CN202924980U - Natural gas liquefaction and heavy hydrocarbon treatment device - Google Patents
Natural gas liquefaction and heavy hydrocarbon treatment device Download PDFInfo
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- CN202924980U CN202924980U CN2012206882327U CN201220688232U CN202924980U CN 202924980 U CN202924980 U CN 202924980U CN 2012206882327 U CN2012206882327 U CN 2012206882327U CN 201220688232 U CN201220688232 U CN 201220688232U CN 202924980 U CN202924980 U CN 202924980U
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 200
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 200
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 189
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 180
- 239000003345 natural gas Substances 0.000 title claims abstract description 88
- 239000007788 liquid Substances 0.000 claims abstract description 68
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 65
- 239000007791 liquid phase Substances 0.000 claims abstract description 58
- 238000005406 washing Methods 0.000 claims abstract description 48
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 33
- 230000006835 compression Effects 0.000 claims abstract description 32
- 238000007906 compression Methods 0.000 claims abstract description 32
- 239000012071 phase Substances 0.000 claims abstract description 32
- 239000003915 liquefied petroleum gas Substances 0.000 claims abstract description 23
- 239000003507 refrigerant Substances 0.000 claims abstract description 13
- 239000007789 gas Substances 0.000 claims description 77
- 235000009508 confectionery Nutrition 0.000 claims description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 30
- 239000007792 gaseous phase Substances 0.000 claims description 21
- 239000002994 raw material Substances 0.000 claims description 9
- 239000000284 extract Substances 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 35
- 239000003949 liquefied natural gas Substances 0.000 abstract 2
- 238000009825 accumulation Methods 0.000 abstract 1
- 239000012530 fluid Substances 0.000 abstract 1
- 238000005057 refrigeration Methods 0.000 abstract 1
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 24
- 239000000470 constituent Substances 0.000 description 13
- 239000000047 product Substances 0.000 description 13
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 9
- 238000001816 cooling Methods 0.000 description 8
- 239000000203 mixture Substances 0.000 description 8
- 238000000926 separation method Methods 0.000 description 8
- 239000006227 byproduct Substances 0.000 description 5
- 238000000746 purification Methods 0.000 description 5
- 210000000689 upper leg Anatomy 0.000 description 5
- 239000012808 vapor phase Substances 0.000 description 5
- 230000000903 blocking effect Effects 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 238000007710 freezing Methods 0.000 description 4
- 230000008014 freezing Effects 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 230000002411 adverse Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 241000521257 Hydrops Species 0.000 description 1
- 206010030113 Oedema Diseases 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- -1 benzene Chemical class 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 150000002829 nitrogen Chemical class 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 239000002594 sorbent 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
- F25J1/02—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
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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
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
- F25J1/0238—Purification or treatment step is integrated within one refrigeration cycle only, i.e. the same or single refrigeration cycle provides feed gas cooling (if present) and overhead gas cooling
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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
- F25J1/0243—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
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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
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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
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
Abstract
The utility model relates to a natural gas liquefaction and heavy hydrocarbon treatment device which comprises a low-temperature liquefaction device and a heavy hydrocarbon treatment device, wherein the low-temperature liquefaction device comprises a cold box, a refrigerant separator, a heavy hydrocarbon separator, a heavy hydrocarbon booster pump, a nitrogen flash tank, a refrigerant compression system and four throttling devices, wherein the heavy hydrocarbon treatment device comprises a heavy hydrocarbon washing tower, a deethanizer, a rectifying tower and two throttling devices. The device provided by the utility model produces LNG (liquefied natural gas) as well as LPG (liquefied petroleum gas) and light oil, the process route is advanced, and the device is economical and reliable; with relatively high operation flexibility, the device can adapt to relatively large range of heavy hydrocarbon content of natural gas; cold is provided by a circulation process of mixed refrigerant, gas-phase and liquid-phase refrigerants enter the cold box respectively for heat exchange so that the heat exchange curves of the cold and hot fluids are matched better; and the refrigeration process can effectively avoid liquid accumulation at the bottom of the cold box.
Description
Technical field
The utility model provides a kind of brand-new natural gas liquefaction and heavy hydrocarbon treatment unit, be specifically related to a kind ofly from the Sweet natural gas that is rich in heavy hydrocarbon, remove heavy hydrocarbon, when liquefaction obtains natural gas liquids (LNG), but the device of by-product liquefied petroleum gas (LPG) and light oil products also.
Background technology
Sweet natural gas promotes at social every field proportion just gradually as primary energy source, and its Application Areas expands the aspects such as generating, automobile use gas, industrial gas, city resident's use gas gradually to, and market demand increases sharply.But limited by material condition and user distribution, there is quite a few resource can't adopt the defeated method of supplying of traditional natural gas tube to carry out the pipe long-distance conveying, and more convenient rational method is the mode that adopts liquefaction, changes methane into liquid and adopt again mode of transport flexibly that it is sent to user terminal.Natural gas liquids (LNG) volume only has with 1/625 of amount gas volume, can reduce after liquefaction and store and transportation cost, and can improve the combustion value of unit volume.
