CN100565060C - A kind of method of natural gas liquefaction and device thereof - Google Patents
A kind of method of natural gas liquefaction and device thereof Download PDFInfo
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- CN100565060C CN100565060C CNB2007100784413A CN200710078441A CN100565060C CN 100565060 C CN100565060 C CN 100565060C CN B2007100784413 A CNB2007100784413 A CN B2007100784413A CN 200710078441 A CN200710078441 A CN 200710078441A CN 100565060 C CN100565060 C CN 100565060C
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- liquid
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- natural gas
- methane
- propane
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 491
- 239000003345 natural gas Substances 0.000 title claims abstract description 109
- 238000000034 method Methods 0.000 title claims abstract description 59
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 204
- 239000007789 gas Substances 0.000 claims abstract description 159
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 123
- 239000001294 propane Substances 0.000 claims abstract description 103
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 50
- 238000001704 evaporation Methods 0.000 claims abstract description 34
- 230000008020 evaporation Effects 0.000 claims abstract description 34
- 239000003507 refrigerant Substances 0.000 claims abstract description 20
- 239000007788 liquid Substances 0.000 claims description 186
- 239000005977 Ethylene Substances 0.000 claims description 60
- 238000000926 separation method Methods 0.000 claims description 56
- 239000003595 mist Substances 0.000 claims description 51
- 239000012530 fluid Substances 0.000 claims description 45
- 238000001816 cooling Methods 0.000 claims description 25
- 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
- 238000002156 mixing Methods 0.000 claims description 21
- 230000005484 gravity Effects 0.000 claims description 9
- 239000012535 impurity Substances 0.000 claims description 8
- 238000007789 sealing Methods 0.000 claims description 8
- 229910001220 stainless steel Inorganic materials 0.000 claims description 7
- 239000010935 stainless steel Substances 0.000 claims description 7
- 238000004781 supercooling Methods 0.000 claims description 7
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 6
- 238000010521 absorption reaction Methods 0.000 claims description 6
- 239000002826 coolant Substances 0.000 claims description 6
- 229910052802 copper Inorganic materials 0.000 claims description 6
- 239000010949 copper Substances 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 5
- 238000003860 storage Methods 0.000 claims description 4
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 claims description 3
- 239000003245 coal Substances 0.000 abstract description 9
- 238000012544 monitoring process Methods 0.000 abstract description 4
- 238000009434 installation Methods 0.000 abstract 1
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- 239000000203 mixture Substances 0.000 description 9
- 241000196324 Embryophyta Species 0.000 description 8
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
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- 150000001335 aliphatic alkanes Chemical class 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000002360 explosive Substances 0.000 description 3
- 239000002737 fuel gas Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- 230000003416 augmentation Effects 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
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- 230000000630 rising effect Effects 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 241000519996 Teucrium chamaedrys Species 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
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- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002699 waste material Substances 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
- F25J1/0032—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- 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
- F25J1/0032—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
-
- 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
- F25J1/0201—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 only internal refrigeration means, i.e. without external refrigeration
- F25J1/0202—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 only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
-
- 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
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
-
- 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
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
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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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
- F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
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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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
Abstract
A kind of method of natural gas liquefaction and device thereof.The present invention only compresses circulating refrigerant and the raw natural gas that is formed by propane, ethene and methane blended with a compressor, and then liquefied natural gas.Package unit has successively the compressor that connects, cooler, the separator box of each component, cooler, on-condensible gas separator box and the liquid natural gas holding vessel etc. of each component.The present invention is corresponding component in having solved stage evaporation, resorption circulating refrigerant, only allow two strands of air-flows carry out the actual application problem of heat exchange after, proposed to control the method and the apparatus structure thereof of each component resorption amount again with the mode of level monitoring.Apparatus structure and operating procedure thereof have further been simplified.Installation cost of the present invention and operating cost are low, are suitable for the daily output less than 50000Nm
3, the residue Device in Gas that can not all utilize after from the coal seam, extracting out, the liquefaction of the natural gas in the unprofitable abandoned well originally.
Description
Technical field
The present invention relates to the liquifying method and the device thereof of combustion gas, relate in particular to method and device thereof that natural gas that methane content is produced at the coal bed gas more than 90%, low yield gas well liquefies.
Background technology
Comprised alkanes fuel gas in the component of coal bed gas (also claiming Device in Gas) based on methane.The natural gas of exploiting out from gas well also is the alkanes fuel gas based on methane.So in this case, both unified natural gases that calls.
Wherein, the natural gas in the coal seam is the arch-criminal that the colliery gas explosion takes place, causes mine disaster.One of way that prevents gas explosion is earlier natural gas to be extracted out by the collecting pipe that pierces in the coal seam before seam mining.Near resident's the daily life natural gas of extracting out all is used for.But too much at the natural gas of extracting out, near resident when toing many or too much for use, just having to runs in these exhaustless natural gas straights to put or be allowed to condition in the atmosphere burns.Like this, not only cause great waste, but also had influence on environment.If can be liquid natural gas (LNG) with these coal gas gasifications, be transported to the city of closing on, in supply station after the vaporization, resupply civilian or to the refueling comparatively feasible scheme of will can yet be regarded as with tank car.Five, the sixties, early had natural gas liquefaction device abroad, China has also introduced several.At present, by domestic deep cooling industry and research institutions' independent research, also produced many.From the liquefaction flow path aspect, above-mentioned existing apparatus adopts the cascade system of multi-stage compression mostly, promptly adopts the independently circulation separately of cold-producing mediums such as freon, propane, ethane, nitrogen.For reclaiming callable energy as much as possible, also used decompressor to recover energy in its system as throttling arrangement.In addition, no matter above that a kind of liquefying plant, its heat-exchanger rig has all adopted the aluminum plate-fin type high-performance heat exchanger.
Yet, because the daily output of external natural gas liquefaction device is all at hundreds of thousands～millions of Nm
3Between, the daily output of the natural gas liquefaction device of domestic independent research also is not less than 50000Nm
3And single group coal bed gas well yield is generally all little, usually only at 5000～20000Nm
3Between/day.Therefore, no matter be to introduce abroad, or buy domestic independent research, not only the natural gas liquefaction in single group coal seam is seemed excessive, and operating cost is also very high.In addition, various places are in the natural gas drilling process, because of the daily output is crossed low unprofitable substantially abandoned well (just having about 200～300 mouthfuls) also quite a lot in the scope of Chongqing.Equally also need to be fit to the natural gas liquefaction device of its corresponding gas production, so that these abandoned wells obtain utilizing.But, at present at home and abroad all less than suitable its daily output less than 50000Nm
3, natural gas liquefaction device that operating cost is cheap.Reason be present these separately independent cooling agent circulation liquid device, need multiple compressors, multiply air-flow to carry out heat exchange, all be not suitable for midget plant from investment, processing technology and operational management aspect.
Say that in theory only the natural gas liquefaction that compresses full mix refrigerant with the separate unit compressor is feasible.But up to the present, also only rest in the theoretic discussion, go back real method and the utility unit of implementing thereof of neither one so far.
