CN105890284A - Heavy hydrocarbon removal device and method for liquefied natural gas - Google Patents
Heavy hydrocarbon removal device and method for liquefied natural gas Download PDFInfo
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- CN105890284A CN105890284A CN201610302516.0A CN201610302516A CN105890284A CN 105890284 A CN105890284 A CN 105890284A CN 201610302516 A CN201610302516 A CN 201610302516A CN 105890284 A CN105890284 A CN 105890284A
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- Prior art keywords
- heavy hydrocarbon
- ice chest
- azeotrope
- pipeline
- unstripped gas
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 124
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 124
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 122
- 238000000034 method Methods 0.000 title claims abstract description 42
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 29
- 239000007789 gas Substances 0.000 claims abstract description 80
- 239000007791 liquid phase Substances 0.000 claims abstract description 48
- 238000001816 cooling Methods 0.000 claims abstract description 20
- 238000005406 washing Methods 0.000 claims abstract description 11
- 239000007792 gaseous phase Substances 0.000 claims abstract description 7
- 238000002156 mixing Methods 0.000 claims description 22
- 238000010992 reflux Methods 0.000 claims description 15
- 239000012808 vapor phase Substances 0.000 claims description 13
- 239000006200 vaporizer Substances 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 9
- 238000001704 evaporation Methods 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 6
- 238000005057 refrigeration Methods 0.000 claims description 6
- 239000003507 refrigerant Substances 0.000 claims description 5
- 239000000284 extract Substances 0.000 claims description 3
- 230000036651 mood Effects 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 claims 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 32
- 239000003345 natural gas Substances 0.000 abstract description 16
- 238000003860 storage Methods 0.000 abstract description 10
- 238000005516 engineering process Methods 0.000 abstract description 8
- 238000009833 condensation Methods 0.000 abstract description 6
- 230000005494 condensation Effects 0.000 abstract description 5
- 239000000463 material Substances 0.000 abstract description 5
- 239000002826 coolant Substances 0.000 abstract 1
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 16
- 230000008569 process Effects 0.000 description 14
- 230000000694 effects Effects 0.000 description 9
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 8
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 238000005201 scrubbing Methods 0.000 description 6
- 238000007654 immersion Methods 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000008859 change Effects 0.000 description 3
- 238000005457 optimization Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 125000004836 hexamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 101100298225 Caenorhabditis elegans pot-2 gene Proteins 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000001914 calming effect Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 230000008407 joint function Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000010181 polygamy Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—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
-
- 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
- F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
-
- 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
- F25J5/005—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 in a reboiler-condenser, e.g. within a column
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a heavy hydrocarbon removal device and method for liquefied natural gas. The heavy hydrocarbon removal device comprises a mixed coolant circulation device, a cooling box, a low-temperature separator, a heavy hydrocarbon heat exchanger and a material gas input pipeline connected with the cooling box, wherein the top of the low-temperature separator is provided with a condensation evaporator; a material gas outlet in the upper part of the cooling box is connected with the inlet of the condensation evaporator; the gaseous phase outlet of the condensation evaporator is connected with a material gas inlet end at the lower part of the cooling box; and the liquid phase outlet of the condensation evaporator is connected with the inlet of the low-temperature separator. According to the heavy hydrocarbon removal device and method, a technology of self-condensation and backflow of heavy hydrocarbon in natural gas is adopted; the system self-regulating function is high; applicability is high; and a heavy hydrocarbon backflow pump, a heavy hydrocarbon backflow storage cylinder and the like are omitted, so that investment is favorably reduced, and system operability is increased; and control on the content of the heavy hydrocarbon in the natural gas entering the lower part of the cooling box is increased through heavy hydrocarbon backflow washing, so that operation stability is favorably improved. The technology is particularly suitable for a condition that the content of the heavy hydrocarbon in the natural gas is high, and the heavy hydrocarbon needs to be removed.
Description
Technical field
The present invention relates to the de-weight of MRC (azeotrope refrigeration) technique LNG (liquefied natural gas) of a kind of improvement
Hydrocarbon devices and methods therefor, compared with current existing LNG de-heavy hydrocarbon apparatus and method thereof, the invention enables de-
Heavy hydrocarbon process requirements equipment reduces, and flow process is compacter, and operation easier reduces, under variable working condition or different makings
Adaptability dramatically increase.