In the process of natural gas liquefaction, heavy hydrocarbon is C6 especially
+hydrocarbon always first is condensed, and as heavy hydrocarbon first not separated, thereby heavy hydrocarbon may freeze to stop up ice chest, therefore requires to enter heavy hydrocarbons content in the Sweet natural gas of ice chest and is down to enough low.At present, in prior art, adopt removes the heavy hydrocarbon in Sweet natural gas with sorbent materials such as water-fast silica gel, gacs more, but can significantly increase facility investment when heavy hydrocarbons content is higher; Adopt obtaining of this kind of technology resurgent gases also more difficult, and need to consider the whereabouts of resurgent gases.Accompanying drawing 1 is depicted as another kind of existing Technology, and the device of its use comprises two-section type mixing medium compressor, water cooler, gas-liquid separator, throttling set, one group of plate-fin heat exchanger group and a LNG storage tank.At first raw natural gas after purification enters the plate-fin heat exchanger group and carries out precooling, enter the heavy hydrocarbon separator after being cooled to-30 ℃～-60 ℃ and carry out gas-liquid separation, continued to enter all the other interchanger at different levels of heat exchanger package by the isolated vapor phase stream thigh in heavy hydrocarbon separator top, and be cooled to therein-130 ℃～-166 ℃, the natural gas liquids obtained is sent in natural gas liquids (LNG) storage tank and is stored, heavy hydrocarbon separator bottom cutting out partial heavy hydrocarbon; But this method is not good to the removal effect of the aromatic hydrocarbon such as benzene, with aromatic hydrocarbon content, increase, removal effect is poorer, as unstripped gas contains a large amount of aromatic hydrocarbon (fusing point of benzene only has 5.51 degree), will cause Cold box blocking and freezing; And the heavies removal effect of this technique also is difficult to control.For this situation, the utility model proposes a kind of method of new natural gas liquefaction and de-heavy hydrocarbon, when also obtaining natural gas liquids (LNG), but also by-product liquefied petroleum gas (LPG) (LPG) and light oil.
The utility model content
The utility model provides a kind of natural gas liquefaction and heavy hydrocarbon treatment unit, and this device comprises: low-temperature liquefaction device and heavy hydrocarbon treatment unit;
The low-temperature liquefaction device comprises an ice chest, a cryogen separator, a heavy hydrocarbon separator, a heavy hydrocarbon topping-up pump, a nitrogen flash tank, a refrigerant compression systems and four throttling sets; The heavy hydrocarbon treatment unit comprises a heavy hydrocarbon washing tower, a deethanizing column, a rectifying tower and two throttling sets;
Wherein, the liquor pump that the First water cooler that this refrigerant compression systems comprises a two-section type azeotrope compressor, be connected with second segment with the first paragraph of described azeotrope compressor respectively and second water cooler, the First gas-liquid separator that is connected with second water cooler with described First water cooler respectively and second gas-liquid separator are connected with First with in the middle of described two gas-liquid separators, the exit end of this liquor pump is connected to the inlet end of second water cooler via pipeline;
Wherein, the gas phase end of the First gas-liquid separator in two gas-liquid separators of refrigerant compression systems is connected with the second compression section of azeotrope compressor, the liquid phase end of First gas-liquid separator is connected to second water cooler in described two water coolers after converging via the outlet conduit of liquor pump and the second compression section, and with two heat exchanger channels of described ice chest, an end of the first heat exchanger channels and an end of the second heat exchanger channels are connected respectively via two pipelines for the gas phase end of second gas-liquid separator and liquid phase end;
Described nitrogen flash tank comprises entrance, gaseous phase outlet, liquid-phase outlet;
Described cryogen separator comprises inlet end, top gas phase end and, the bottom liquid phases end;
This heavy hydrocarbon separator comprises a gas inlet passage, a heavy hydrocarbon exit passageway, a gas exit passageway; This heavy hydrocarbon washing tower comprises a natural gas _ raw material gas access road, a gas exit passageway, a heavy hydrocarbon access road, the heavy hydrocarbon exit passageway be connected with inlet end with the 5th throttling set; This deethanizing column comprises a heavy hydrocarbon access road, the liquid-phase outlet passage that gaseous phase outlet passage is connected with inlet end with the 6th throttling set; This rectifying tower comprises a liquid phase access road, a gaseous phase outlet passage and a light oil exit passageway;
This ice chest comprises at least seven heat exchanger channels, at least comprises the first, second, third, fourth, the 5th, the 6th and the 7th heat exchanger channels;
The other end of the first heat exchanger channels of described ice chest is connected with an end of the 3rd heat exchanger channels via the first throttle device, and the other end of the 3rd heat exchanger channels is connected with the inlet end of cryogen separator;
The other end of the second heat exchanger channels also is connected with cryogen separator inlet end via the second throttling set;
One end of the 4th heat exchanger channels is connected with the gas inlet passage of described heavy hydrocarbon separator, and the other end of the 4th heat exchanger channels is connected with the top gas exit passageway of heavy hydrocarbon washing tower;
One end of the 5th heat exchanger channels is connected with the top gas phase end of heavy hydrocarbon separator, and the other end is connected to LNG tank after via the 4th throttling set;
After the gaseous phase outlet passage of deethanizing column optionally converges with evaporated natural gas (being BOG) passage from LNG tank, be connected to an end of the 6th heat exchanger channels of ice chest, the other end of the 6th heat exchanger channels is connected in the entrance (or inlet end) of nitrogen flash tank via the 3rd throttling set, nitrogen flash tank liquid-phase outlet also is connected to LNG tank by pipeline;
The top gas phase end of described cryogen separator and bottom liquid phases end converge an end of rear connection the 7th heat exchanger channels, and the other end of the 7th heat exchanger channels is connected with the first compression section of azeotrope compressor;
The heavy hydrocarbon exit passageway of described heavy hydrocarbon separator is connected to the input terminus of heavy hydrocarbon topping-up pump; Heavy hydrocarbon supercharging delivery side of pump connects the heavy hydrocarbon access road of heavy hydrocarbon washing tower;
The natural gas _ raw material gas access road of described heavy hydrocarbon washing tower is connected to the pipeline of carrying purified natural gas (being natural gas _ raw material gas), and the heavy hydrocarbon exit passageway of heavy hydrocarbon washing tower connects the heavy hydrocarbon access road of deethanizing column via the 5th throttling set;
The liquid-phase outlet of described deethanizing column is connected in the liquid phase access road of rectifying tower via the 6th throttling set;
After connecting the light oil water cooler, the light oil exit passageway that the gaseous phase outlet passage of described rectifying tower is connected to liquefied petroleum gas product storage tank and this tower via an aftercooler is connected to the light oil products storage tank.
In one embodiment, the top gas phase end of heavy hydrocarbon separator successively by after the 5th heat exchanger channels of ice chest further other the 8th heat exchanger channels by ice chest be connected to the 4th throttling set, then be connected to LNG tank.