Summary of the invention
First purpose of the present invention is that a kind of little gas production that is suitable for that can implement is provided, and (daily output is less than 50000Nm
3) natural gas liquefaction;
Second purpose of the present invention is, provides a kind of and is suitable for little gas production (daily output is less than 50000Nm
3) small-scaled natural gas liquification device.
The 3rd purpose of the present invention is that a kind of apparatus structure with low cost, can monitor and adjust the mix refrigerant ratio in small-scaled natural gas liquification device is provided.
For reaching first goal of the invention, provide a kind of like this method of natural gas liquefaction.Its aspect same as the prior art is to have adopted compressor and cold-producing medium in the method.Its improvements are, the compressor among the present invention only needs one, and cold-producing medium is the circulating refrigerant that is formed by propane, ethene and methane blended.The weight mixing ratio of propane, ethene and methane is that (specify: natural gas itself was exactly based on the alkanes fuel gas of methane content in 1.76: 1.27: 1.0, the present invention puts forward methane separately and natural gas difference statement, be because this part methane is brought as the cold-producing medium utilization in the process of preparation liquefied natural gas and finally do not stored and transport outward with liquefied natural gas, but return compressor) as backflow.
The process of natural gas liquefaction of the present invention comprises:
A, the raw natural gas that will remove impurity and circulating refrigerant suck the step in this compressor, to compress together.
B, the HTHP mist from the output of this compressor is cooled off, the heavy hydrocarbon component that will bring from raw natural gas then, be condensed into liquid through cooling separates and gets rid of the step of this heavy hydrocarbon component from this mist.
C, the mist of having removed the heavy hydrocarbon component is further cooled off, with the step of the biphase gas and liquid flow that obtains having LPG.
D, LPG is separated from the biphase gas and liquid flow at its place, then this LPG is carried out the throttling step-down, allows its required amount evaporation of returning propane flammable gas according to keeping mixing ratio, and borrow its evaporation endothermic process to come the mist of remainder is further cooled off, to obtain having the biphase gas and liquid flow of liquid ethylene, then the propane flammable gas after the heat absorption is transmitted back to the step of going in the compressor.
E, liquid ethylene is separated from the biphase gas and liquid flow at its place, then this liquid ethylene is carried out the throttling step-down, allows the ethene tolerance evaporation that it need return according to keeping mixing ratio, and borrow its evaporation endothermic process to come the mist of remainder is further cooled off, to obtain having the biphase gas and liquid flow of liquid methane, then the ethylene gas after the heat absorption is transmitted back to the step of going in the compressor.
F, the biphase gas and liquid flow that has liquid methane is carried out the throttling step-down and allows methane liquid partly evaporate; Then liquid methane is separated, as cooling medium, be allowed to condition at further cooled natural gas in the subsequent process, make it liquefaction after the throttling step-down, then further make the cold excessively step of liquefied natural gas.
G, last is a step of overcooled liquified natural gas being injected the liquid natural gas holding vessel.
Further improve and be, in above-mentioned steps f, natural gas is carried out also having a step of separating and get rid of incoagulable gas from the natural gas that is cooled to liquid before the supercooling.
For reaching second goal of the invention, provide a kind of like this device of natural gas liquefaction.Aspect same as the prior art is in this device compressor to be arranged.Its improvements are, the compressor among the present invention only has one, and what compress by this compressor is to have removed the raw natural gas of impurity and the circulating refrigerant that is formed by propane, ethene, methane blended.The weight mixing ratio of propane, ethene and methane is 1.76: 1.27: 1.0.
The equipment that connects successively after this compressor comprises:
Cooling is from first aftercooler of the HTHP mist of compressor output;
The heavy hydrocarbon component that brings from raw natural gas, be condensed into liquid through cooling separated from this mist and this heavy hydrocarbon component get rid of from its bottom, the heavy hydrocarbon separator box of this mist from its top output;
The mist of having removed the heavy hydrocarbon component is cooled off, with second aftercooler of the biphase gas and liquid flow that obtains having LPG;
The propane fluid separation applications case of the gravity type that LPG is separated from the biphase gas and liquid flow at its place; Isolated LPG is from the bottom output of this propane fluid separation applications case, and remaining mist is from the top output of this propane fluid separation applications case;
One allows the remaining mist that has separated propane enter further cooling in the dish type heat exchanger tube that is provided with in its shell space on its housing top, to obtain having the biphase gas and liquid flow of liquid ethylene, after allowing LPG by a choke valve throttling step-down that bottom propane fluid separation applications case, communicates simultaneously, entering the amount that need return propane flammable gas in its shell space according to keeping mixing ratio at its housing middle part by several nozzles (this specific embodiment is 12) evaporates, and the propane flammable gas that evaporation is obtained be transmitted back to go in the compressor before, cool off earlier the propane cooler of the mist in this dish type heat exchanger tube as cold-producing medium;
The Ethylene Liquid separator box of the gravity type that liquid ethylene is separated from the biphase gas and liquid flow at its place; Isolate the bottom output of liquid ethylene from this Ethylene Liquid separator box, remaining mist is from the top output of this Ethylene Liquid separator box;
One allows the remaining mist that has separated ethene enter further cooling in the dish type heat exchanger tube that is provided with in its shell space on its housing top, to obtain having the biphase gas and liquid flow of liquid methane, after allowing liquid ethylene by a choke valve throttling step-down that bottom the Ethylene Liquid separator box, communicates simultaneously, entering the amount that need return ethylene gas in its shell space according to keeping mixing ratio at its housing middle part by several nozzles evaporates, and ethylene gas that evaporation is obtained be transmitted back to through propane cooler go in the compressor before, cool off the ethylene chiller of the mist in this dish type heat exchanger tube earlier as cold-producing medium;
The biphase gas and liquid flow that has separated ethene and had a liquid methane imported in the dish type heat exchanger tube that is provided with in its shell space a return-air cooler of further cooling and liquefaction;
The methane fluid separation applications case of the gravity type that liquid methane is separated from the biphase gas and liquid flow at its place; Isolate the bottom output of liquid methane from this methane fluid separation applications case, remaining natural gas is from the top output of this methane fluid separation applications case;
The remaining natural gas that handle has separated liquid methane enters further cooling in the dish type heat exchanger tube that is provided with in its shell space on its housing top, allow simultaneously isolated liquid methane by with a choke valve throttling step-down that methane fluid separation applications case bottom communicates after, in its lower housing portion enters its shell space according to keeping the required methane tolerance evaporation of mixing ratio, and the methane gas that evaporation obtains cooled off as cold-producing medium and this dish type heat exchanger tube that liquefies in the methane cooler of natural gas;
The upper end of an interior dish type heat exchanger tube that is provided with of its shell space and the dish type heat exchanger tube lower end UNICOM in the methane housing of cooler body space, its dish type heat exchanger tube lower end is by the liquefied natural gas subcooler of a control valve and a liquid natural gas holding vessel UNICOM;
And the choke valve and methane cooler casing of methane fluid separation applications case bottom UNICOM between, be connected with a branched pipe.The housing UNICOM of the other end of this branched pipe and liquefied natural gas subcooler to allow by the methane after this choke valve throttling step-down, does further supercooling to the natural gas in the dish type heat exchanger tube in this liquefied natural gas subcooler simultaneously.Between the housing bottom between the housing middle part of the case top of this liquefied natural gas subcooler and methane cooler, at the case top of this methane cooler and return-air cooler, between in the middle part of the housing of the case top of this return-air cooler and ethylene chiller, respectively be connected with a muffler.
