CN202328997U - Device for refrigerating liquefied natural gas by adopting single mixed working medium - Google Patents
Device for refrigerating liquefied natural gas by adopting single mixed working medium Download PDFInfo
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- CN202328997U CN202328997U CN201120459032.XU CN201120459032U CN202328997U CN 202328997 U CN202328997 U CN 202328997U CN 201120459032 U CN201120459032 U CN 201120459032U CN 202328997 U CN202328997 U CN 202328997U
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- 239000003949 liquefied natural gas Substances 0.000 title abstract description 25
- 239000007788 liquid Substances 0.000 claims abstract description 126
- 239000012530 fluid Substances 0.000 claims abstract description 52
- 239000012071 phase Substances 0.000 claims abstract description 34
- 239000007791 liquid phase Substances 0.000 claims abstract description 25
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 64
- 239000007789 gas Substances 0.000 claims description 52
- 238000007906 compression Methods 0.000 claims description 32
- 239000003345 natural gas Substances 0.000 claims description 32
- 230000006835 compression Effects 0.000 claims description 29
- 239000004215 Carbon black (E152) Substances 0.000 claims description 26
- 229930195733 hydrocarbon Natural products 0.000 claims description 26
- 150000002430 hydrocarbons Chemical class 0.000 claims description 26
- 238000005057 refrigeration Methods 0.000 claims description 13
- 238000003860 storage Methods 0.000 abstract description 11
- 239000003507 refrigerant Substances 0.000 abstract description 5
- 238000000926 separation method Methods 0.000 description 16
- 238000000034 method Methods 0.000 description 13
- 210000000689 upper leg Anatomy 0.000 description 10
- 238000005265 energy consumption Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 239000012808 vapor phase Substances 0.000 description 4
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 239000003915 liquefied petroleum gas Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 241000521257 Hydrops Species 0.000 description 1
- 244000188472 Ilex paraguariensis Species 0.000 description 1
- 206010030113 Oedema Diseases 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000001816 cooling Methods 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
Images
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
Abstract
The utility model relates to a device for refrigerating liquefied natural gas (LNG) by adopting a single mixed working medium. The device comprises a two-section mixed working medium compressor driven by a motor, two coolers, a liquid pump, three gas-liquid separators, two throttling devices, a plate-fin heat exchanger group and an LNG storage tank. The two-section mixed working medium compressor is used for gradually compressing and separating a mixed refrigerant; separated gas-phase and liquid-phase mixed working medium streams enter different channels of the heat exchanger group for throttling and heat exchange; and furthermore, two-stage heat exchange is adopted, so that heat exchange curves of cold fluid and hot fluid are well matched during whole heat exchange, and the flow of the mixed refrigerant is reduced effectively.
Description
Technical field
The utility model relates to the liquefaction production of being rich in hydrocarbon gas, is specifically related to a kind of device 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 a motor-driven two-period form mixed working fluid compressor, two coolers, two gas-liquid separators, two liquid pumps, a platen fin heat exchanger and a LNG storage tank; 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, and the optimization of heat transfer temperature difference receives certain limitation between the stream thigh, and plant energy consumption is higher, in addition, the varying duty running of installing is not had excellent adaptability.
The utility model content
The utility model adopts single mixed working fluid refrigeration to make natural gas liquefaction.
The utility model provides a kind of device that adopts single mixed working fluid refrigeration liquefying natural gas; It comprises azeotrope compressibility and ice chest system; Wherein the azeotrope compressibility adopts two-period form mixed working fluid compressor to compress; This compressibility comprise two-period form mixed working fluid compressor, respectively with first section two cooler that are connected with second section (i.e. first cooler and second cooler) of said two-period form mixed working fluid compressor, 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 a liquid pump being connected of first gas-liquid separator; Wherein the ice chest system comprise with said two gas-liquid separators in one group of plate-fin heat exchanger group being connected of the liquid phase end of second gas-liquid separator, two throttling arrangements that are connected with the heat exchanger channels of said plate-fin heat exchanger group and a natural gas heavy hydrocarbon separator that is connected with an independent heat exchanger channels of said plate-fin heat exchanger group; 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 a liquid pump and second compression section, and the gas phase end of second gas-liquid separator is connected with two heat exchanger channels of said one group of plate-fin heat exchanger group respectively with the liquid phase end; Wherein natural gas line is connected to the heavy hydrocarbon separator through the above-mentioned independent heat exchanger channels of heat exchanger package, is connected to the LNG storage tank behind the heat exchanger channels of the top gas phase end of heavy hydrocarbon separator through heat exchanger package.