Background technology
Along with LNG industry develops rapidly in recent years, MRC technique LNG device is used gradually to increase.And at this
Whether in a little devices, the removing of natural gas heavy hydrocarbon is a very important link, also contribute to LNG device and can
Even running.Current domestic MRC refrigeration process LNG device takes off heavy hydrocarbon technique mainly to be had following several existing
Technology；
1, Conventional cryogenic separating technology:
Such as Fig. 1, including azeotrope circulating device, and natural gas liquefaction device, and de-heavy hydrocarbon apparatus.
Room temperature in azeotrope circulating device, low-pressure vapor phase cryogen, after refrigerant compressor compresses, are divided into height
Phase of calming the anger cryogen and high-pressure liquid phase cryogen two-way, high-pressure liquid phase cryogen through heavy hydrocarbon exchanger heat exchange after with high pressure
The mixing of gas phase cryogen obtains high pressure mixing cryogen and enters from the top of ice chest, and from top to down with from bottom to top
Reflux azeotrope carry out heat exchange, time to ice chest obtain low temperature liquid phase cryogen, azeotrope temperature
It is about-150 DEG C, then through valve expansion throttling, it is thus achieved that lower temperature, the liquid-phase mixing cryogen of lower pressure,
Flowing from bottom to top, and carry out heat exchange with high temperature azeotrope, the unstripped gas of both sides, azeotrope is multiple
Rise to room temperature after heat by ice chest Base top contact, again enter compressor and complete a kind of refrigeration cycle.
Purifying raw natural gas to enter from ice chest top, from ice chest, cold section of extraction, is divided by cold catch pot
After heavy hydrocarbon, return to ice chest continue cooling, finally obtain LNG product from ice chest bottom, and send to after treatment
Storage tank.
The heavy hydrocarbon of cold catch pot bottom removing carries out heat exchange with high-pressure liquid phase cryogen and reclaims cold.Treated
After send to storage tank.
In said apparatus start-up process, the thermograde of ice chest has a process gradually built up.Setting up
Cheng Zhong, the temperature before the unstripped gas drawn in the middle part of ice chest enters cold catch pot can't drop to temperature required,
Will result in heavy hydrocarbon natural gas off quality and introduce the bottom of ice chest heat exchanger, will result in startup procedure low temperature
Blocking risk increases, and therefore, above-mentioned Conventional cryogenic separating technology generally also needs to increase by one group of heat exchanger that goes into operation.
As CN201320066196.5-LNG produces the removing heavy hydrocarbon apparatus of equipment.The heat exchanger that goes into operation is positioned at heavy hydrocarbon and divides
(not shown in figure 1) before device, it is ensured that when initial stage ice chest top of driving cannot provide cold, raw material
Gas cools to about one 60 DEG C by the heat exchanger that goes into operation, the most again by cold catch pot by heavy hydrocarbon condense after from
Unstripped gas is separated.
2, the heavy hydrocarbon separating technology of band washing:
Such as Fig. 2, azeotrope circulating device is compared with technology 1.
Purify raw natural gas and lead to heavy hydrocarbon scrubbing tower from ice chest precooling zone, return in ice chest after washing
Cold section of cooling, then return to ice chest after leading to heavy hydrocarbon return tank separation heavy hydrocarbon and continue cooling, finally from ice chest
Portion obtains LNG product, and sends to storage tank after treatment.
The heavy hydrocarbon separated from heavy hydrocarbon return tank is squeezed into heavy hydrocarbon scrubbing tower by heavy hydrocarbon reflux pump and is washed, weight
The heavy hydrocarbon of hydrocarbon scrubbing tower bottom removing carries out heat exchange with high-pressure liquid phase cryogen and reclaims cold.Send to after treatment
Storage tank.
3, room temperature washing process: such as Fig. 3, this technique typically uses isopentane to be solvent, at room temperature or lower slightly
Under room temperature, by the similar principle that mixes of isopentane, in heavy hydrocarbon scrubbing tower, isopentane flows from the top down,
Natural gas flows from bottom to top, by natural gas and isopentane contact and perforated space exchanges and makes the heavy hydrocarbon of natural gas
Abjection, and directly go storage tank to store rich in the isopentane that heavy hydrocarbon is many.Heavy hydrocarbon scrubbing tower bottom removing heavy hydrocarbon with
Isopentane carries out heat exchange and reclaims cold.Send to storage tank after treatment.