Further improve is that an incoagulable gas separator box has been advanced in series connection between two groups of dish type heat exchanger tubes of methane cooler and liquefied natural gas subcooler.This incoagulable gas separator box is made of with the flash chamber that is positioned at its underpart the incoagulable gas separation chamber that is positioned at its top.The dish type heat exchanger tube UNICOM of this incoagulable gas separation chamber and methane cooler, an incoagulable gas delivery pipe is arranged at its top; The dish type heat exchanger tube UNICOM of the bottom of this flash chamber and liquefied natural gas subcooler, its top is by the housing UNICOM of a choke valve and methane cooler.Pass through a choke valve UNICOM between incoagulable gas separation chamber and the flash chamber.
Further improving is that in said apparatus, all dish type heat exchanger tubes all are to be made by low temperature resistant stainless steel tube or copper pipe.
For reaching the 3rd goal of the invention, provide a kind of like this and can in small-scaled natural gas liquification device, monitor and the apparatus structure of adjusting the mix refrigerant ratio.This apparatus structure is: in the bottom of propane cooler and ethylene chiller, respectively be connected with a liquid level gauge that is filled with painted refrigerator oil in it.Be to be the liquid sealing pipe UNICOM of being inverted the U font between the bottom liquid of the lower end of each liquid level gauge and each corresponding cooler by one section, the headroom UNICOM of the upper end of each liquid level gauge and corresponding cooler.Near liquid level gauge one side the painted refrigerator oil storage tube that has enlarged diameter in a section is arranged at this liquid sealing pipe.Under LPG in propane cooler and ethylene chiller bottom, the liquid ethylene liquid level discharging tube is arranged respectively, a blowdown pipe is respectively arranged on this liquid level, and the media outlet that is cooled in propane cooler and ethylene chiller bottom respectively has a point for measuring temperature.
Compare with the method and the device thereof of existing natural gas liquefaction, superiority of the present invention is as follows:
1, from the scheme that realizes first, second goal of the invention as can be seen, because the present invention is according to the needs of miniaturization, only adopted a compressor to compress multiple cold-producing medium and substituted the decompressor in the existing apparatus with choke valve, like this, only on higher compressor of expense ratio and decompressor, just saved a large amount of costs.After being well understood to method of the present invention and device thereof, those skilled in the art can enough public methods (and instrument) monitor and adjust the ratio that is transmitted back to each component in the mix refrigerant that goes in the compressor fully.If can be in conjunction with spectrum analysis, then the control of its component ratio and adjustment be with more convenient.Like this, both overcome in existing large-scale plant the sort of separately independently the circulatory system, multiply air-flow carry out heat exchange, and need the defective of multiple compressors, complicated heat exchanger equipment and complicated technology; Again the natural gas liquefaction (promptly only having heat exchange in device between two strands of air-flows) of the full mix refrigerant that only compresses with the separate unit compressor rise to can practice degree.
2, the further improvement part from realize second goal of the invention as can be seen since this device in the dish type heat exchanger tube make by low temperature resistant stainless steel tube or copper pipe.So, changeable to the component that coal bed gas, this class of low yield gas well gas have, the uncertain source of the gas of impurity content in the unstripped gas, just needn't be as treating aluminum plate-fin heat exchanger of the prior art, very high to the purification requirement of unstripped gas, as could to guarantee equipment long-term, operation reliably.Remove that impurity (has generally included H in the raw natural gas
2S, SO
2, CO
2, H
2O, N
2, O
2And Hg etc.) after requirement reduced, equipment cost and operating cost can be saved many again.
3, for ease of understanding, realize the monitoring and principle and the operating process of adjusting the mix refrigerant ratio of the 3rd goal of the invention apparatus structure, in having " specific embodiment " of Reference numeral, introduce, only introduce its advantage in this part.Its advantage is, saved spectroanalysis instrument etc. and has been used in the instrument that its price too seems expensive in the small-scaled natural gas liquification device, saved a large sum of training, management and maintenance funds.
In addition, compared with prior art, because in the present invention, capital equipment and pertinent instruments have been reduced or have simplified, so package unit just can manufacture the version of being convenient to cut to, for example: skid-mounted type.Like this, for coal bed gas and gas stringer, have more applicability, utilization rate is higher.
The present invention is further illustrated below in conjunction with accompanying drawing.
Description of drawings
The flow system schematic diagram of Fig. 1---natural gas liquefaction device of the present invention
Fig. 2---propane among the present invention (or ethene) fluid separation applications case and propane (or ethene) cooler package are combined into the structural representation (two assemblies are basic identical, just in the assembly that Ethylene Liquid separator box and ethylene chiller are combined into less than the ethylene gas muffler that is drawn by double dot dash line) of a component devices
Fig. 3---methane fluid separation applications case, methane cooler, incoagulable gas separator box, liquefied natural gas subcooler and liquefied natural gas subcooler are combined as the structural representation of a component devices among the present invention
The specific embodiment
A kind of method of natural gas liquefaction has adopted compressor and cold-producing medium in the method.Compressor in the inventive method only needs one, and cold-producing medium of the present invention is the circulating refrigerant that is formed by propane, ethene and methane blended.The weight mixing ratio of propane, ethene and methane is 1.76: 1.27: 1.0.
The process of its natural gas liquefaction comprises:
A, the raw natural gas that will remove impurity and circulating refrigerant suck the step in this compressor, to compress together.In this step, its compressor delivery pressure is 3.0Mpa～4.0Mpa, and outlet temperature is 120 ℃～140 ℃.
B, the HTHP mist from the output of this compressor is cooled off, the heavy hydrocarbon component that will bring from raw natural gas then, be condensed into liquid through cooling separates and gets rid of the step of this heavy hydrocarbon component from this mist.In this step, the temperature after mist is cooled is 79 ℃～81 ℃.
C, the mist of having removed the heavy hydrocarbon component is further cooled off, with the step of the biphase gas and liquid flow that obtains having LPG.In this step, the temperature after mist is cooled is 30 ℃～35 ℃.
D, LPG is separated from the biphase gas and liquid flow at its place, then this LPG is carried out the throttling step-down, allows its required amount evaporation of returning propane flammable gas according to keeping mixing ratio, and borrow its evaporation endothermic process to come the mist of remainder is further cooled off, to obtain having the biphase gas and liquid flow of liquid ethylene, then the propane flammable gas after the heat absorption is transmitted back to the step of going in the compressor.In this step, the pressure after its LPG throttling step-down is 0.102Mpa～0.105Mpa, at this moment, the temperature of having evaporated and not evaporated the biphase gas and liquid flow of propane after the throttling is-42 ℃～-40 ℃.The resulting temperature that has the biphase gas and liquid flow of liquid ethylene in back that is cooled is-38 ℃～-36 ℃.