The utility model adopts single mixed working fluid to freeze to come the device 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 compresses through secondary, follows gas-liquid separation step by step simultaneously in the compression process step by step 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; Compare traditional handicraft and saved final stage liquid pump (promptly only using a liquid pump), and adopt the secondary heat exchange to make that the heat exchange curve of hot-fluid thigh and cold flow thigh more matees in the whole process.
The single mixed working fluid of the said employing of the utility model freezes and comes the device of liquefied natural gas, comprises two-period form mixed working fluid compressor, cooler, gas-liquid separator, throttling arrangement, one group of plate-fin heat exchanger group and a LNG storage tank.The compressibility of its mix refrigerant comprises a two-period form mixed working fluid compressor, two coolers, two gas-liquid separators and a liquid pump, and the ice chest system comprises one group of plate-fin heat exchanger group (secondary heat exchange), a heavy hydrocarbon separator (gas-liquid 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 outlet of first compression section of compressor is connected to first order cooler; First order cooler is connected with first order gas-liquid separator again; The gas phase end of first order gas-liquid separator is connected to second compression section, and the bottom liquid phases end of first order gas-liquid separator is connected to a liquid pump, is connected to second-stage cooler after the outlet conduit of the output channel of this liquid pump and second compression section converges; Second-stage cooler is connected with second level gas-liquid separator again, and the top gas phase end of second level gas-liquid separator is connected with first heat exchanger channels (gas phase channel) of heat exchanger package; The bottom liquid phases end of second level gas-liquid separator is connected with second heat exchanger channels of heat exchanger package;
In the ice chest system; The liquid phase end of the second level gas-liquid separator of being derived by the azeotrope compressibility is connected to an end of first throttle device through second heat exchanger channels in the heat exchanger package, and the other end of first throttle device is connected with the 3rd heat exchanger channels of heat exchanger package; The gas phase end that gas-liquid separator top, the second level obtains is through heat exchanger package first heat exchanger channels (gas phase channel) precooling; Be connected with an end of second throttling arrangement, the other end of second throttling arrangement is connected to first compression section after being connected to the 3rd heat exchanger channels of heat exchanger package again; Natural gas line is connected to the heavy hydrocarbon separator through the 4th heat exchanger channels of heat exchanger package, and the top gas phase end of heavy hydrocarbon separator is connected to the LNG storage tank behind all the other heat exchangers at different levels (for example the 5th heat exchanger channels) through heat exchanger package successively.
The technical scheme of the utility model 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 and
Wherein the ice chest system comprises: one group of plate-fin heat exchanger group; It comprises at least five heat exchanger channels; Promptly comprise the first, second, third, fourth and the 5th heat exchanger channels at least; 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 3rd heat exchanger channels is connected to first compression section via pipeline;
First throttling arrangement that is connected with the 3rd heat exchanger channels with second heat exchanger channels of said plate-fin heat exchanger group;
Second throttling arrangement that is connected with the 3rd heat exchanger channels with first heat exchanger channels of said plate-fin heat exchanger group;
With
With an independent heat exchanger channels of said plate-fin heat exchanger group is the natural gas heavy hydrocarbon separator that the 4th 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 first heat exchanger channels be connected with second heat exchanger channels; The above-mentioned independent heat exchanger channels of the pipeline that wherein is used to carry purified natural gas through heat exchanger package i.e. the 4th 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 5th heat exchanger channels through a heat exchanger channels of heat exchanger package.
In addition, the top gas phase end of heavy hydrocarbon separator successively through behind the 5th heat exchanger channels of heat exchanger package further other the 6th heat exchanger channels through heat exchanger package be connected to LNG tank.
" first section compression " described here or " one section compression " and " first compression section " interchangeable use, by that analogy.