In another embodiment, the gaseous phase outlet passage of described rectifying tower is at first via described aftercooler with optionally via a rectifying tower return tank, then separate two arms, an arm is connected with the liquefied petroleum gas product storage tank, and another arm, optionally via a pump, be connected in the liquid phase access road of rectifying tower after converging with the liquid-phase outlet after the 6th throttling set of deethanizing column.
Can adopt the reboiler of any pattern at the bottom of the tower of described deethanizing column and/or described rectifying tower, for example built-in, autoclave, thermosyphon reboiler.
In a preferred implementation, in the temperature range of-30 ℃～-80 ℃ of the 4th heat exchanger channels of described ice chest, at least one (preferably a plurality of, for example 2 ~ 10) Sweet natural gas precooling is set and extracts out mouthful.
In a preferred implementation, the gaseous phase outlet passage of described deethanizing column with from evaporated natural gas (the being BOG) output channel of LNG tank, converge after, be connected to an end of the 6th heat exchanger channels of ice chest.
" first paragraph compression " described here or " one section compression " are used interchangeably with " the first compression section ", by that analogy.
Use the technique of device of the present utility model to comprise low-temperature liquefaction operation and heavy hydrocarbon treatment process two portions;
The low-temperature liquefaction operation be included in the heavy hydrocarbon washing tower in the heavy hydrocarbon treatment process Sweet natural gas after the de-heavy hydrocarbon of part in ice chest, realize cooling, in the heavy hydrocarbon separator fully de-heavy hydrocarbon and liquefying in ice chest, the heavy hydrocarbon treatment process comprises that the Sweet natural gas after purification sloughs the part heavy hydrocarbon in the heavy hydrocarbon washing tower, the Sweet natural gas of the de-heavy hydrocarbon of part goes the low-temperature liquefaction operation from scrubber overhead, enter successively in deethanizing column and carry out stripping and isolate light constituent (being mainly C1 with heavy hydrocarbon at the bottom of the washing tower that is removed out, C2 hydrocarbon etc.) and heavy constituent, wherein light constituent is transported in ice chest and carries out that cooling (light constituent flows through the nitrogen flash tank after cooling, bottom at the nitrogen flash tank obtains natural gas liquids), wherein heavy constituent enters in rectifying tower and isolates light oil (byproduct) and isolate gas phase, this gas phase is cooled into liquefied petroleum gas (LPG) (LPG).
In addition, the technique of using appts can adapt to the situation that contains the aromatic hydrocarbon such as benzene in unstripped gas, and the aromatic hydrocarbon such as benzene are removed with heavy hydrocarbon component, prevents Cold box blocking and freezing.
Preferably, above-mentioned technique comprises following operation:
The low-temperature liquefaction operation:
In described low-temperature liquefaction device or low-temperature liquefaction operation, from the Sweet natural gas in the heavy hydrocarbon washing tower of heavy hydrocarbon treatment process, whole C5 in the heavy hydrocarbon washing tower, have been removed
+and part C3, the Sweet natural gas of C4 heavy hydrocarbon component, at first the 4th heat exchanger channels that enters ice chest carries out precooling, be cooled to-30 ℃～-80 ℃ (preferably-35 ℃～-75 ℃, more preferably-40 ℃～-70 ℃, more preferably-45 ℃～-65 ℃) after enter the heavy hydrocarbon separator and carry out gas-liquid separation, isolate remaining C3 Sweet natural gas from heavy hydrocarbon separator bottom, the components such as C4 heavy hydrocarbon, continue to enter all the other heat exchanger channels (for example the 5th heat exchanger channels) of ice chest from the isolated vapor phase stream thigh in heavy hydrocarbon separator top, and be cooled to therein-130 ℃～-166 ℃ and (be preferably-135 ℃～-160 ℃, more preferably-140 ℃～-155 ℃, more preferably-145 ℃～-152 ℃), obtain natural gas liquids (LNG) after the 4th throttling set throttling, heavy hydrocarbon separator bottom liquid phases goes to carry out heat and mass with raw natural gas in the heavy hydrocarbon washing tower of described heavy hydrocarbon treatment process,
The heavy hydrocarbon treatment process:
In described heavy hydrocarbon treatment process, be rich in Sweet natural gas after the purification of heavy hydrocarbon (for example, through depickling as CO
2deng the Sweet natural gas after, demercuration, dehydration) enter heavy hydrocarbon wash tower bottoms gas inlet as unstripped gas, with top-down liquid phase counter current contact in the heavy hydrocarbon washing tower, fully after heat and mass, remove the whole C5 in Sweet natural gas
+and the heavy hydrocarbon components such as part C3, C4; C3, the C4 heavy hydrocarbon component of heavy hydrocarbon washing tower tower top liquid phase source for separating through heavy hydrocarbon separator bottom in described low-temperature liquefaction operation.Gas phase in the heavy hydrocarbon washing tower is gone described low-temperature liquefaction operation from tower top; Heavy hydrocarbon wash tower bottoms liquid phase is decompressed to 2.5MPaA～4.0MPaA(through the 5th throttling set and is preferably 2.8 ~ 3.7MPaA, 3.0 ~ 3.5MPaA more preferably), then enter deethanizing column, conduct heat with the gas phase adverse current contact mass transfer that tower bottom reboiler produces, remove light constituent (being mainly C1, C2 hydrocarbon etc.) wherein; Light constituent enters that the 6th heat exchanger channels of ice chest is cooling, liquefaction, through the 3rd throttling set throttling and enter flash distillation in the nitrogen flash tank, will be from the BOG(boil-off gas of LNG tank) in the nitrogen (being the nitrogen that unstripped gas liquefaction may be carried while for LNG, entering LNG tank) that may exist from the nitrogen flash tank, separate, nitrogen flash tank bottom obtains the preferred 0.8mol% of a nitrogen content<1mol%(in LNG, further preferred 0.6mol%); Liquid phase at the bottom of the deethanizing column tower (is mainly C3, C4, C5, C6
+the mixture of paraffinic hydrocarbons) be decompressed to 0.5MPaA～2.0MPaA(through the 6th throttling set and be preferably 0.7 ~ 1.8MPaA, 1.0 ~ 1.5MPaA more preferably) enter the rectifying tower middle part after, obtain the mixture (for gas phase) of the components such as C3, C4 paraffinic hydrocarbons from tower top through rectifying, partial reflux (converging with the inlet duct of rectifying tower), the part extraction, be liquefied petroleum gas (LPG) (LPG) product, at the bottom of tower, separate and obtain C5, C6
+etc. the mixture of component, after the light oil water cooler is cooled to normal temperature, be light oil products.