E, liquid ethylene is separated from the biphase gas and liquid flow at its place, then this liquid ethylene is carried out the throttling step-down, allows the ethene tolerance evaporation that it need return according to keeping mixing ratio, and borrow its evaporation endothermic process to come the mist of remainder is further cooled off, to obtain having the biphase gas and liquid flow of liquid methane, then the ethylene gas after the heat absorption is transmitted back to the step of going in the compressor.In this step, pressure after its liquid ethylene throttling step-down is 0.102Mpa～0.105Mpa, the temperature of having evaporated and not evaporated the biphase gas and liquid flow of ethene after the throttling is-103 ℃～-102 ℃, and the resulting temperature that has the biphase gas and liquid flow of liquid methane in cooling back is-98 ℃～-97 ℃.
F, the biphase gas and liquid flow that has liquid methane is carried out the throttling step-down, its pressure is dropped to 1.25Mpa～1.6Mpa and allows methane liquid partly evaporate, make temperature drop to-119 ℃; Then liquid methane is separated, as cooling medium, be allowed to condition at further cooled natural gas in the subsequent process, make it liquefaction after the throttling step-down, then further make the cold excessively step of liquefied natural gas.In this step, afterwards as cooling medium, the pressure after its step-down is 0.102Mpa～0.105Mpa to liquid methane by the throttling step-down, and temperature is-163 ℃～-162 ℃.
G, last is a step of overcooled liquified natural gas being injected the liquid natural gas holding vessel.
In this specific embodiment, for the incoagulable gas that is not subjected to bring from raw natural gas influences, with guarantee to compress, the process of liquefied natural gas can go on constantly, in step f, natural gas is carried out before the supercooling, also increase a step of from the natural gas that is cooled to liquid, separating and get rid of incoagulable gas.In this step, the pressure that separates and get rid of incoagulable gas is 1.5Mpa～1.6Mpa, and temperature is-120 ℃～-119 ℃; After getting rid of incoagulable gas, liquified natural gas is further throttling step-down again, and pressure is reduced to 0.5Mpa from 1.5Mpa～1.6Mpa; Reduce to-158 ℃ through temperature after the supercooling again.
After those skilled in the art had carefully understood the step of natural gas liquefaction of the present invention and whole process thereof, one surely according to the content that discloses previously, designed and realized that various devices of the present invention come.Below, in conjunction with the method for above-mentioned natural gas liquefaction, further disclose device of the present invention (with reference to figure 1).
In the natural gas liquefaction device of the present invention, compressor 1 only has one (obviously, in order to guarantee enough outlet pressures, selected compressor should be a double-stage compressor), what compress by this compressor 1 is to have removed the raw natural gas of impurity and the circulating refrigerant that is formed by propane, ethene, methane blended.Wherein, the mix refrigerant weight mixing ratio of propane, ethene and methane is 1.76: 1.27: 1.0.
The equipment that connects successively after this compressor 1 comprises:
Cooling is from first aftercooler 2 of the HTHP mist of compressor 1 output;
The heavy hydrocarbon component that brings from raw natural gas, be condensed into liquid through cooling separated from this mist and this heavy hydrocarbon component get rid of from its bottom, a heavy hydrocarbon separator box 3 (the heavy hydrocarbon component of eliminating of this mist from its top output, it can be vaporized once more, as fuel; Or with liquid situation sale);
The mist of having removed the heavy hydrocarbon component is cooled off, with second aftercooler 4 (first and second coolers are bought commercially available water-cooled cooler and get final product, and are common, provide by Compressors Factory is supporting) of the biphase gas and liquid flow that obtains having LPG;
The propane fluid separation applications case 5 of the gravity type that LPG is separated from the biphase gas and liquid flow at its place; Isolated LPG is from the bottom output of this propane fluid separation applications case 5, and remaining mist is from the top output (with reference to figure 2) of this propane fluid separation applications case 5;
One allows the remaining mist that has separated propane enter further cooling in the dish type heat exchanger tube that is provided with in its shell space on its housing top, to obtain having the biphase gas and liquid flow of liquid ethylene, allow simultaneously LPG by with a choke valve 6 throttling step-downs that propane fluid separation applications case 5 bottoms communicate after, entering the amount that need return propane flammable gas in its shell space according to keeping mixing ratio at its housing middle part by several nozzles (this specific embodiment is 12) evaporates, and the propane flammable gas that evaporation is obtained be transmitted back to go in the compressor 1 before, cool off earlier the propane cooler 7 (with reference to figure 2) of the mist in this dish type heat exchanger tube as cold-producing medium;
The Ethylene Liquid separator box 8 of the gravity type that liquid ethylene is separated from the biphase gas and liquid flow at its place; Isolate the bottom output of liquid ethylene from this Ethylene Liquid separator box 8, remaining mist is from the top output (with reference to figure 2) of this Ethylene Liquid separator box 8;
One allows the remaining mist that has separated ethene enter further cooling in the dish type heat exchanger tube that is provided with in its shell space on its housing top, to obtain having the biphase gas and liquid flow of liquid methane, after allowing liquid ethylene by a choke valve 9 throttling step-downs that communicate with Ethylene Liquid separator box 8 bottoms simultaneously, entering the amount that need return ethylene gas in its shell space according to keeping mixing ratio at its housing middle part by several nozzles (this specific embodiment is 12) evaporates, and ethylene gas that evaporation is obtained be transmitted back to through propane cooler 7 go in the compressor 1 before, cool off the ethylene chiller 10 (with reference to figure 2) of the mist in this dish type heat exchanger tube earlier as cold-producing medium;
The biphase gas and liquid flow that has separated ethene and had a liquid methane imported in the dish type heat exchanger tube that is provided with in its shell space a return-air cooler 11 of further cooling and liquefaction;
The methane fluid separation applications case 13 of a gravity type 11 that be connected by a choke valve 12 and this return-air cooler, that liquid methane is separated from the biphase gas and liquid flow at its place; Isolate the bottom output of liquid methane from this methane fluid separation applications case 13, remaining natural gas is from the top output (with reference to figure 3) of this methane fluid separation applications case 13;
The remaining natural gas that handle has separated liquid methane enters further cooling in the dish type heat exchanger tube that is provided with in its shell space on its housing top, allow simultaneously isolated liquid methane by with a choke valve 14 throttling step-downs that methane fluid separation applications case 13 bottoms communicate after, in entering its shell space, its lower housing portion evaporates according to the required methane tolerance of maintenance mixing ratio, and the methane gas that evaporation obtains cooled off as cold-producing medium and this dish type heat exchanger tube that liquefies in the methane cooler 15 of natural gas (with reference to figure 1, Fig. 3)---from the f of aforementioned liquefaction mode the step as can be seen, in this methane cooler 15, natural gas should liquefy, therefore, in order to ensure there being enough methane refrigerant to enter in this methane cooler 15, can be arranged on control valve 141 apertures in the following branched pipe by adjusting, perhaps by the different restricting orifice of its pore size be set respectively on the branched pipe pipeline realize upper and lower the stating of the pipeline that enters this methane cooler 15 behind the choke valve 14;
The upper end of an interior dish type heat exchanger tube that is provided with of its shell space and the dish type heat exchanger tube lower end UNICOM in methane cooler 15 shell spaces, its dish type heat exchanger tube lower end is by the liquefied natural gas subcooler 19 of a control valve 201 and liquid natural gas holding vessel 20 UNICOMs.Between this liquid natural gas holding vessel 20 and liquefied natural gas subcooler 19 housings, be connected to the return-air valve 191 of a steady pressure, so that be heated when boosting or annotating liquid natural gas, to the gaseous natural gas of liquefied natural gas subcooler 19 discharging superpressures at liquid natural gas holding vessel 20.