The shortcoming of above-mentioned prior art is:
Prior art 1 is simple low temperature separating process, uses separator to separate heavy hydrocarbon at low temperatures, and fills
Put technique can not absolute stability, by raw natural gas change of component, and the component of azeotrope and
Just pressure reduction impact, makes to increase into the temperature of charge of separator or time pressure increases, the former separator of being dissolved in
The heavy constituents such as benzene in liquid phase, hexamethylene, pungent pentane can flash off, and causes the variation of separating effect, from
And easily cause the blocking of ice chest low temperature.The de-heavy hydrocarbon result of different temperatures is shown in Fig. 5.
Secondly, the heat exchanger that goes into operation of increase only uses in the stage that goes into operation, and is again that equipment is not busy at normal operating phase
Put waste, shortage effect.
Prior art 2 is to use Conventional cryogenic washing process to increase the dynamic equipment such as heavy hydrocarbon pump, increases answering of operation
Polygamy and energy expenditure, increase the complexity of system.Limited by pump performance, thus limited device heavy hydrocarbon
Adaptability.
Prior art 3 room temperature isopentane washing process increases the consumption of isopentane, and the operation adding device becomes
This.
Summary of the invention
Present invention aim at: provide that a kind of technique is simple, equipment is few, flow process is compact, operation easier is low
Liquefied natural gas de-heavy hydrocarbon apparatus and method, use apparatus and method of the present invention, variable working condition or different makings
Under adaptability dramatically increase.
The present invention use a kind of liquefied natural gas de-heavy hydrocarbon apparatus, including azeotrope circulating device, ice chest,
Cold catch pot, heavy hydrocarbon heat exchanger, and unstripped gas the first intake pipeline being connected with ice chest, cryogenic separation
The top of device arranges a condenser/evaporator, and cold catch pot constitutes knockout tower with condenser/evaporator；Ice chest top
Unstripped gas exit by unstripped gas the second intake pipeline connect condenser/evaporator entrance, condenser/evaporator
Gaseous phase outlet by unstripped gas the 3rd intake pipeline connect ice chest bottom unstripped gas arrival end；
The liquid-phase outlet of described condenser/evaporator connects the entrance of cold catch pot by reflux pipeline.
Use the said apparatus of the present invention, by increasing condenser/evaporator, it is achieved that the heavy hydrocarbon removing of unstripped gas,
Heavy hydrocarbon after removing is back to cold catch pot by reflux pipeline, carries out the backflow washing of heavy hydrocarbon self, has
Effect departs from heavy hydrocarbon, and removes benzene that may be present, hexamethylene etc. and easily block material, it is ensured that the removing of heavy hydrocarbon
Effect.When operating mode changes, when making the unstripped gas temperature extracted out from ice chest change, condensation evaporation
Device, by adjusting the flow (controlling the liquid level of azeotrope) of low-temperature receiver medium (azeotrope), can be adjusted automatically
The whole cold carrying out heat exchange with unstripped gas, the heavy hydrocarbon reflux temperature of gas-liquid separation removing can easily control
With regulation, so that it is guaranteed that heavy hydrocarbon enters stablizing of the heavy hydrocarbon reflux temperature of cold catch pot, automatically improve heavy hydrocarbon
Abjection effect.
Particularly go into operation the stage at device, when the unstripped gas temperature extracted out from ice chest or room temperature, suitably increase
Adding the flow of low-temperature receiver medium, condenser/evaporator serves the effect of the heat exchanger that goes into operation, and goes into operation heat exchanger with routine
Compare, owing to changing into heat exchange after knockout tower before entering separator, this independent condenser/evaporator can be made
In addition to playing the effect of the heat exchanger that goes into operation, the effect of the overhead condenser also brought into normal play.