Preferably, the low-temperature liquefaction of Sweet natural gas completes in the ice chest of low-temperature liquefaction device, and the cold of ice chest is provided by the azeotrope circulation:
By C1～C5 and N
2the azeotrope formed (is selected from C1, C2, C3, C4 and C5 paraffinic hydrocarbons and N usually
2in four kinds, five kinds or six kinds, they mix according to the arbitrary volume ratio or according to the volume ratio that approximately is equal to) enter the entrance of azeotrope compressor, be compressed to 0.6～1.8MPaA through first paragraph, enter first step water cooler and be cooled to 30 ℃～45 ℃, enter again first step gas-liquid separator and carry out gas-liquid separation, the isolated gas in first step gas-liquid separator top continues to enter the second segment entrance of compressor, be compressed to 1.2～5.4MPaA through two sections, after the isolated liquid of first step gas-liquid separator bottom liquid phases end converges with the hot gas of second segment compression outlet conduit after liquor pump pressurization, enter again in second-stage cooler and be cooled to 30 ℃～45 ℃, in second-stage cooler, cooled azeotrope enters subsequently second stage gas-liquid separator and carries out gas-liquid separation, the first heat exchanger channels that the top gas of second stage gas-liquid separator enters ice chest subsequently participates in heat exchange, the second heat exchanger channels that the isolated liquid in gas-liquid separator bottom, the second stage enters ice chest participates in heat exchange,
At first the liquid of being drawn by second stage gas-liquid separator bottom enter the second heat exchanger channels of ice chest, is chilled in advance therein approximately-30 ℃～-80 ℃, after the second throttling set throttling to 0.2 ~ 0.8MPaA, enters the cryogen separator, the first heat exchanger channels by the vapor phase stream thigh of the isolated azeotrope in gas-liquid separator top, the described second stage by ice chest is cooled to-135 ℃～-169 ℃, oppositely enter again the 3rd heat exchanger channels heat exchange of ice chest after first throttle device throttling to 0.2～0.8MPaA, re-heat for example, is drawn to certain temperature (-30 ℃～-80 ℃), with the above-mentioned cryogen that goes out the second throttling set, converge, enter in the cryogen separator and be separated into gas-liquid two-phase, be back to after the gas-liquid two-phase that goes out the cryogen separator converges in the 7th heat exchanger channels of ice chest and cold be provided and then turn back to azeotrope compressor the first compression section for ice chest.
In a preferred implementation, the light constituent of described deethanizing tower top converges with evaporated natural gas (the being BOG gas) stream strand from LNG tank, the 6th heat exchanger channels that enters again described ice chest is cooling, liquefaction, throttling enter flash distillation in the nitrogen flash tank, the be removed to<1mol% of nitrogen in nitrogen flash tank bottom natural gas liquids (LNG).
Preferably, can adopt the reboiler of pattern arbitrarily such as built-in, autoclave, heat siphon type at the bottom of the tower of deethanizing column and rectifying tower.
In a preferred implementation, the gas phase that the rectifying tower tower top obtains is cooled into liquid phase, the part of this liquid phase stores as liquefied petroleum gas product, another part of this liquid phase, optional through pump delivery, enter the liquid phase access road of rectifying tower after converging with the liquid phase at the bottom of tower from deethanizing column.
Here, pressure unit MPaA is MPa, absolute pressure.
For adapting to different unstripped gas heavy hydrocarbons, form, technique described in the utility model arranges at least one Sweet natural gas precooling extraction mouthful in the temperature range of-30 ℃～-80 ℃ of the 4th heat exchanger channels of ice chest, the precooling temperature of the Sweet natural gas by adjusting the 4th heat exchanger channels, capable of regulating enters the amount of liquid phase of heavy hydrocarbon washing tower for the Sweet natural gas washing, even in Sweet natural gas, heavy hydrocarbons content is lower, also can guarantee the normal running of heavy hydrocarbon washing tower.
In this application, generally speaking, an equipment was realized with being connected by pipeline of another equipment.
In this application, " operation " is used interchangeably with " process ".Described " first paragraph compression " or " one section compression " are used interchangeably with " the first compression section ", by that analogy.
Advantage of the present utility model:
1, device of the present utility model adopts brand-new natural gas liquefaction and heavy hydrocarbon to process route, by the methane component liquefaction of being rich in the Sweet natural gas of heavy hydrocarbon, and heavy hydrocarbon component is processed and is reclaimed, and obtains LNG major product and LPG and light oil byproduct, economic and reliable simultaneously;
2, by raw natural gas, self-contained part heavy hydrocarbon component separates, and for the washing of Sweet natural gas heavy constituent, does not need the outside absorption agent of introducing, and Process Route is reasonable;
3, by being set, a plurality of Sweet natural gas precoolings extract mouth out, precooling temperature with the Sweet natural gas that adjusts ice chest the 4th heat exchanger channels, capable of regulating enters the amount of liquid phase of heavy hydrocarbon washing tower for the Sweet natural gas washing, thereby can adapt to larger unstripped gas heavy hydrocarbon compositing range, and turndown ratio is large;
4, use the technique of this device can adapt to the situation that contains the aromatic hydrocarbon such as benzene in unstripped gas, the aromatic hydrocarbon such as benzene are removed with heavy hydrocarbon component, prevent Cold box blocking and freezing.