Operating process is described below.
The device of the said two-period form mixed working fluid of the utility model compressibility; In its azeotrope compressibility; The exit gas that compressor is first section gets into the back that is cooled in the first order cooler and carries out gas-liquid separation through first order gas-liquid separator; Gas phase after the separation continues to get into second compression section; Liquid phase after the separation through liquid pump pressurization back with converge through the hot gas after second section compression, in the gas-liquid separator of the entering second level, second-stage cooler cooling back, carry out gas-liquid separation again, first heat exchanger channels (gas phase channel) of the gas phase entering downstream heat exchanger after the separation; The liquid that gas-liquid separator bottom, the second level obtains gets into the second liquid phase heat exchanger channels of downstream heat exchanger respectively.In the ice chest system; The second liquid phase heat exchanger channels that the liquid cryogen that is come by the second level gas-liquid separator bottom of cryogen compressibility gets into heat exchanger package by precooling after again through the first throttle device, this stream after the throttling strand is back in the 3rd heat exchanger channels of heat exchanger package cold is provided; The gas phase cryogen that is come by gas-liquid separator top, the second level carries out throttling via first heat exchanger channels of heat exchanger package, second throttling arrangement of flowing through again after by precooling, in the 3rd heat exchanger channels of burst reverse entering heat exchanger package of this stream after the throttling cold is provided.The azeotrope that flows out from the 3rd heat exchanger channels is transferred gets back to first compression section.Natural gas at first is cooled to get in the heavy hydrocarbon separator after the uniform temperature through the 4th heat exchanger channels of heat exchanger package and separates; The bottom obtains the heavy hydrocarbon component; All the other heat exchangers at different levels (for example the 5th heat exchanger channels) that the gas phase that the top obtains partly continues to get into heat exchanger package carry out heat exchange; Be cooled to supercooled state, the LNG that obtains gets in the LNG storage tank and is stored.
The technological process of the device that adopts single mixed working fluid to freeze to come liquefied natural gas is following:
The natural gas circulation:
The 4th heat exchanger channels that raw natural gas after the purification at first gets into the plate-fin heat exchanger group carries out precooling; Get into the heavy hydrocarbon separator after being cooled to-30 ℃～-60 ℃ and carry out gas-liquid separation; Continue to get into all the other heat exchangers at different levels (for example the 5th heat exchanger channels) 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 (, be selected from C1, C2, C3, C4 and C5 alkane and N usually
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 first section, gets into first order cooler and is cooled to 30 ℃～40 ℃; Get into first order gas-liquid separator again and carry out gas-liquid separation; The isolated gas in first order gas-liquid separator top continues to get into second section inlet of compressor, is compressed to 1.2～5.4MPaA through two sections, and the isolated liquid of first order gas-liquid separator bottom liquid phases end is after the hot gas of liquid pump pressurization back and second section compression outlet conduit converges; Get into again and be cooled to 30 ℃～40 ℃ in the second-stage cooler; Cooled mixed working fluid gets into second level gas-liquid separator subsequently and carries out gas-liquid separation, and the top gas of second level gas-liquid separator gets into first heat exchanger channels of main heat exchanger group subsequently and participates in heat exchange, and the isolated liquid in second level 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 the gas-liquid separator bottom, the second level of mixed working fluid compressibility 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 0.25～0.75MPaA, converging and oppositely get into third level heat exchanger channels with the mixed working fluid stream thigh that flows through the first order heat exchanger channels of main heat exchanger group and return through second choke valve then is that heat exchanger package provides cold and turns back to first compression section then; Be cooled to-135 ℃～-169 ℃ by the vapor phase stream thigh of the isolated mixed working fluid in gas-liquid separator top, the second level gas phase channel (first heat exchanger channels) through heat exchanger package, reverse the 3rd heat exchanger channels that gets into heat exchanger package is that heat exchanger provides cold behind second choke valve throttling to 0.25～0.75MPaA again.
Here, pressure unit MPaA is a MPa, absolute pressure.In the utility model, generally speaking, an equipment was realized with being connected through pipeline of another equipment.
The advantage of the utility model:
1. adopt two-period form azeotrope compressor in the utility model device, azeotrope has been compressed and separation step by step step by step, reduced the power consumption of gas compression.