And the choke valve 14 and methane cooler 15 housings of methane fluid separation applications case 13 bottom UNICOMs between, be connected with a branched pipe.The housing UNICOM of the other end of this branched pipe and liquefied natural gas subcooler 19, to allow, simultaneously the natural gas in the dish type heat exchanger tube in this liquefied natural gas subcooler 19 is done further supercooling (purpose is to reduce the evaporation loss of liquefied natural gas in storage and transportation) by the methane after the 14 throttling step-downs of this choke valve.Between the housing bottom between the housing middle part of the case top of this liquefied natural gas subcooler 19 and methane cooler 15, at the case top of this methane cooler 15 and return-air cooler 11, between in the middle part of the housing of the case top of this return-air cooler 11 and ethylene chiller 10, respectively be connected with a muffler.
As said in aforementioned liquifying method, for the incoagulable gas that is not subjected to bring from raw natural gas influences, with guarantee to compress, the process of liquefied natural gas can go on constantly.In this specific embodiment, an incoagulable gas separator box 17 (with reference to figure 3) has been advanced in series connection between two groups of dish type heat exchanger tubes of methane cooler 15 and liquefied natural gas subcooler 19.This incoagulable gas separator box 17 is made of with the flash chamber that is positioned at its underpart the incoagulable gas separation chamber that is positioned at its top.The dish type heat exchanger tube UNICOM of this incoagulable gas separation chamber and methane cooler 15, an incoagulable gas delivery pipe 21 is arranged at its top; The dish type heat exchanger tube UNICOM of the bottom of this flash chamber and liquefied natural gas subcooler 19, its top is by the housing UNICOM of a choke valve 16 with methane cooler 15.Pass through choke valve 18 UNICOMs between incoagulable gas separation chamber and the flash chamber.
In this specific embodiment, propane fluid separation applications case 5 and propane cooler 7, Ethylene Liquid separator box 8 and ethylene chiller 10, all with separately separator box last, separately cooler under form be combined as respectively component devices; Dish type heat exchanger tube is wherein made (with reference to figure 2) by low temperature resistant stainless steel tube or copper pipe.
In this specific embodiment, in accordance with the order from top to bottom, described methane fluid separation applications case 13, methane cooler 15, incoagulable gas separator box 17 and liquefied natural gas subcooler 19 are combined as a component devices; Dish type heat exchanger tube is wherein also made (with reference to figure 3) by low temperature resistant stainless steel tube or copper pipe.
Other parts in apparatus of the present invention, all adopt low temperature resistant stainless steel manufacturing as housing, adapter, flange etc.Further, for device of the present invention can move very reliably, in the casing of propane fluid separation applications case 5, Ethylene Liquid separator box 8 and methane fluid separation applications case 13, all be provided with the remaining mist of a chimney-like or the discharge pipe of remaining natural gas.The outer space of this discharge pipe is the separation chamber, and each choke valve (6,9,14) that is connected this propane fluid separation applications case 5, Ethylene Liquid separator box 8 and methane fluid separation applications case 13 bottoms is connected this bottom, separation chamber.Bottom in this discharge pipe have one with they the remaining mist that communicates of the dish type heat exchanger tube upper end of UNICOM or the pooling zone B of remaining natural gas separately.In the bottom of propane cooler 7, ethylene chiller 10 and liquefied natural gas subcooler 19, have respectively that its top communicates with the lower end of dish type heat exchanger tube, its bottommost has a pooling zone A (with reference to figure 2, Fig. 3) who is connected to drain pipe.
As previously mentioned, be transmitted back to the ratio of each component in the mix refrigerant that goes in the compressor, should monitor and adjust and can monitor and adjust with public method fully.In this specific embodiment, then adopted a kind of monitoring and adjustment structure (with reference to figure 2) that is fit to small-scaled natural gas liquification device of the present invention.Its architectural feature is, in propane cooler 7 and ethylene chiller 10, respectively is connected with a liquid level gauge 23 that is filled with painted refrigerator oil in it.Be the liquid sealing pipe UNICOM of being inverted the U font by one section between the bottom liquid of the lower end of each liquid level gauge 23 and each corresponding cooler, the headroom UNICOM of the upper end of each liquid level gauge 23 and corresponding cooler.Near liquid level gauge 23 1 sides the painted refrigerator oil storage tube that has enlarged diameter in a section is arranged at this liquid sealing pipe, the highest point of this liquid sealing pipe generally should be higher than the LPG in each corresponding cooler bottom, the liquid level of liquid ethylene.Under LPG in propane cooler 7 and ethylene chiller 10 bottoms, the liquid ethylene liquid level discharging tube 24 is arranged respectively, a blowdown pipe 22 is respectively arranged on this liquid level, and the media outlet that is cooled in propane cooler 7 and ethylene chiller 10 bottoms respectively has a point for measuring temperature 25.Obviously, described " media outlets that are cooled of propane cooler 7 and ethylene chiller 10 bottoms " are meant the biphase gas and liquid flow that has liquid ethylene to the former, the latter are meant the biphase gas and liquid flow that has liquid methane.
Be example with propane fluid separation applications case 5 with propane cooler 7 below, be combined in the entire work process in this component devices, monitoring principle and adjustment process thereof are described: isolated propane liquid in propane fluid separation applications case 5, after choke valve 6 throttling step-downs, the shell space that enters propane cooler 7 (preferably, spray into by several nozzles of arranging around propane cooler 7, with augmentation of heat transfer), be subjected to natural gas mobile in the dish type heat exchanger tube from top to bottom, the heating of methane and ethylene gas and part evaporation, unevaporated propane liquid then drops to the bottom of shell space, form liquid level, continuation is by the natural gas in the dish type heat exchanger tube, methane and the heating of ethene medium, and continuously explosive evaporation.The propane gas that is evaporated, converge methane and ethylene gas, be heated the back together and flow out from top and return compressor 1 from ethylene chiller 10.The natural gas that is cooled in the coil pipe, methane and ethylene gas, in the decline process, ethene wherein begins to condense into liquid, finally become Ethylene Liquid, natural gas and steam methane mixture, discharge from propane cooler 7 bottoms, enter Ethylene Liquid separator box 8.