5, adopt the azeotrope circulation process that cold is provided, and gas phase and liquid phase cryogen enter respectively the ice chest heat exchange, the heat exchange curve of hot and cold liquid is more mated;
6, light constituent deethanizing column separated has carried out reclaiming liquefaction, has improved the liquefied fraction of Sweet natural gas;
7, enter the cryogen separator after the re-heat of backflowing of second stage gas-liquid separator top gas phase cryogen after throttling, can effectively avoid the ice chest hydrops.
The accompanying drawing explanation
Below by accompanying drawing, the utility model is described, in Fig. 1 and Fig. 2, identical parts mean with identical Reference numeral.
Fig. 1 is a kind of process device figure of prior art;
Fig. 2 is process device figure of the present utility model.
Embodiment
The utility model provides a kind of natural gas liquefaction and heavy hydrocarbon treatment unit.Below in conjunction with accompanying drawing, further illustrate.
Device of the present utility model comprises: low-temperature liquefaction device and heavy hydrocarbon treatment unit; The low-temperature liquefaction device comprises an ice chest 7, cryogen separator 9, heavy hydrocarbon separator 6, heavy hydrocarbon topping-up pump 8, nitrogen flash tank 13, refrigerant compression systems and four throttling sets 51,52,53,54, and the heavy hydrocarbon treatment unit comprises a heavy hydrocarbon washing tower 10, deethanizing column 11, rectifying tower 12 and two throttling sets 55,56;
Wherein, the liquor pump 4 that the First water cooler 21 that this refrigerant compression systems comprises a two-section type azeotrope compressor 1, be connected with second segment with the first paragraph of described azeotrope compressor 1 respectively and second water cooler 22, the First gas-liquid separator 31 that is connected with second water cooler 22 with described First water cooler 21 respectively and second gas-liquid separator 32 are connected with First 31 with in the middle of described two gas-liquid separators, the exit end of this liquor pump 4 is connected to the inlet end of second water cooler 22 via pipeline;
Wherein, the gas phase end of the First gas-liquid separator 31 in two gas-liquid separators of refrigerant compression systems is connected with the second compression section of azeotrope compressor 1, with two heat exchanger channels of described ice chest 7, an end (or first end) of the first heat exchanger channels and an end (or first end) of the second heat exchanger channels are connected respectively via two pipelines for the liquid phase end of First gas-liquid separator 31 is connected to 22, the second gas-liquid separators 32 of second water cooler in described two water coolers gas phase end after converging via the outlet conduit of liquor pump 4 and the second compression section and liquid phase end;
This nitrogen flash tank 13 comprises entrance, gaseous phase outlet, liquid-phase outlet;
This heavy hydrocarbon separator 6 comprises a gas inlet passage, a heavy hydrocarbon exit passageway, a gas exit passageway; This heavy hydrocarbon washing tower 10 comprises a natural gas _ raw material gas access road, a gas exit passageway, a heavy hydrocarbon access road, the heavy hydrocarbon exit passageway be connected with inlet end with the 5th throttling set 55; This deethanizing column 11 comprises a heavy hydrocarbon access road, the liquid-phase outlet passage that gaseous phase outlet passage is connected with inlet end with the 6th throttling set 56; This rectifying tower 12 comprises a liquid phase access road, gaseous phase outlet passage (leading to an aftercooler 14) and a light oil exit passageway (leading to a light oil water cooler 17);
This ice chest 7 comprises at least seven heat exchanger channels, at least comprises the first, second, third, fourth, the 5th, the 6th and the 7th heat exchanger channels;
The other end of the first heat exchanger channels of described ice chest (or second end) is connected with an end (or first end) of the 3rd heat exchanger channels via first throttle device 51, and the other end of the 3rd heat exchanger channels (or second end) is connected with the inlet end of cryogen separator 9;
The other end of the second heat exchanger channels (or second end) also is connected with cryogen separator inlet end via the second throttling set 52;
One end (or first end) of the 4th heat exchanger channels is connected with the gas inlet passage of described heavy hydrocarbon separator 6, and the other end of the 4th heat exchanger channels (or second end) is connected with the top gas exit passageway of heavy hydrocarbon washing tower 10;
One end (or first end) of the 5th heat exchanger channels is connected with the top gas phase end of heavy hydrocarbon separator 6, and the other end is connected to LNG tank after via the 4th throttling set 54;
The gaseous phase outlet passage of deethanizing column 11 is optionally evaporated natural gas with the BOG(from LNG tank) after output channel converges, be connected to an end (or first end) of the 6th heat exchanger channels of ice chest 7, the other end of the 6th heat exchanger channels (or second end) is connected in the entrance of nitrogen flash tank 13 via the 3rd throttling set 53, the liquid-phase outlet of nitrogen flash tank 13 also is connected to LNG tank by pipeline;
The top gas phase end of described cryogen separator 9 and bottom liquid phases end converge an end of rear connection the 7th heat exchanger channels, and the other end of the 7th heat exchanger channels is connected with the first compression section of azeotrope compressor 1;
The heavy hydrocarbon exit passageway of described heavy hydrocarbon separator 6 is connected to the input terminus of heavy hydrocarbon topping-up pump 8; The output terminal of heavy hydrocarbon topping-up pump 8 connects the heavy hydrocarbon access road of heavy hydrocarbon washing tower 10;
The natural gas _ raw material gas access road of described heavy hydrocarbon washing tower 10 is connected to the pipeline of carrying purified natural gas (being natural gas _ raw material gas), and the heavy hydrocarbon exit passageway of heavy hydrocarbon washing tower 10 is connected to the heavy hydrocarbon access road of deethanizing column 11 via the 5th throttling set 55;
The liquid-phase outlet of described deethanizing column 11 is connected in the liquid phase access road of rectifying tower 12 via the 6th throttling set 56;
After connecting light oil water cooler 17, the light oil exit passageway that (top) gaseous phase outlet passage of described rectifying tower 12 is connected to liquefied petroleum gas product storage tank and this tower via an aftercooler 14 is connected to the light oil products storage tank.
Wherein, the top gas phase end of heavy hydrocarbon separator 6 can be successively by further being connected to LNG tank after other the 8th heat exchanger channels connection the 4th throttling set by ice chest 7 after the 5th heat exchanger channels of ice chest 7.