After device progresses into normal production, the condenser/evaporator keeping azeotrope to stablize liquid level provides steady
Determining cold temperature source, when feed gas composition or technological parameter (unstripped gas temperature) occur fluctuation, heavy hydrocarbon passes through
The adjustment of the azeotrope liquid level of immersion condenser/evaporator, it is ensured that the cooling needed for unstripped gas removing heavy hydrocarbon
Temperature, it is ensured that pure from knockout tower unstripped gas out, enters ice chest bottom and does not blocks.
Condenser/evaporator recommends to take the structure of intrusive mood condenser/evaporator, uses plate-fin heat exchanger to make cold
Condenser, can effectively reduce equipment size and weight, it is simple to the system integration.
Further improve and be, described unstripped gas the first intake pipeline also by unstripped gas the 5th intake pipeline with
The arrival end of heavy hydrocarbon heat exchanger connects, and the port of export of heavy hydrocarbon heat exchanger is connected by unstripped gas the 6th intake pipeline
Unstripped gas the second intake pipeline.
Heavy hydrocarbon and unstripped gas heat exchange rather than with liquid refrigerant heat exchange, no matter be to drive or product stream in device cold conditions
In the case of amount unusual fluctuations, all stable heat exchange on heavy hydrocarbon do not affect, with conventional liq cryogen and separator
End heavy hydrocarbon heat exchange compares, and can guarantee that heavy hydrocarbon re-heat is good, and downstream process equipment does not has brittle fracture under low temperature risk,
Being also beneficial to the efficient recovery of heavy hydrocarbon cold, prior art, when start-up is without liquid phase cryogen, heavy hydrocarbon cannot
Heat exchange, can only abandon the recovery of heavy hydrocarbon.Particularly use plate type heat exchanger when heat exchanger, it is simple to ice chest collection
Becoming, heat exchanger is shorter with knockout tower connecting line, and device is compacter.
Further improve is that the separator liquid-phase outlet in described azeotrope circulating device is cold by mixing
Agent the second intake pipeline connects ice chest top, and by the pipeline high-pressure liquid phase cryogen from side in the middle part of ice chest
Exit passes, and through first throttle valve, is again introduced into ice chest bottom with azeotrope the 6th intake pipeline even
Connect；Separator gaseous phase outlet by azeotrope the 3rd intake pipeline connect ice chest top, and by pipeline from
Pass bottom ice chest, through second throttle, by azeotrope the 5th intake pipeline bottom ice chest again
Enter ice chest and be connected with azeotrope the 6th intake pipeline；Azeotrope the 6th intake pipeline is from ice chest top
Pass and connect compressor by azeotrope the first intake pipeline；In the middle part of ice chest, high-pressure liquid phase cryogen in side is drawn
Hold the low-temperature receiver entrance connecting condenser/evaporator also by azeotrope the 7th intake pipeline, the steaming of condenser/evaporator
Send out side outlet and connect reflux azeotrope intake pipeline by azeotrope the 8th intake pipeline；Described reflux is mixed
Close cryogen intake pipeline include azeotrope the 5th intake pipeline, azeotrope the 6th intake pipeline, mix cold
Agent the first intake pipeline.
Low-pressure vapor phase azeotrope from evaporation side out after, reflux can be entered according to selecting under different working temperatures
The diverse location of azeotrope intake pipeline, in order to efficient recovery cold.
As the replacement of apparatus of the present invention, above-mentioned separator liquid-phase outlet is connected by azeotrope intake pipeline
The low-temperature receiver entrance of condenser/evaporator.
Present invention additionally comprises a kind of liquefied natural gas and take off heavy hydrocarbon method, circulate stream including azeotrope；With former
The liquefaction stream of material gas, specifically includes following steps:
A purifies unstripped gas and enters ice chest, and the unstripped gas exit from ice chest top is extracted out；
The unstripped gas that B extracts out enters the condensing vaporizer on knockout tower top, carries out gas-liquid separation removing heavy hydrocarbon；
The heavy hydrocarbon that C separates from unstripped gas is entered by backflow heavy hydrocarbon pipeline from the liquid-phase outlet of condensing vaporizer
The cold catch pot entering knockout tower bottom washs；
Heavy hydrocarbon after D washing is extracted out bottom cold catch pot, after cold is reclaimed in heavy hydrocarbon heat exchanger heat exchange,
Pipeline is drawn.
