEG C～40 DEG C, cooled mixed working fluid enters subsequently secondary gas-liquid separator 32 and carries out gas-liquid separation, the first heat exchanger channels that secondary gas-liquid separator 32 top gas enter main heat exchanger group 8 subsequently participates in heat exchange, the second heat exchanger channels that the secondary gas-liquid separator 32 isolated liquid in bottom enter main heat exchanger group 8 participates in heat exchange,
First the liquid of drawing from mixed working fluid compressibility secondary gas-liquid separator 32 bottoms enter the second heat exchanger channels of heat exchanger package, is chilled in advance therein approximately-30 DEG C～-80 DEG C, after choke valve 51 throttling to 0.2～0.8MPaA, enters cryogen separator 7, vapor phase stream thigh by the secondary gas-liquid separator 32 isolated mixed working fluids in top is cooled to-135 DEG C～-169 DEG C by the gas phase channel (the first heat exchanger channels) of heat exchanger package 8, after choke valve 52 throttling to 0.2～0.8MPaA, oppositely enter again heat exchanger package 8 the 4th heat exchanger channels, re-heat enters cryogen separator 7 middle parts to drawing heat exchanger package after-30 DEG C～-80 DEG C, with the liquid phase of secondary gas-liquid separator 32 through cooling, the stream thigh producing after throttling converges, after going out to be back to after the top gas phase of cryogen separator and bottom liquid phases two-phase are converged and to provide cold in heat exchanger package the 3rd heat exchanger channels, turn back to a section of compressor as azeotrope.
Claims (4)
1. the device that adopts single mixed working fluid refrigeration liquefying natural gas, this device comprises azeotrope compressibility and ice chest system,
Wherein this compressibility comprises two-period form mixed working fluid compressor, respectively the First cooler that is connected with first paragraph and the second segment of described two-period form mixed working fluid compressor and second cooler, respectively the First gas-liquid separator that is connected with described First cooler and second cooler and second gas-liquid separator and the liquor pump being connected with the First in the middle of described two gas-liquid separators
Wherein ice chest system comprises:
One group of plate-fin heat exchanger group, it comprises at least six heat exchanger channels: first, second, third, fourth, the 5th and the 6th heat exchanger channels, the input of described the second heat exchanger channels and the first heat exchanger channels is connected with liquid phase end and the gas phase end of second gas-liquid separator in described azeotrope compressibility respectively via two pipelines, and the output of the 3rd heat exchanger channels is connected to the first compression section via pipeline;
The First throttling arrangement being connected with the output of the second heat exchanger channels of described plate-fin heat exchanger group;
Second throttling arrangement being connected with the output of the first heat exchanger channels and the input of the 4th heat exchanger channels of described plate-fin heat exchanger group;
With
Input, the output of the 4th heat exchanger channels and the cryogen separator that First throttling arrangement is connected with the 3rd heat exchanger channels of described plate-fin heat exchanger group;
With the independent heat exchanger channels natural gas heavy hydrocarbon separator that the 5th heat exchanger channels is connected of described plate-fin heat exchanger group,
Wherein the gas phase end of the First gas-liquid separator in two gas-liquid separators is connected with the 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 described two coolers after converging via the outlet conduit of liquor pump and the second compression section, and the gas phase end of second gas-liquid separator is connected with the input that liquid phase end is the first heat exchanger channels and the second heat exchanger channels with two heat exchanger channels of described one group of plate-fin heat exchanger group respectively, wherein after above-mentioned First throttling arrangement, connect cryogen separator, the top gas phase end of cryogen separator and bottom liquid phases end converge the input of rear connection the 3rd heat exchanger channels, the output of the 3rd heat exchanger channels is connected with the first paragraph of two-period form mixed working fluid compressor, after connecting the 4th heat exchanger channels input, above-mentioned the second throttling arrangement is connected to cryogen separator, the above-mentioned independent heat exchanger channels of crossing heat exchanger package for delivery of the device for cleaning pipeline of purified natural gas is that the 5th heat exchanger channels is connected to heavy hydrocarbon separator, the top gas phase end of heavy hydrocarbon separator is connected to LNG tank after the 6th heat exchanger channels by 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 by after the 6th heat exchanger channels of heat exchanger package further other the 7th heat exchanger channels by heat exchanger package be connected to LNG tank.