2. 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.
3. the gas phase and the liquid-phase mixing refrigerant flow stock that obtain through the azeotrope compressor compresses do not get into the various heat exchange passage of heat exchanger package and do not need final stage liquid pump (promptly only using a liquid pump); Make energy consumption decrease; And 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.
4. the varying duty running to device has excellent adaptability, can effectively avoid ice chest bottom hydrops, thereby guarantee that when running on the lower load product energy consumption and nominal situation energy consumption are approaching.
Description of drawings
Fig. 1 is a kind of structure chart of prior art;
Fig. 2 is the device allocation plan of the said two-period form mixed working fluid of the utility model compressibility.
The specific embodiment
Further specify below in conjunction with accompanying drawing.
Device shown in Figure 2 comprises two-period form mixed working fluid compressor 1; First cooler 21, second cooler 22; First gas-liquid separator 31, second gas-liquid separator 32, heavy hydrocarbon separator 6 (gas-liquid separator); Liquid pump 4, first throttle device 51,52, one groups of plate-fin heat exchanger groups 7 of second throttling arrangement (being the main heat exchanger group) and a LNG storage tank 8.The compressibility of its mix refrigerant comprises a two-period form mixed working fluid compressor 1; Two coolers 21,22; Two gas- liquid separators 31,32; A liquid pump 4, the ice chest system comprises one group of plate-fin heat exchanger group 7 (two-stage heat exchange), a heavy hydrocarbon separator 6 (gas-liquid separator) and two throttling arrangements 51,52; Mixed working fluid and natural gas are accomplished whole heat transfer process in the ice chest system.In the azeotrope compressibility; The outlet that compressor is 1 first section is connected to first order cooler 21; First order cooler 21 is connected with first order gas-liquid separator 31 again; The gas phase end of first order gas-liquid separator 31 is connected to second compression section, and first order gas-liquid separator 31 bottom liquid phases ends are connected to liquid pump 4, is connected to second-stage cooler 22 after the outlet conduit of the output of liquid pump 4 and second compression section converges; Second-stage cooler 22 is connected with second level gas-liquid separator 32 again, and gas-liquid separator 32 top gas phase ends in the second level are connected with first heat exchanger channels (gas phase channel) of heat exchanger package 7; Gas-liquid separator 32 bottom liquid phases ends in the second level are connected with the second liquid phase heat exchanger channels of heat exchanger package 7;
In the ice chest system; The second level gas-liquid separator 32 liquid phase ends that come by the azeotrope compressibility are connected to an end of first throttle device 51 through second heat exchanger channels in the heat exchanger package 7, and the other end of first throttle device 51 is connected with the 3rd heat exchanger channels of heat exchanger package 7; The gas phase end that secondary gas-liquid separator 32 tops obtain passes through first heat exchanger channels of heat exchanger package 7 by precooling; Be connected with second throttling arrangement, 52 1 ends, the other end of second throttling arrangement 52 is connected to first compression section after being connected to the 3rd heat exchanger channels of heat exchanger package 7 again; Natural gas line is connected to heavy hydrocarbon separator 6 through the 4th heat exchanger channels of heat exchanger package; The top gas phase end of heavy hydrocarbon separator 6 is connected to LNG storage tank 8 behind all the other heat exchangers at different levels through heat exchanger package 7 (the 5th heat exchanger channels for example, randomly can also through the 6th heat exchanger channels) successively.
The technological process of the device of use Fig. 2 is following:
The natural gas circulation:
Shown in accompanying drawing 2; Raw natural gas after the purification at first gets in the 4th heat exchanger channels in the plate-fin main heat exchanger group 7 (two-stage heat exchange) by precooling; Get in the heavy hydrocarbon separator 6 after being cooled to-30 ℃～-60 ℃ and carry out gas-liquid separation; Continue to get into all the other heat exchangers at different levels of main heat exchanger group 7 by the isolated vapor phase stream thigh in heavy hydrocarbon separator 6 tops; And be cooled to-130 ℃～-166 ℃ therein, and the liquefied natural gas that obtains is sent in the LNG storage tank 8 and is stored, and the bottom of heavy hydrocarbon separator 6 obtains liquefied petroleum gas (LPG).