Further improve is that the purification unstripped gas of described step A enters heavy hydrocarbon heat exchanger also by pipeline
Cooling duct, the heavy hydrocarbon heat exchange obtained with step D, absorb the unstripped gas after cold by pipeline and step A
The unstripped gas mixing that ice chest top unstripped gas exit is extracted out.
Further improving and be, described azeotrope circulation stream comprises the steps:
From ice chest top, low-pressure vapor phase azeotrope out enters compressor boost to a；
Then b carries out gas-liquid separation by separator；
High-pressure liquid phase azeotrope after c separates enters ice chest cooling by pipeline, and the high-pressure liquid phase after cooling mixes
Closing cryogen to draw from ice chest, a part obtains low pressure liquid-phase mixing cryogen through choke valve expenditure and pressure, by pipe
Road is again introduced into ice chest；The low-temperature receiver that another part enters the condensing vaporizer described in step B by pipeline leads to
Road, carries out re-heat after heat exchange with the unstripped gas of step B, by pipeline from the evaporation side of condensing vaporizer
Low-pressure vapor phase azeotrope is drawn in outlet；
High pressure vapor azeotrope after d separates enters ice chest cooling by pipeline, draws, warp bottom ice chest
After choke valve expenditure and pressure, bottom ice chest, it is again introduced into ice chest, and cold with the low pressure liquid-phase mixing of step c
Agent is converged by pipeline；
E low pressure liquid-phase mixing cryogen flows from bottom to top, and with step c, d enter ice chest azeotrope,
Step A enters the unstripped gas of ice chest and carries out after heat exchange by ice chest Base top contact, again enters compressor and completes one
Individual kind of refrigeration cycle stream.
The low-pressure vapor phase azeotrope that step d described in f is drawn according to different temperatures, select or with step c institute
The low pressure liquid-phase mixing cryogen stated is converged by pipeline, or with described in step d enter ice chest low pressure liquid phase
Azeotrope pipeline converges, or with the low pressure liquid-phase mixing refrigerant tube from ice chest Base top contact described in step e
Road is converged.
Accompanying drawing explanation
The present invention by by embodiment and with reference to Figure of description by the way of illustrate, wherein:
Fig. 1 is the process chart of prior art 1.
Fig. 2 is the process chart of prior art 2.
Fig. 3 is the process chart of prior art 3.
Fig. 4 is the process chart of the present invention.
Fig. 5 is different temperatures unstripped gas Comparative result of de-heavy hydrocarbon in separator.
Detailed description of the invention
All features disclosed in this specification, or disclosed all methods or during step, except mutually
Beyond the feature repelled and/or step, all can combine by any way.This specification (includes any additional
Claim, summary and accompanying drawing) disclosed in any feature, unless specifically stated otherwise, all can by other equivalence
Or the alternative features with similar purpose replaced.I.e., unless specifically stated otherwise, each feature is one to be
An example in row equivalence or similar characteristics.
The embodiment of the present invention a kind of MRC liquefied natural gas de-heavy hydrocarbon apparatus as shown in Figure 4, cold including mixing
The knockout tower of condenser/evaporator 3 composition at agent circulating device, ice chest 1, cold catch pot 2 and its top, weight
Hydrocarbon heat exchanger 4, said apparatus and connecting line define azeotrope circulation stream and the fluidized flow of unstripped gas
Road.
The liquefaction stream of unstripped gas specifically includes following steps:
The purification unstripped gas of A, 4-6MPa enters ice chest by the first intake pipeline NG-1, cold through ice chest
But to-50 DEG C--70 DEG C, the unstripped gas exit from ice chest top is extracted out；
It should be noted that go into operation the stage, the unstripped gas extracted out from the unstripped gas exit of ice chest is room temperature.
B, unstripped gas enter the condensing vaporizer on knockout tower top by unstripped gas the second intake pipeline NG-2,
Condense after condenser/evaporator with azeotrope heat exchange, it is achieved gas-liquid separation removing heavy hydrocarbon, after removing heavy hydrocarbon
The gaseous phase outlet of unstripped gas condensed formula vaporizer is again introduced into ice chest by unstripped gas the 3rd intake pipeline NG-3
Lower feed gas arrival end, continues cooling, liquefaction, by the 4th intake pipeline bottom ice chest in ice chest
NG-4 draws, it is thus achieved that temperature is the LNG product of about-155 DEG C, removes LNG after the 3rd choke valve V3 throttling
Storage tank.