Analyze the inside and outside diabatic process of coil pipe in the propane cooler 7, its top is natural gas, ethene and the methane gas diabatic process for propane gas and backflow gas, is called the diabatic process of gas phase and gas phase.At the middle part, rise when ethene begins condensation in the coil pipe, the coil pipe outside mainly remains propane flammable gas and backflow gas (effect of augmentation of heat transfer is only played in the effect of spray), and therefore, the middle part is the diabatic process of condensation and gas phase; In the bottom, when coil pipe enters the propane liquid level when following, just become the diabatic process of condensation and explosive evaporation.Show the size of the heat transfer coefficient of middle part condensation and gas phase, genus hundred figure place grades by calculating to the different heat transfer process; And the heat transfer coefficient of bottom condensation and explosive evaporation, its size belong to thousands digit grade, and both differ an order of magnitude.Therefore, if change the liquid level of propane in propane cooler 7 housings, just can change the evaporation capacity of propane significantly.In other words, control the evaporation capacity that liquid level also just can be controlled propane, also promptly returned the propane reflux amount of compressor 1.
The method of propane liquid level is very simple and easy in the control housing, and the aperture that only needs to change choke valve 6 just can reach.Open when big when choke valve 6, liquid level will rise; Otherwise, choke valve 6 descends when closing hour liquid level.This operating process, required choke valve 6 and liquid level gauge 23 all are placed on the panel of incubator (also the claiming ice chest) casing in the actual device.It must be noted that, the propane liquid in liquid level gauge 23 tube connectors after long-term the stop, all can flash to gas, can not reflect actual liquid level.Therefore, must fill other in the liquid level gauge 23 can evaporated liquid, and this specific embodiment is painted refrigerator oil, and the liquid level of propane is to change by the propane flammable gas pressure in the inverted U font liquid sealing pipe to transmit.
When regulating the aperture of choke valve 6, must be noted that following 2 points:
(1) aperture of choke valve 6 can not be excessive, otherwise the propane liquid level in the propane fluid separation applications case 5 will be lower than the mouth of pipe of propane fairlead, make methane, natural gas and ethylene gas enter propane cooler 7 housings in a large number, and be back to compressor 1 inlet, cause the invalid circulation of above-mentioned gas, reduce natural gas liquefaction output greatly.For this reason, propane fluid separation applications case 5 has also been installed liquid level gauge, to prevent propane liquid level low excessively (Ethylene Liquid separator box 8 is as the same).
(2) though open the cooling effect that big choke valve 6 can improve natural gas in the coil pipe, ethene and methane, help the liquefaction of natural gas.But choke valve 6 apertures are excessive, must increase the evaporation capacity of propane, tie up the share of other cold-producing mediums, cause out of proportion.Therefore, the aperture of choke valve 6 should keep suitable Qi Biao Chi of position that the Ethylene Liquid of propane cooler 7 and the outlet temperature of natural gas (being the described biphase gas and liquid flow that has liquid ethylene) are remained in-38 ℃～-36 ℃, must not be lower than-38 ℃ [among Fig. 2, measuring the bottom of the point for measuring temperature 25 of outlet temperature] at these propane cooler 7 housings (low head).
Propane liquid level in the said temperature scope, in the cooler casing is the control liquid level.But this liquid level can constantly raise in running, and this is because the reason that contains the propane component in the raw natural gas, constantly liquefies in the liquefaction cycle process, also here constantly gathers.For this reason, the throttle valve opening that should regulate on the discharging tube 24 carries out continuous blow-down, to keep the substantially constant of propane liquid level.In general, the frequency of revising operation is very little.In case of necessity, discharge process can be implemented by Liquid level adjusting valve.
Profit uses the same method, and can regulate the evaporation capacity of Ethylene Liquid in the ethylene chiller.Be noted that, because the content of ethene is extremely low in the raw natural gas, in gas deliquescence process, have small amount of ethylene and be dissolved in the liquefied natural gas and constantly be pulled away, so in the ordinary course of things, here to be operating as the master from blowdown pipe 22 inside tonifying Qi.
For the control of methane liquid level in methane cooler 15 housings, its method is identical with two coolers.Its difference is for no other reason than that the main component in the raw natural gas is a methane, the operation of fluid infusion and discharge opeing recedes into the background, so can not establish liquid level gauge, only need to regulate the throttle valve opening on methane fluid separation applications case 13 backs, the methane liquid fairlead, the outlet temperature of control methane cooler 15 bottom methane liquid, that it is remained between-120 ℃～-119 ℃ is just passable.
Because the housing liquid level in the whole liquefaction flow path between three coolers (being propane cooler 7, ethylene chiller 10 and methane cooler 15) is to be mutually related, the liquid level of regulating any one cooler all can cause the variation of the middle liquid level of other coolers, therefore, the adjustment of each throttle valve opening need be carried out just finishing for 2～3 times repeatedly.
Below, the separation and the emissions operation of incoagulable gas is further described.
So-called incoagulable gas is meant the N that contains in the raw natural gas
2, O
2And the gases such as He, Ar of trace, their condensing temperature is all much lower than the condensing temperature of natural gas itself.Therefore, in gas deliquescence process, they are present in the circulatory system with the form of gas, if not with its discharge system, then this class gas constantly accumulates in system, ties up the capacity share of compressor 1, makes the decline of exerting oneself of liquefying plant.What is more, the existence of incoagulable gas, and the diabatic process of each heat exchanger in the liquefying plant that deteriorates significantly, thereby further reduced exerting oneself of liquefying plant.This situation occurred in many homemade liquefying plants.Several liquefying plants do not reach exerts oneself, and this may be an one of the main reasons.
In this liquefying plant, methane cooler 15 bottoms, natural gas (wherein main component is a methane) that are positioned at 1.25Mpa～1.3Mpa major part obtain liquefaction, the temperature of liquid is between-120 ℃～-119 ℃, and the steam methane partial pressure on the liquid level should also be between 1.25Mpa～1.3Mpa.But the incoagulable gas accumulation is here constantly arranged, and the partial pressure of supposing these gases is P, and this partial pressure P value raises, makes gross pressure to surpass 1.25Mpa～1.3Mpa along with the continuous accumulation of these gases, and in continuous rising.If these incoagulable gas in the supposition raw natural gas (mainly are N
2) content about 5%, in order to get rid of this part gas, must drain useful natural gas together simultaneously.According to calculating, if the discharge capacity of control natural gas useful component total liquefied natural gas amount 1% in, should control pressure in the exhaust chamber between 1.5Mpa～1.6Mpa; This can regulate the preceding choke valve 12 of methane fluid separation applications case and the choke valve 211 on the incoagulable gas delivery pipe reaches.At this moment, capacity is about about 6% of the total air inflow of unstripped gas, wherein 1% is active ingredient.
Realize that the item that above measure should be noted is: no matter exhaust chamber pressure has surpassed 1.25Mpa～1.3Mpa and reached 1.5Mpa～1.6Mpa, but the temperature of exhaust chamber bottom liquid must remain in-120 ℃～-119 ℃, can not raise because of the rising of pressure.In order to reach this purpose, can to regulate methane fluid separation applications case 13 bottom choke valves 14 and reach.