The azeotrope circulation:
By C1～C5 and N
2The mixed working fluid of forming is selected from C1, C2, C3, C4 and C5 alkane and N usually
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 second section inlet of entering compressor, and warp is compressed to 1.2～5.4MPaA for two sections, and the isolated liquid of first order gas-liquid separator 31 bottom liquid phases ends is after the hot gas that exports with two sections compressions after 4 pressurizations of liquid pump converges; Get into second-stage cooler 22 again and be cooled to 30 ℃～40 ℃; Cooled mixed working fluid gets into subsequently and carries out gas-liquid separation in the second level gas-liquid separator 32, and gas-liquid separator 32 top gas in the second level get into first heat exchanger channels of main heat exchanger group 7 subsequently and participate in heat exchange, and the isolated liquid in second level gas-liquid separator 32 bottoms gets into second heat exchanger channels of main heat exchanger group 7 and participates in heat exchange;
The liquid of drawing from second level gas-liquid separator 32 bottoms of mixed working fluid compressibility at first gets into second heat exchanger channels of heat exchanger package; Therein by-30 ℃～-80 ℃ extremely approximately of precoolings; The mixed working fluid stream that behind choke valve 51 throttlings to 0.25～0.75MPaA, returns (promptly flowing through first heat exchanger channels and second choke valve) with the first-class heat exchanger from heat exchanger package 7 back strand converges and oppositely gets into previous stage heat exchanger (i.e. the 3rd heat exchanger channels) provides cold for heat exchanger package 7; Be cooled to-135 ℃～-169 ℃ by the vapor phase stream thigh of the isolated mixed working fluid in the second level gas-liquid separator 32 tops gas phase channel (i.e. first heat exchanger channels) through heat exchanger package 7; Again behind second choke valve, 52 throttlings to 0.25～0.75MPaA in reverse the 3rd heat exchanger channels that gets into heat exchanger package 7 for heat exchanger package provides cold, turn back to first compression section then.
Claims (2)
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 and
Wherein the ice chest system comprises:
One group of plate-fin heat exchanger group; It comprises at least five heat exchanger channels: the first, second, third, fourth and the 5th heat exchanger channels; 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 3rd heat exchanger channels is connected to first compression section via pipeline;
First throttling arrangement that is connected with the 3rd heat exchanger channels with second heat exchanger channels of said plate-fin heat exchanger group;
Second throttling arrangement that is connected with the 3rd heat exchanger channels with first heat exchanger channels of said plate-fin heat exchanger group;
With
With an independent heat exchanger channels of said plate-fin heat exchanger group is the natural gas heavy hydrocarbon separator that the 4th 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 first heat exchanger channels be connected with second heat exchanger channels; The above-mentioned independent heat exchanger channels of the pipeline that wherein is used to carry purified natural gas through heat exchanger package i.e. the 4th 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 5th 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 5th heat exchanger channels of heat exchanger package further other the 6th heat exchanger channels through heat exchanger package be connected to LNG tank.