Go into operation the stage, suitably increase the flow of condenser/evaporator low-temperature receiver medium, as increased the liquid level of azeotrope,
Realize room temperature is purified the heavy hydrocarbon removing of unstripped gas.
The heavy hydrocarbon separated in C, step B is entered by backflow heavy hydrocarbon pipeline from the liquid-phase outlet of condensing vaporizer
The cold catch pot of knockout tower bottom washs；Cold catch pot pressure general control is at 3-4MPa；
D, bottom cold catch pot extract out washing after heavy hydrocarbon Cx, through heavy hydrocarbon heat exchanger heat exchange reclaim cold
After, pipeline leads to heavy hydrocarbon storage tank.
Optimization as apparatus of the present invention designs, and condenser/evaporator recommends to take the knot of intrusive mood condenser/evaporator
Structure, uses plate-fin heat exchanger to make condenser.
Optimization as apparatus of the present invention designs, and step A unstripped gas passes through unstripped gas the 5th intake pipeline NG-5
Divide a plume to be connected with the cooling duct arrival end of heavy hydrocarbon heat exchanger, obtain with step D in heavy hydrocarbon heat exchanger
Heavy hydrocarbon heat exchange, absorb the shunting unstripped gas after cold by unstripped gas the 6th intake pipeline NG-6 and step A
The unstripped gas that ice chest top unstripped gas exit is extracted out converges.
Optimization as apparatus of the present invention designs, and described azeotrope circulation stream comprises the steps:
From ice chest top, low-pressure vapor phase azeotrope MR-1 out enters surge tank 6 and enters back into compressor 4 a
Supercharging；
Then b carries out gas-liquid separation by separator 5；
High-pressure liquid phase azeotrope MR-2 after step c b separates is entered by pipeline from separator liquid-phase outlet
Ice chest is cooled to-50 DEG C--and 70 DEG C, the high-pressure liquid phase azeotrope after cooling is drawn from ice chest, a part of warp
First throttle valve V1 expenditure and pressure obtains low pressure liquid-phase mixing cryogen MR-3 to 0.3MPa, by pipeline again
Enter ice chest；Another part high-pressure liquid phase azeotrope MR-7 is entered by the 4th choke valve V4 expenditure and pressure
The low-temperature receiver passage of condensing vaporizer, carries out re-heat after heat exchange with the unstripped gas of step B, by pipeline from
Low-pressure vapor phase azeotrope MR-8 is drawn in the evaporation side outlet of condensing vaporizer；
High pressure vapor azeotrope MR-3 after Step d b separates is entered by pipeline from separator gaseous phase outlet
Ice chest is cooled to-150 DEG C to-155 DEG C, draws bottom ice chest, throttles through second throttle V2 expenditure and pressure
It is decompressed to after 0.4MPa obtain low pressure liquid-phase mixing cryogen MR-5, bottom ice chest, is again introduced into ice chest, and with
The low pressure liquid-phase mixing cryogen of step c converges acquisition low-pressure vapor phase azeotrope MR-6 by pipeline in ice chest；
Low pressure liquid-phase mixing cryogen in e ice chest flows from bottom to top, and enters the mixed of ice chest with step c, d
Conjunction cryogen MR-2, MR-3, step A enter the unstripped gas of ice chest and carry out heat exchange, by ice chest top after re-heat
Draw and obtain low-pressure vapor phase azeotrope MR-1, again entered compressor by surge tank and complete a kind of refrigeration cycle
Stream.
The low-pressure vapor phase azeotrope MR-8 that step c described in f is drawn, according to different temperatures, selects or and step
Low pressure liquid-phase mixing cryogen described in c is converged by pipeline 1B, or with described in step d enter ice chest low
Hydraulic fluid phase azeotrope is converged by pipeline 1C, or with the low pressure gas from ice chest Base top contact described in step e
Phase azeotrope is converged by pipeline 1A.Thus effectively reclaim flow.