Pressure in apparatus of the present invention in each casing (tank body) is measured (with reference to figure 3 by the pressure gauge that is arranged on each corresponding pressure tap 26 place, all the other pressure taps do not omit and draw), the thermometer measure (with reference to figure 2,3, all the other points for measuring temperature do not omit and draw) that temperature in each casing (tank body) is located by being arranged on each corresponding point for measuring temperature (25,27).
Claims (9)
1, a kind of method of natural gas liquefaction has adopted compressor and cold-producing medium in the method, it is characterized in that, described compressor only need have been used one, and described cold-producing medium is the circulating refrigerant that is formed by propane, ethene and methane blended; The weight mixing ratio of propane, ethene and methane is 1.76: 1.27: 1.0;
The process of described natural gas liquefaction comprises:
A, the raw natural gas that will remove impurity and circulating refrigerant suck the step in this compressor, to compress together;
B, the HTHP mist from the output of this compressor is cooled off, the heavy hydrocarbon component that will bring from raw natural gas then, be condensed into liquid through cooling separates and gets rid of the step of this heavy hydrocarbon component from this mist;
C, the mist of having removed the heavy hydrocarbon component is further cooled off, with the step of the biphase gas and liquid flow that obtains having LPG;
D, LPG is separated from the biphase gas and liquid flow at its place, then this LPG is carried out the throttling step-down, allows its required amount evaporation of returning propane flammable gas according to keeping mixing ratio, and borrow its evaporation endothermic process to come the mist of remainder is further cooled off, to obtain having the biphase gas and liquid flow of liquid ethylene, then the propane flammable gas after the heat absorption is transmitted back to the step of going in the compressor;
E, liquid ethylene is separated from the biphase gas and liquid flow at its place, then this liquid ethylene is carried out the throttling step-down, allows the ethene tolerance evaporation that it need return according to keeping mixing ratio, and borrow its evaporation endothermic process to come the mist of remainder is further cooled off, to obtain having the biphase gas and liquid flow of liquid methane, then the ethylene gas after the heat absorption is transmitted back to the step of going in the compressor;
F, the biphase gas and liquid flow that has liquid methane is carried out the throttling step-down, and allow methane liquid partly evaporate; Then liquid methane is separated, as cooling medium, be allowed to condition at further cooled natural gas in the subsequent process, make it liquefaction after the throttling step-down, then further make the cold excessively step of liquefied natural gas;
G, last is a step of overcooled liquified natural gas being injected the liquid natural gas holding vessel.
2, according to the method for the described natural gas liquefaction of claim 1, it is characterized in that, in step f, natural gas carried out before the supercooling to also have a step of from the natural gas that is cooled to liquid, separating and get rid of incoagulable gas.
According to the method for claim 1 or 2 described natural gas liquefactions, it is characterized in that 3, in step a, its compressor delivery pressure is 3.0Mpa～4.0Mpa, outlet temperature is 120 ℃～140 ℃; In step b, the temperature after mist is cooled is 79 ℃～81 ℃; In step c, the temperature after mist is cooled is 30 ℃～35 ℃; In steps d, the pressure after its LPG throttling step-down is 0.102Mpa～0.105Mpa, and the temperature of having evaporated and not evaporated the biphase gas and liquid flow of propane is-42 ℃～-40 ℃; The resulting temperature that has the biphase gas and liquid flow of liquid ethylene in back that is cooled is-38 ℃～-36 ℃; In step e, pressure after its liquid ethylene throttling step-down is 0.102Mpa～0.105Mpa, the temperature of having evaporated and not evaporated the biphase gas and liquid flow of ethene is-103 ℃～-102 ℃, and the resulting temperature that has the biphase gas and liquid flow of liquid methane in cooling back is-98 ℃～-97 ℃; In step f, the force value that the biphase gas and liquid flow that has liquid methane is carried out after the throttling step-down is 1.25Mpa～1.6Mpa, and part methane liquid evaporation back temperature is-119 ℃; Afterwards as cooling medium, the pressure after its step-down is 0.102Mpa～0.105Mpa to liquid methane by the throttling step-down after separating, and its temperature is-163 ℃～-162 ℃.
According to the method for the described natural gas liquefaction of claim 2, it is characterized in that 4, the pressure that separates and get rid of incoagulable gas is 1.5Mpa～1.6Mpa, temperature is-120 ℃～-119 ℃; After getting rid of incoagulable gas, liquified natural gas is further throttling step-down again, and pressure is reduced to 0.5Mpa; Then, further again mistake is as cold as-158 ℃.
5, a kind of device of natural gas liquefaction, in this device compressor is arranged, it is characterized in that described compressor (1) only has one, what compress by this compressor (1) is to have removed the raw natural gas of impurity and the circulating refrigerant that is formed by propane, ethene, methane blended; Wherein, the weight mixing ratio of propane, ethene and methane is 1.76: 1.27: 1.0,
The equipment that connects successively afterwards at this compressor (1) comprises:
Cooling is from first aftercooler (2) of the HTHP mist of compressor (1) output;
The heavy hydrocarbon component that brings from raw natural gas, be condensed into liquid through cooling separated from this mist and this heavy hydrocarbon component get rid of from its bottom, the heavy hydrocarbon separator box (3) of this mist from its top output;
The mist of having removed the heavy hydrocarbon component is cooled off, with second aftercooler (4) of the biphase gas and liquid flow that obtains having LPG;
The propane fluid separation applications case (5) of the gravity type that LPG is separated from the biphase gas and liquid flow at its place; Isolated LPG is from the bottom output of this propane fluid separation applications case (5), and remaining mist is from the top output of this propane fluid separation applications case (5);
One allows the remaining mist that has separated propane enter further cooling in the dish type heat exchanger tube that is provided with in its shell space on its housing top, to obtain having the biphase gas and liquid flow of liquid ethylene, after allowing LPG by a choke valve (6) the throttling step-down that bottom propane fluid separation applications case (5), communicates simultaneously, entering the amount that need return propane flammable gas in its shell space according to keeping mixing ratio at its housing middle part by several nozzles evaporates, and the propane flammable gas that evaporation is obtained be transmitted back to go in the compressor (1) before, cool off earlier the propane cooler (7) of the mist in this dish type heat exchanger tube as cold-producing medium;
The Ethylene Liquid separator box (8) of the gravity type that liquid ethylene is separated from the biphase gas and liquid flow at its place; Isolate the bottom output of liquid ethylene from this Ethylene Liquid separator box (8), remaining mist is from the top output of this Ethylene Liquid separator box (8);
One allows the remaining mist that has separated ethene enter further cooling in the dish type heat exchanger tube that is provided with in its shell space on its housing top, to obtain having the biphase gas and liquid flow of liquid methane, after allowing liquid ethylene by a choke valve (9) the throttling step-down that bottom Ethylene Liquid separator box (8), communicates simultaneously, entering the amount that need return ethylene gas in its shell space according to keeping mixing ratio at its housing middle part by several nozzles evaporates, and ethylene gas that evaporation is obtained be transmitted back to through propane cooler (7) go in the compressor (1) before, cool off the ethylene chiller (10) of the mist in this dish type heat exchanger tube earlier as cold-producing medium;