In another embodiment, the gaseous phase outlet passage of described rectifying tower 12 is at first via described aftercooler 14 with optionally via a rectifying tower return tank 15, then separate two arms (or being divided into two-way), an arm (or branch road) is connected with the liquefied petroleum gas product storage tank, and another arm (or another branch road), optionally via a pump 16, be connected in the liquid phase access road of rectifying tower 12 after converging with the liquid-phase outlet after the 6th throttling set 56 of deethanizing column 11.
In a preferred implementation, in the temperature range of-30 ℃～-80 ℃ of the 4th heat exchanger channels of described ice chest, at least one Sweet natural gas precooling being set extracts out mouthful, the precooling temperature of the Sweet natural gas by adjusting the 4th heat exchanger channels, capable of regulating enters the amount of liquid phase of heavy hydrocarbon washing tower for the Sweet natural gas washing, even in Sweet natural gas, heavy hydrocarbons content is lower, also can guarantee the normal running of heavy hydrocarbon washing tower.
In a preferred implementation, the gaseous phase outlet passage of described deethanizing column with from the BOG passage of LNG tank, converge after, be connected to an end of the 6th heat exchanger channels of ice chest, realize cooling, liquefaction at the 6th heat exchanger channels of ice chest, again via after the 3rd throttling set 53, being connected to nitrogen flash tank 13, can guarantee the be removed to<1mol% of nitrogen in LNG that nitrogen flash tank bottom obtains.
" first paragraph compression " described here or " one section compression " are used interchangeably with " the first compression section ", by that analogy.
The technical process of the device of use Fig. 2 is as follows:
Use the technique of device of the present utility model to comprise low-temperature liquefaction and heavy hydrocarbon processing two portions; Low-temperature liquefaction partly comprises that in the heavy hydrocarbon treatment unit, the Sweet natural gas after the de-heavy hydrocarbon of part provides cold to realize that in ice chest cooling, fully de-heavy hydrocarbon and liquefaction obtain LNG by azeotrope; The heavy hydrocarbon treating part comprises that the qualified Sweet natural gas of purification that is rich in heavy hydrocarbon sloughs the part heavy hydrocarbon in the heavy hydrocarbon washing tower, the Sweet natural gas of the de-heavy hydrocarbon of part goes the low-temperature liquefaction operation from tower top, and at the bottom of the heavy hydrocarbon washing tower heavy hydrocarbon to enter successively that stripping in deethanizing column removes light constituent (being mainly C1, C2 hydrocarbon etc.) wherein, enters in rectifying tower be LPG and light oil byproduct by the heavy hydrocarbon component rectifying separation; In addition, use the technique of this device can adapt to the situation that contains the aromatic hydrocarbon such as benzene in unstripped gas, the aromatic hydrocarbon such as benzene are removed with heavy hydrocarbon component, prevent Cold box blocking and freezing.
The low-temperature liquefaction operation:
With reference to accompanying drawing 2, in described low-temperature liquefaction operation, whole C5 have been removed from the heavy hydrocarbon treatment process, in heavy hydrocarbon washing tower 10
+and the 4th heat exchanger channels that at first Sweet natural gas of part C3, C4 heavy hydrocarbon component enters ice chest 7 carries out precooling, enter heavy hydrocarbon separator 6 after being cooled to-30 ℃～-80 ℃ and carry out gas-liquid separation, isolate the component such as remaining C3, C4 heavy hydrocarbon Sweet natural gas from heavy hydrocarbon separator 6 bottoms, continue to enter all the other heat exchanger channels (for example the 5th heat exchanger channels) of ice chest 7 from the heavy hydrocarbon separator 6 isolated vapor phase stream thighs in top, and be cooled to therein-130 ℃～-166 ℃, obtain natural gas liquids (LNG); Heavy hydrocarbon separator 6 bottom liquid phases are gone described heavy hydrocarbon treatment process.
Generally, in the low-temperature liquefaction operation, the cold of ice chest is provided by the azeotrope circulation:
The azeotrope be comprised of C1～C5 and N2 (is selected from C1 usually, C2, C3, in C4 and C5 paraffinic hydrocarbons and N2 four kinds, five kinds or six kinds, they mix according to the arbitrary volume ratio or according to the volume ratio that approximately is equal to) enter the entrance of azeotrope compressor 1, be compressed to 0.6～1.8MPaA through first paragraph, enter first step water cooler 21 and be cooled to 30 ℃～45 ℃, enter again first step gas-liquid separator 31 and carry out gas-liquid separation, the first step gas-liquid separator 31 isolated gases in top continue to enter the second segment entrance of compressor, be compressed to 1.2～5.4MPaA through two sections, after the isolated liquid of first step gas-liquid separator 31 bottom liquid phases end converges with the hot gas of second segment compression outlet conduit after liquor pump 4 pressurization, enter again in second-stage cooler 22 and be cooled to 30 ℃～45 ℃, cooled azeotrope enters subsequently second stage gas-liquid separator 32 and carries out gas-liquid separation, the first heat exchanger channels that the top gas of second stage gas-liquid separator 32 enters ice chest 7 subsequently participates in heat exchange, the second heat exchanger channels that the gas-liquid separator 32 isolated liquid in bottom in the second stage enter ice chest 7 participates in heat exchange,
At first the liquid of being drawn by second stage gas-liquid separator 32 bottoms enter the second heat exchanger channels of ice chest 7, is chilled in advance therein approximately-30 ℃～-80 ℃, after the second throttling set 52 throttlings to 0.2 ~ 0.8MPaA, enters cryogen separator 9, the first heat exchanger channels by the vapor phase stream thigh of the described second stage gas-liquid separator 32 isolated azeotropes in top by ice chest 7 is cooled to-135 ℃～-169 ℃, oppositely enter again the 3rd heat exchanger channels heat exchange of ice chest 7 after first throttle device 51 throttlings to 0.2～0.8MPaA, re-heat for example, is drawn to certain temperature (-30 ℃～-80 ℃), with the above-mentioned cryogen that goes out the second throttling set 52, converge, enter cryogen separator 9 and be divided into gas-liquid two-phase, be back to after the gas-liquid two-phase that goes out cryogen separator 9 converges in the 7th heat exchanger channels of ice chest 7 and cold be provided and then turn back to azeotrope compressor 1 first compression section for ice chest 7.