By technical scheme, MRC technique LNG device is only by adding compact immersion
Formula condenser/evaporator and the trickle change of technological process, but make whole technique decrease heavy hydrocarbon return tank, heavy hydrocarbon
Scrubbing tower, low temperature heavy hydrocarbon pump, go into operation the equipment such as heat exchanger, substantially reduces technological process, improves device
Stability and operability.Have the following characteristics that
1 employing immersion condenser/evaporator is ingenious with the combination of cold catch pot is used in MRC technique LNG
Device takes off in heavy hydrocarbon technique, it is achieved backflow, the stable heavy hydrocarbon effect certainly of heavy hydrocarbon；
2 simultaneously this immersion condenser/evaporator double as, in the stage of going into operation, the heat exchanger that goes into operation, in normal production, make tower
Top condenser；
The heavy hydrocarbon of 3 separator bottom enters hydrocarbon mixture storage tank after carrying out re-heat heat exchange with partial raw gas, and cold
But before the natural gas after enters heavy hydrocarbon separator.
This technique compared with the prior art, the technique using heavy hydrocarbon self condensing reflux in natural gas, have
System self-regulation joint function is strong, strong adaptability；Decrease heavy hydrocarbon reflux pump, heavy hydrocarbon reflux accumulator etc. simultaneously, have
It is beneficial to reduce investment, and adds system operability；By heavy hydrocarbon backflow washing, increase entering ice chest
The control of the heavy hydrocarbons content of the natural gas of bottom, is conducive to improving the stability run.This technique adapts to especially
The more situation needing again de-heavy hydrocarbon of heavy hydrocarbons content in natural gas.
Above-mentioned steps c draws high-pressure liquid phase cryogen MR-2 to immersion condenser/evaporator also dependent on practical situation
Cooling duct, provides low-temperature receiver for condenser/evaporator.
Although the present invention having been carried out example and description according to preferred embodiment, it is to be understood that this
Bright it is not limited to aforesaid detailed description of the invention.The present invention's illustrated in without departing substantially from claims
In the case of, this can be made alterations and modifications, the present invention expands to any new spy disclosed in this manual
Levy or any new combination, and the arbitrary new method that discloses or the step of process or any new combination.
Claims (8)
1. a liquefied natural gas de-heavy hydrocarbon apparatus, including azeotrope circulating device, ice chest, cold catch pot, heavy hydrocarbon heat exchanger, and unstripped gas the first intake pipeline being connected with ice chest, it is characterised in that:
The top of cold catch pot arranges a condenser/evaporator, and cold catch pot forms knockout tower with condenser/evaporator；The unstripped gas exit on ice chest top connects the entrance of condenser/evaporator by unstripped gas the second intake pipeline, and the gaseous phase outlet of condenser/evaporator connects the unstripped gas arrival end of ice chest bottom by unstripped gas the 3rd intake pipeline；
The liquid-phase outlet of described condenser/evaporator connects the entrance of cold catch pot by reflux pipeline.
MRC liquefied natural gas de-heavy hydrocarbon apparatus the most according to claim 1, it is characterized in that: described unstripped gas the first intake pipeline is connected with the arrival end of heavy hydrocarbon heat exchanger also by unstripped gas the 5th intake pipeline, the port of export of heavy hydrocarbon heat exchanger connects unstripped gas the second intake pipeline by unstripped gas the 6th intake pipeline.
Liquefied natural gas de-heavy hydrocarbon apparatus the most according to claim 1 and 2, it is characterized in that: the separator liquid-phase outlet in described azeotrope circulating device connects ice chest top by azeotrope the second intake pipeline, and passed from the high-pressure liquid phase cryogen exit of side in the middle part of ice chest by pipeline, through first throttle valve, it is again introduced into ice chest bottom and is connected with azeotrope the 6th intake pipeline；
Separator gaseous phase outlet connects ice chest top by azeotrope the 3rd intake pipeline, and passed bottom ice chest by pipeline, through second throttle, bottom ice chest, it is again introduced into ice chest by azeotrope the 5th intake pipeline and is connected with azeotrope the 6th intake pipeline；
Azeotrope the 6th intake pipeline passes from ice chest top and connects compressor by azeotrope the first intake pipeline；
In the middle part of ice chest, high-pressure liquid phase cryogen exit in side connects the low-temperature receiver entrance of condenser/evaporator also by azeotrope the 7th intake pipeline, and the evaporation side outlet of condenser/evaporator connects reflux azeotrope intake pipeline by azeotrope the 8th intake pipeline；
Described reflux azeotrope intake pipeline includes azeotrope the 5th intake pipeline, azeotrope the 6th intake pipeline, azeotrope the first intake pipeline.