The biphase gas and liquid flow that has separated ethene and had a liquid methane imported in the dish type heat exchanger tube that is provided with in its shell space a return-air cooler (11) of further cooling and liquefaction;
The methane fluid separation applications case (13) of a gravity type that is connected with this return-air cooler (11) by a choke valve (12), liquid methane is separated from the biphase gas and liquid flow at its place; Isolate the bottom output of liquid methane from this methane fluid separation applications case (13), remaining natural gas is from the top output of this methane fluid separation applications case (13);
The remaining natural gas that handle has separated liquid methane enters further cooling in the dish type heat exchanger tube that is provided with in its shell space on its housing top, allow simultaneously isolated liquid methane by with a choke valve (14) throttling step-down that methane fluid separation applications case (13) bottom communicates after, in its lower housing portion enters its shell space according to keeping the required methane tolerance evaporation of mixing ratio, and the methane gas that evaporation obtains cooled off as cold-producing medium and this dish type heat exchanger tube that liquefies in the methane cooler (15) of natural gas;
The upper end of an interior dish type heat exchanger tube that is provided with of its shell space and the dish type heat exchanger tube lower end UNICOM in methane cooler (15) shell space, its dish type heat exchanger tube lower end is by the liquefied natural gas subcooler (19) of a control valve (201) with a liquid natural gas holding vessel (20) UNICOM; Between this liquid natural gas holding vessel (20) and liquefied natural gas subcooler (19) housing, be connected to the return-air valve (191) of a steady pressure;
And the choke valve (14) and methane cooler (15) housing of methane fluid separation applications case (13) bottom UNICOM between, be connected with a branched pipe; The housing UNICOM of the other end of this branched pipe and liquefied natural gas subcooler (19) to allow by the methane after this choke valve (14) throttling step-down, does further supercooling to the natural gas in the interior dish type heat exchanger tube of this liquefied natural gas subcooler (19) simultaneously; Between the housing bottom between the housing middle part of the case top of this liquefied natural gas subcooler (19) and methane cooler (15), at the case top of this methane cooler (15) and return-air cooler (11), between in the middle part of the housing of the case top of this return-air cooler (11) and ethylene chiller (10), respectively be connected with a muffler.
According to the device of the described natural gas liquefaction of claim 5, it is characterized in that 6, an incoagulable gas separator box (17) has been advanced in series connection between two groups of dish type heat exchanger tubes of described methane cooler (15) and liquefied natural gas subcooler (19); This incoagulable gas separator box (17) is made of with the flash chamber that is positioned at its underpart the incoagulable gas separation chamber that is positioned at its top; The dish type heat exchanger tube UNICOM of this incoagulable gas separation chamber and methane cooler (15), an incoagulable gas delivery pipe (21) is arranged at its top; The dish type heat exchanger tube UNICOM of the bottom of this flash chamber and liquefied natural gas subcooler (19), its top is by the housing UNICOM of a choke valve (16) with methane cooler (15); Pass through a choke valve (18) UNICOM between incoagulable gas separation chamber and the flash chamber.
7, according to the device of claim 5 or 6 described natural gas liquefactions, it is characterized in that,, respectively be connected with a liquid level gauge (23) that is filled with painted refrigerator oil in it in described propane cooler (7) and ethylene chiller (10); Be the liquid sealing pipe UNICOM of being inverted the U font, the upper end of each liquid level gauge (23) and the headroom UNICOM of corresponding cooler by one section between the bottom liquid of the lower end of each liquid level gauge (23) and each corresponding cooler; Near liquid level gauge (23) one sides the painted refrigerator oil storage tube that has enlarged diameter in a section is arranged at this liquid sealing pipe; Under LPG in propane cooler (7) and ethylene chiller (10) bottom, the liquid ethylene liquid level discharging tube 24 is arranged respectively, a blowdown pipe 22 is respectively arranged on this liquid level, and the media outlet that is cooled in propane cooler (7) and ethylene chiller (10) bottom respectively has a point for measuring temperature (25).
8, according to the device of claim 5 or 6 described natural gas liquefactions, it is characterized in that, described propane fluid separation applications case (5) and propane cooler (7), Ethylene Liquid separator box (8) and ethylene chiller (10), all with separately separator box last, separately cooler under form be combined as respectively component devices; Dish type heat exchanger tube is wherein made by low temperature resistant stainless steel tube or copper pipe.
9, according to the described natural gas liquefaction device of claim 6, it is characterized in that, in accordance with the order from top to bottom, described methane fluid separation applications case (13), methane cooler (15), incoagulable gas separator box (17) and liquefied natural gas subcooler (19) are combined as a component devices; Dish type heat exchanger tube is wherein made by low temperature resistant stainless steel tube or copper pipe.
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| CNB2007100784413A CN100565060C (en) | 2007-04-28 | 2007-04-28 | A kind of method of natural gas liquefaction and device thereof |
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| CN101608860B (en) * | 2008-06-17 | 2011-08-17 | 北京安瑞科新能能源科技有限公司 | Gas liquefying process for mixed refrigerant and mixed refrigerant |
| EP2561294B1 (en) * | 2010-03-31 | 2019-07-24 | Linde Aktiengesellschaft | Rebalancing a main heat exchanger in a process for liquefying a tube side stream |
| CN101922850B (en) * | 2010-09-15 | 2012-01-04 | 煤炭科学研究总院重庆研究院 | Method for utilizing coalbed methane containing oxygen to prepare liquefied natural gas |
| CN101929788B (en) * | 2010-09-15 | 2012-01-04 | 中国科学院理化技术研究所 | Device for preparing liquefied natural gas by oxygen-bearing coal mine methane |
| FR3016436B1 (en) * | 2014-01-10 | 2019-05-10 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | METHOD AND APPARATUS FOR LIQUEFACTING A GASEOUS CO2 CURRENT |
| CN104449923B (en) * | 2014-10-21 | 2016-06-08 | 中国海洋石油总公司 | A kind of method reducing LNG evaporation capacity |
| CN105647606B (en) * | 2016-03-31 | 2019-06-18 | 大庆市中瑞燃气有限公司 | A kind of natural gas gasifying stabilizer |
| CN107556969B (en) * | 2016-06-30 | 2020-09-08 | 中石化洛阳工程有限公司 | Working medium for liquefied natural gas cold energy organic Rankine cycle power generation |
| JP6741565B2 (en) * | 2016-12-08 | 2020-08-19 | 川崎重工業株式会社 | Raw material gas liquefier and control method thereof |
| CN111718769A (en) * | 2020-06-29 | 2020-09-29 | 山西晋煤天源化工有限公司 | Comprehensive utilization synthetic ammonia tail gas preparation PNG system |
| US11499775B2 (en) * | 2020-06-30 | 2022-11-15 | Air Products And Chemicals, Inc. | Liquefaction system |
| CN112304026B (en) * | 2020-11-03 | 2022-06-24 | 江苏科技大学 | Crude oil volatile gas grading liquefaction system and working method thereof |
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