3. adopt single mixed working fluid to freeze and carry out the method for liquefied natural gas, it is characterized in that: the method comprises natural gas circulation and azeotrope circulation:
Natural gas circulation:
First raw natural gas after purification enters plate-fin heat exchanger group and carries out precooling, after being cooled to-30 DEG C～-80 DEG C, enter heavy hydrocarbon separator and carry out gas-liquid separation, continued to enter 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 therein-130 DEG C～-166 DEG C, the liquefied natural gas obtaining is sent in LNG storage tank and is stored;
Azeotrope circulation:
By C1～C5 and N
2the mixed working fluid of composition enters the entrance of compressor, be compressed to 0.6～1.8MPaA through one section, enter one-level cooler and be cooled to 30 DEG C～40 DEG C, enter again one-level gas-liquid separator and carry out gas-liquid separation, the isolated gas in one-level gas-liquid separator top continues to enter two sections of entrances of compressor, be compressed to 1.2～5.4MPaA through two sections, the isolated liquid of one-level gas-liquid separator bottom liquid phases end is after liquor pump is forced into 1.2～5.4MPaA and two sections compression outlet hot gas and converges, enter again secondary coolers and be cooled to 30 DEG C～40 DEG C, cooled mixed working fluid enters subsequently secondary gas-liquid separator and carries out gas-liquid separation, the first heat exchanger channels that secondary gas-liquid separator top gas enters heat exchanger package subsequently participates in heat exchange, the second heat exchanger channels that the isolated liquid in secondary gas-liquid separator bottom enters heat exchanger package participates in heat exchange,
First the liquid of drawing from mixed working fluid compressibility secondary gas-liquid separator bottom enter the second heat exchanger channels of heat exchanger package, be chilled in advance therein-30 DEG C～-80 DEG C, after first throttle valve throttling to 0.2～0.8MPaA, enter cryogen separator middle part, vapor phase stream thigh by the isolated mixed working fluid in secondary gas-liquid separator top is that the first heat exchanger channels is cooled to-135 DEG C～-169 DEG C by the gas phase channel of heat exchanger package, after second choke valve throttling to 0.2～0.8MPaA, oppositely enter again heat exchanger package the 4th heat exchanger channels and provide cold for heat exchanger, re-heat also enters cryogen separator middle part to drawing heat exchanger package after-30 DEG C～-80 DEG C, converge with the same stream thigh that enters cryogen separator going out after first throttle valve, after converging, the gas-liquid two-phase that goes out cryogen separator is back in heat exchanger package the 3rd heat exchanger channels as heat exchanger package provides cold, then turn back to a section of compressor as azeotrope.
4. the single mixed working fluid of employing according to claim 3 freezes and carrys out the method for liquefied natural gas, it is characterized in that, by C1～C5 and N
2the mixed working fluid of composition is for being selected from C1, C2, C3, C4 and C5 alkane and N
2in four kinds, five kinds or six kinds, each contains according to arbitrary volume ratio.
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 |
| PCT/CN2012/081340 WO2013135037A1 (en) | 2012-03-13 | 2012-09-13 | Apparatus and method for liquefying natural gas by refrigerating single mixed working 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 |
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 CN102636000A (en) | 2012-08-15 |
| CN102636000B true 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) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN202328997U (en) * | 2011-11-18 | 2012-07-11 | 新地能源工程技术有限公司 | Device for refrigerating liquefied natural gas by adopting single mixed working medium |
| 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 |
| 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 |
| CN103697661B (en) * | 2013-12-23 | 2016-02-03 | 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 coke-stove 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 |
| DE102015002443A1 (en) * | 2015-02-26 | 2016-09-01 | Linde Aktiengesellschaft | Process for liquefying natural gas |
| US10619918B2 (en) | 2015-04-10 | 2020-04-14 | Chart Energy & Chemicals, Inc. | System and method for removing freezing components from a feed gas |
| TWI707115B (en) | 2015-04-10 | 2020-10-11 | 美商圖表能源與化學有限公司 | Mixed refrigerant liquefaction system and method |
| CN108885035B (en) | 2016-03-31 | 2021-04-16 | 开利公司 | Refrigeration circuit |
| AU2017249441B2 (en) | 2016-04-11 | 2021-05-27 | Geoff Rowe | A system and method for liquefying production gas from a gas source |
| WO2017214723A1 (en) | 2016-06-13 | 2017-12-21 | Geoff Rowe | System, method and apparatus for the regeneration of nitrogen energy within a closed loop cryogenic 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 |
| CN106766669B (en) * | 2016-11-29 | 2019-05-17 | 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 |
| FR3061276B1 (en) * | 2016-12-22 | 2020-01-10 | Engie | DEVICE AND METHOD FOR LIQUEFACTING NATURAL GAS AND VESSEL COMPRISING SUCH A DEVICE |
| FR3061277B1 (en) * | 2016-12-22 | 2019-05-24 | Engie | DEVICE AND METHOD FOR LIQUEFACTING A NATURAL GAS AND SHIP COMPRISING SUCH A DEVICE |
| CN109812701B (en) * | 2019-03-25 | 2024-01-23 | 智马（北京）油气设备有限公司 | Compression device for realizing gas-liquid mixed transportation system and gas-liquid mixed transportation method |
| CN110257118A (en) * | 2019-07-19 | 2019-09-20 | 中冶焦耐(大连)工程技术有限公司 | A kind of LNG pipeline forecooling method and NG cold air generating device |
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Also Published As
| Publication number | Publication date |
|---|---|
| WO2013135037A1 (en) | 2013-09-19 |
| US20150013378A1 (en) | 2015-01-15 |
| CA2864482A1 (en) | 2013-09-19 |
| CN102636000A (en) | 2012-08-15 |
| CA2864482C (en) | 2016-11-08 |
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