Liquefied natural gas de-heavy hydrocarbon apparatus the most according to claim 3, it is characterised in that: separator liquid-phase outlet connects the low-temperature receiver entrance of condenser/evaporator by azeotrope intake pipeline.
Liquefied natural gas de-heavy hydrocarbon apparatus the most according to claim 3, it is characterised in that: described condenser/evaporator is intrusive mood condenser/evaporator.
6. liquefied natural gas takes off a heavy hydrocarbon method, circulates stream including azeotrope；It is characterized in that, also include the liquefaction stream of unstripped gas, specifically include following steps:
A purifies unstripped gas and enters ice chest, and the unstripped gas exit from ice chest top is extracted out；
The unstripped gas that B extracts out enters the condensing vaporizer on knockout tower top, carries out gas-liquid separation removing heavy hydrocarbon；
The cold catch pot that the heavy hydrocarbon that C separates from unstripped gas enters knockout tower bottom from the liquid-phase outlet of condensing vaporizer by backflow heavy hydrocarbon pipeline washs；
Heavy hydrocarbon after D washing is extracted out bottom cold catch pot, and after cold is reclaimed in heavy hydrocarbon heat exchanger heat exchange, pipeline is drawn.
7. a liquefied natural gas as claimed in claim 6 takes off heavy hydrocarbon method, it is characterised in that:
The unstripped gas that purifies of described step A enters the cooling duct of heavy hydrocarbon heat exchanger, the heavy hydrocarbon heat exchange obtained with step D also by pipeline, and the unstripped gas that the unstripped gas after absorption cold is extracted out with step A ice chest top unstripped gas exit by pipeline mixes.
8. a liquefied natural gas as claimed in claims 6 or 7 takes off heavy hydrocarbon method, it is characterised in that: described azeotrope circulation stream comprises the steps:
From ice chest top, low-pressure vapor phase azeotrope out enters compressor boost to a；
Then b carries out gas-liquid separation by separator；
High-pressure liquid phase azeotrope after c separates enters ice chest cooling by pipeline, and the high-pressure liquid phase azeotrope after cooling is drawn from ice chest, and a part obtains low pressure liquid-phase mixing cryogen through choke valve expenditure and pressure, is again introduced into ice chest by pipeline；Another part enters the low-temperature receiver passage of condensing vaporizer described in step B by pipeline, carries out re-heat after heat exchange with the unstripped gas of step B, is exported from the evaporation side of condensing vaporizer by pipeline and draws low-pressure vapor phase azeotrope；
High pressure vapor azeotrope after d separates enters ice chest by pipeline and cools down, and draws, after choke valve expenditure and pressure, be again introduced into ice chest bottom ice chest bottom ice chest, and is converged by pipeline with the low pressure liquid-phase mixing cryogen of step c；
E low pressure liquid-phase mixing cryogen flows from bottom to top, and enter the azeotrope of ice chest with step c, d, step A enters the unstripped gas of ice chest and carries out after heat exchange by ice chest Base top contact, again enter compressor and complete a kind of refrigeration cycle stream.
The low-pressure vapor phase azeotrope that step d described in f is drawn is according to different temperatures, select or converged by pipeline with the low pressure liquid-phase mixing cryogen described in step c, or converge with the low pressure liquid-phase mixing refrigerant circuit entering ice chest described in step d, or converge with the low pressure liquid-phase mixing refrigerant circuit from ice chest Base top contact described in step e.
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Effective date of registration: 20201014 Address after: No. 16, ande Road, Dongcheng District, Beijing 100010 Patentee after: PetroChina Co.,Ltd. Address before: 610100 Sichuan city of Chengdu province Tianfu Huayang Road No. 152 days. Patentee before: Chengdu Natural Gas Chemical General Factory of Southwest Oil and Gas Field Branch, China National Petroleum Corp. |