The heavy hydrocarbon treatment process:
In described heavy hydrocarbon treatment process, after being rich in the purification of heavy hydrocarbon (through depickling as CO
2deng, demercuration, dehydration after qualified) Sweet natural gas enter heavy hydrocarbon washing tower 10 bottoms, with the interior top-down liquid phase counter current contact of heavy hydrocarbon washing tower 10, fully after heat and mass, remove the whole C5 in Sweet natural gas
+and the heavy hydrocarbon components such as part C3, C4; Heavy hydrocarbon washing tower 10 C3, the C4 heavy hydrocarbon components of tower top liquid phase source for separating through heavy hydrocarbon separator 6 bottoms in described low-temperature liquefaction operation.Gas phase in heavy hydrocarbon washing tower 6 is gone described low-temperature liquefaction operation from tower top; Heavy hydrocarbon washing tower 10 bottom liquid phases are decompressed to 2.5MPaA～4.0MPaA through the 5th throttling set 55, then enter deethanizing column 11, with the gas phase adverse current contact mass transfer that tower bottom reboiler produces, conduct heat, and remove light constituent (being mainly C1, C2 hydrocarbon etc.) wherein; Light constituent with from the BOG gas of LNG tank, converge after, the 6th heat exchanger channels that enters ice chest 7 is cooling, liquefaction, through the 3rd throttling set 53 throttlings and enter 13 flash distillations of nitrogen flash tank, will be from the nitrogen that may exist in the BOG of LNG tank, be that the nitrogen that unstripped gas liquefaction may be carried while for LNG, entering LNG tank separates from nitrogen flash tank 13, nitrogen flash tank 13 bottoms obtain a nitrogen content in LNG<1%; At the bottom of deethanizing column 11 towers, liquid phase (is mainly C3, C4, C5, C6
+mixture) enter rectifying tower 12 middle parts after the 6th throttling set 56 is decompressed to 0.5MPaA～2.0MPaA, obtain the mixture of the components such as C3, C4 from tower top through rectifying, partial reflux, the part extraction, be the LPG product, separates at the bottom of tower and obtain C5, C6
+etc. the mixture of component, after light oil water cooler 17 is cooled to normal temperature, be light oil products.
Can adopt the reboiler of pattern arbitrarily such as built-in, autoclave, heat siphon type at the bottom of the tower of deethanizing column 11 and rectifying tower 12.
Here, pressure unit MPaA is MPa, absolute pressure.
For adapting to different unstripped gas heavy hydrocarbons, form, technique described in the utility model arranges a plurality of Sweet natural gas precoolings extractions mouthful in the temperature range of-30 ℃～-80 ℃ of the 4th heat exchanger channels of ice chest 7, the precooling temperature of the Sweet natural gas by adjusting the 4th heat exchanger channels, capable of regulating enters the amount of liquid phase of heavy hydrocarbon washing tower 10 for the Sweet natural gas washing, even in Sweet natural gas, heavy hydrocarbons content is lower, also can guarantee the normal running of heavy hydrocarbon washing tower 10.
Claims (6)
1. a natural gas liquefaction and heavy hydrocarbon treatment unit, is characterized in that, this device comprises: low-temperature liquefaction device and heavy hydrocarbon treatment unit;
The low-temperature liquefaction device comprises an ice chest, a cryogen separator, a heavy hydrocarbon separator, a heavy hydrocarbon topping-up pump, a nitrogen flash tank, a refrigerant compression systems and four throttling sets; The heavy hydrocarbon treatment unit comprises a heavy hydrocarbon washing tower, a deethanizing column, a rectifying tower and two throttling sets;
Wherein, the liquor pump that the First water cooler that this refrigerant compression systems comprises a two-section type azeotrope compressor, be connected with second segment with the first paragraph of described azeotrope compressor respectively and second water cooler, the First gas-liquid separator that is connected with second water cooler with described First water cooler respectively and second gas-liquid separator are connected with First with in the middle of described two gas-liquid separators, the exit end of this liquor pump is connected to the inlet end of second water cooler via pipeline;
Wherein, the gas phase end of the First gas-liquid separator in two gas-liquid separators of refrigerant compression systems is connected with the second compression section of azeotrope compressor, the liquid phase end of First gas-liquid separator is connected to second water cooler in described two water coolers after converging via the outlet conduit of liquor pump and the second compression section, and with two heat exchanger channels of described ice chest, an end of the first heat exchanger channels and an end of the second heat exchanger channels are connected respectively via two pipelines for the gas phase end of second gas-liquid separator and liquid phase end;
Described nitrogen flash tank comprises entrance, gaseous phase outlet, liquid-phase outlet;
Described cryogen separator comprises inlet end, top gas phase end and, the bottom liquid phases end;
This heavy hydrocarbon separator comprises a gas inlet passage, a heavy hydrocarbon exit passageway, a gas exit passageway; This heavy hydrocarbon washing tower comprises a natural gas _ raw material gas access road, a gas exit passageway, a heavy hydrocarbon access road, the heavy hydrocarbon exit passageway be connected with inlet end with the 5th throttling set; This deethanizing column comprises a heavy hydrocarbon access road, the liquid-phase outlet passage that gaseous phase outlet passage is connected with inlet end with the 6th throttling set; This rectifying tower comprises a liquid phase access road, a gaseous phase outlet passage and a light oil exit passageway;
This ice chest comprises at least seven heat exchanger channels, at least comprise first second, third, the 4th, the 5th, the 6th and the 7th heat exchanger channels;
The other end of the first heat exchanger channels of described ice chest is connected with an end of the 3rd heat exchanger channels via the first throttle device, and the other end of the 3rd heat exchanger channels is connected with the inlet end of cryogen separator;
The other end of the second heat exchanger channels also is connected with cryogen separator inlet end via the second throttling set;