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120459032.XU CN202328997U (en) | 2011-11-18 | 2011-11-18 | Device for refrigerating liquefied natural gas by adopting single mixed working medium |
| CA2856096A CA2856096C (en) | 2011-11-18 | 2012-09-13 | System and method for liquefying natural gas using single mixed refrigerant as refrigeration medium |
| PCT/CN2012/081334 WO2013071789A1 (en) | 2011-11-18 | 2012-09-13 | Device and method for liquefying natural gas using single mixed working medium as refrigeration medium |
| US14/354,964 US20140283548A1 (en) | 2011-11-18 | 2012-09-13 | System and method for liquefying natural gas using single mixed refrigerant as refrigeration medium |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120459032.XU CN202328997U (en) | 2011-11-18 | 2011-11-18 | Device for refrigerating liquefied natural gas by adopting single mixed working medium |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202328997U true CN202328997U (en) | 2012-07-11 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201120459032.XU Expired - Lifetime CN202328997U (en) | 2011-11-18 | 2011-11-18 | Device for refrigerating liquefied natural gas by adopting single mixed working medium |
Country Status (4)
| Country | Link |
|---|---|
| US (1) | US20140283548A1 (en) |
| CN (1) | CN202328997U (en) |
| CA (1) | CA2856096C (en) |
| WO (1) | WO2013071789A1 (en) |
Cited By (5)
| 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 |
| CN103712413A (en) * | 2013-12-31 | 2014-04-09 | 苏州制氧机有限责任公司 | Natural gas liquefaction device |
| CN104807287A (en) * | 2015-05-22 | 2015-07-29 | 中国石油集团工程设计有限责任公司 | Small natural gas liquefaction and refrigeration system and small natural gas liquefaction and refrigeration method |
| CN108955084A (en) * | 2013-03-15 | 2018-12-07 | 查特能源化工公司 | Mixed refrigerant systems and method |
| CN111238163A (en) * | 2020-02-13 | 2020-06-05 | 中国科学院理化技术研究所 | Mixed working medium high-pressure gas liquefaction and supercooling system |
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| WO2016094168A1 (en) | 2014-12-12 | 2016-06-16 | Dresser-Rand Company | System and method for liquefaction of natural 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 |
| US10619918B2 (en) | 2015-04-10 | 2020-04-14 | Chart Energy & Chemicals, Inc. | System and method for removing freezing components from a feed gas |
| FR3043451B1 (en) * | 2015-11-10 | 2019-12-20 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | METHOD FOR OPTIMIZING NATURAL GAS LIQUEFACTION |
| CN108885035B (en) | 2016-03-31 | 2021-04-16 | 开利公司 | Refrigeration circuit |
| CA2963649C (en) | 2016-04-11 | 2021-11-02 | 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 |
| WO2019140033A1 (en) * | 2018-01-12 | 2019-07-18 | Edward Peterson | Thermal cascade for cryogenic storage and transport of volatile gases |
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| GB895094A (en) * | 1959-10-21 | 1962-05-02 | Shell Int Research | Improvements in or relating to process and apparatus for liquefying natural gas |
| US3808826A (en) * | 1970-09-28 | 1974-05-07 | Phillips Petroleum Co | Refrigeration process |
| DE69523437T2 (en) * | 1994-12-09 | 2002-06-20 | Kobe Steel Ltd | Gas liquefaction plant and method |
| 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 |
| 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 |
| 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 |
-
2011
- 2011-11-18 CN CN201120459032.XU patent/CN202328997U/en not_active Expired - Lifetime
-
2012
- 2012-09-13 CA CA2856096A patent/CA2856096C/en active Active
- 2012-09-13 US US14/354,964 patent/US20140283548A1/en not_active Abandoned
- 2012-09-13 WO PCT/CN2012/081334 patent/WO2013071789A1/en active Application Filing
Cited By (7)
| 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 |
| CN108955084A (en) * | 2013-03-15 | 2018-12-07 | 查特能源化工公司 | Mixed refrigerant systems and method |
| CN103712413A (en) * | 2013-12-31 | 2014-04-09 | 苏州制氧机有限责任公司 | Natural gas liquefaction device |
| CN103712413B (en) * | 2013-12-31 | 2018-08-17 | 苏州制氧机有限责任公司 | A kind of natural gas liquefaction device |
| CN104807287A (en) * | 2015-05-22 | 2015-07-29 | 中国石油集团工程设计有限责任公司 | Small natural gas liquefaction and refrigeration system and small natural gas liquefaction and refrigeration method |
| CN111238163A (en) * | 2020-02-13 | 2020-06-05 | 中国科学院理化技术研究所 | Mixed working medium high-pressure gas liquefaction and supercooling system |
| CN111238163B (en) * | 2020-02-13 | 2021-12-17 | 中国科学院理化技术研究所 | Mixed working medium high-pressure gas liquefaction and supercooling system |
Also Published As
| Publication number | Publication date |
|---|---|
| CA2856096A1 (en) | 2013-05-23 |
| US20140283548A1 (en) | 2014-09-25 |
| WO2013071789A1 (en) | 2013-05-23 |
| CA2856096C (en) | 2018-06-19 |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
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Granted publication date: 20120711 |