One end of the 4th heat exchanger channels is connected with the gas inlet passage of described heavy hydrocarbon separator, and the other end of the 4th heat exchanger channels is connected with the top gas exit passageway of heavy hydrocarbon washing tower;
One end of the 5th heat exchanger channels is connected with the top gas phase end of heavy hydrocarbon separator, and the other end is connected to LNG tank after via the 4th throttling set;
After the gaseous phase outlet passage of deethanizing column optionally converges with evaporated natural gas (the being BOG) output channel from LNG tank, be connected to an end of the 6th heat exchanger channels of ice chest, the other end of the 6th heat exchanger channels is connected in the entrance of nitrogen flash tank via the 3rd throttling set, nitrogen flash tank liquid-phase outlet also is connected to LNG tank by pipeline;
The top gas phase end of described cryogen separator and bottom liquid phases end converge an end of rear connection the 7th heat exchanger channels, and the other end of the 7th heat exchanger channels is connected with the first compression section of azeotrope compressor;
The heavy hydrocarbon exit passageway of described heavy hydrocarbon separator is connected to the input terminus of heavy hydrocarbon topping-up pump; Heavy hydrocarbon supercharging delivery side of pump connects the heavy hydrocarbon access road of heavy hydrocarbon washing tower;
The natural gas _ raw material gas access road of described heavy hydrocarbon washing tower is connected to the pipeline of carrying purified natural gas (being natural gas _ raw material gas), and the heavy hydrocarbon exit passageway of heavy hydrocarbon washing tower connects the heavy hydrocarbon access road of deethanizing column via the 5th throttling set;
The liquid-phase outlet of described deethanizing column is connected in the liquid phase access road of rectifying tower via the 6th throttling set;
After connecting the light oil water cooler, the light oil exit passageway that the gaseous phase outlet passage of described rectifying tower is connected to liquefied petroleum gas product storage tank and this tower via an aftercooler is connected to the light oil products storage tank.
2. natural gas liquefaction according to claim 1 and heavy hydrocarbon treatment unit, it is characterized in that: the gaseous phase outlet passage of described rectifying tower is at first via described aftercooler with optionally via a rectifying tower return tank, then separate two arms, an arm is connected with the liquefied petroleum gas product storage tank, and another arm, optionally via a pump, be connected in the liquid phase access road of rectifying tower after converging with the liquid-phase outlet after the 6th throttling set of deethanizing column.
3. natural gas liquefaction according to claim 1 and 2 and heavy hydrocarbon treatment unit, it is characterized in that: the top gas phase end of described heavy hydrocarbon separator connects the 4th throttling set by other the 8th heat exchanger channels that further passes through ice chest after the 5th heat exchanger channels of ice chest successively, then is connected to LNG tank.
4. natural gas liquefaction according to claim 1 and 2 and heavy hydrocarbon treatment unit is characterized in that: adopt built-in, autoclave or thermosyphon reboiler at the bottom of the tower of described deethanizing column and/or described rectifying tower.
5. natural gas liquefaction according to claim 1 and 2 and heavy hydrocarbon treatment unit is characterized in that: in the temperature range of-30 ℃～-80 ℃ of the 4th heat exchanger channels of described ice chest, at least one Sweet natural gas precooling is set and extracts out mouthful.
6. natural gas liquefaction according to claim 1 and 2 and heavy hydrocarbon treatment unit, it is characterized in that: the gaseous phase outlet passage of described deethanizing column with from evaporated natural gas (the being BOG) output channel of LNG tank, converge after, be connected to an end of the 6th heat exchanger channels of ice chest.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012206882327U CN202924980U (en) | 2012-12-13 | 2012-12-13 | Natural gas liquefaction and heavy hydrocarbon treatment device |
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| CN2012206882327U CN202924980U (en) | 2012-12-13 | 2012-12-13 | Natural gas liquefaction and heavy hydrocarbon treatment device |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103031169A (en) * | 2012-12-13 | 2013-04-10 | 新地能源工程技术有限公司 | Method and device for carrying out liquefaction and heavy hydrocarbon treatment on natural gas |
| CN104089463A (en) * | 2014-07-16 | 2014-10-08 | 北京安珂罗工程技术有限公司 | Mixed refrigerant gas-liquid separating type throttling and refrigerating method and system |
| CN108700372A (en) * | 2016-02-26 | 2018-10-23 | 巴布科克知识产权管理（第）有限公司 | The method and its device of cooling boil-off gas |
| CN113390283A (en) * | 2020-03-13 | 2021-09-14 | 气体产品与化学公司 | Heat exchanger device, manifold arrangement for a heat exchanger device and related method |
-
2012
- 2012-12-13 CN CN2012206882327U patent/CN202924980U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103031169A (en) * | 2012-12-13 | 2013-04-10 | 新地能源工程技术有限公司 | Method and device for carrying out liquefaction and heavy hydrocarbon treatment on natural gas |
| CN103031169B (en) * | 2012-12-13 | 2014-05-07 | 新地能源工程技术有限公司 | Method and device for carrying out liquefaction and heavy hydrocarbon treatment on natural gas |
| CN104089463A (en) * | 2014-07-16 | 2014-10-08 | 北京安珂罗工程技术有限公司 | Mixed refrigerant gas-liquid separating type throttling and refrigerating method and system |
| CN104089463B (en) * | 2014-07-16 | 2017-11-17 | 北京安珂罗工程技术有限公司 | A kind of method and system of azeotrope gas-liquid separating throttling refrigeration |
| CN108700372A (en) * | 2016-02-26 | 2018-10-23 | 巴布科克知识产权管理（第）有限公司 | The method and its device of cooling boil-off gas |
| CN108700372B (en) * | 2016-02-26 | 2020-11-03 | 巴布科克知识产权管理（第一）有限公司 | Method and apparatus for cooling boil-off gas |
| CN113390283A (en) * | 2020-03-13 | 2021-09-14 | 气体产品与化学公司 | Heat exchanger device, manifold arrangement for a heat exchanger device and related method |
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