CN105890284B - 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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- CN105890284B CN105890284B CN201610302516.0A CN201610302516A CN105890284B CN 105890284 B CN105890284 B CN 105890284B CN 201610302516 A CN201610302516 A CN 201610302516A CN 105890284 B CN105890284 B CN 105890284B
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- azeotrope
- ice chest
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- unstripped gas
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 129
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 129
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 127
- 238000000034 method Methods 0.000 title claims abstract description 40
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 28
- 239000007789 gas Substances 0.000 claims abstract description 81
- 239000007791 liquid phase Substances 0.000 claims abstract description 48
- 238000001816 cooling Methods 0.000 claims abstract description 15
- 238000005406 washing Methods 0.000 claims abstract description 11
- 239000007792 gaseous phase Substances 0.000 claims abstract description 6
- 239000002826 coolant Substances 0.000 claims abstract 9
- 210000000038 chest Anatomy 0.000 claims description 114
- 239000007788 liquid Substances 0.000 claims description 21
- 239000012808 vapor phase Substances 0.000 claims description 20
- 238000010992 reflux Methods 0.000 claims description 15
- 238000002156 mixing Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- 238000000746 purification Methods 0.000 claims description 8
- 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
- 239000012071 phase Substances 0.000 claims description 2
- 230000006835 compression Effects 0.000 claims 2
- 238000007906 compression Methods 0.000 claims 2
- 230000006837 decompression Effects 0.000 claims 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 30
- 239000003345 natural gas Substances 0.000 abstract description 15
- 238000003860 storage Methods 0.000 abstract description 10
- 238000009833 condensation Methods 0.000 abstract description 8
- 238000005516 engineering process Methods 0.000 abstract description 8
- 230000005494 condensation Effects 0.000 abstract description 7
- 239000000463 material Substances 0.000 abstract description 5
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 16
- 230000008569 process Effects 0.000 description 12
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 238000007654 immersion Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 238000005201 scrubbing Methods 0.000 description 5
- 230000006641 stabilisation Effects 0.000 description 4
- 238000011105 stabilization Methods 0.000 description 4
- 238000000605 extraction Methods 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000005457 optimization 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
- 230000008859 change Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 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
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- 230000001419 dependent effect Effects 0.000 description 1
- 230000000994 depressogenic effect Effects 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
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- 239000002904 solvent Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—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
- 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
- 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 a kind of MRC of improvement (azeotrope refrigeration) technique LNG (liquefied natural gas) de-heavy hydrocarbon apparatus and
Its method, compared with current existing LNG de-heavy hydrocarbon apparatus and its method, subtracts the invention enables de- heavy hydrocarbon process requirements equipment
Few, flow is compacter, operation difficulty reduction, and the adaptability under variable working condition or different makings is dramatically increased.
Background technology
As LNG industries are developed rapidly in recent years, gradually increased using MRC technique LNG devices.And it is natural in these devices
The removing of gas heavy hydrocarbon is a very important link, and whether also contribute to LNG devices being capable of even running.Current country MRC systems
The de- heavy hydrocarbon technique of cold technique LNG devices mainly has following several prior arts；
1st, Conventional cryogenic separating technology：
Such as Fig. 1, including azeotrope EGR, and natural gas liquefaction device, and de-heavy hydrocarbon apparatus.
After normal temperature, low-pressure vapor phase cryogen in azeotrope EGR compress through refrigerant compressor, it is divided into high pressure vapor
Cryogen and high pressure liquid phase cryogen two-way, high pressure liquid phase cryogen mix acquisition after being exchanged through heavy hydrocarbon exchanger heat with high pressure vapor cryogen
High pressure mixing cryogen enters from the top of ice chest, and with reflux azeotrope from bottom to top carries out heat exchange from top to down,
To low temperature liquid phase cryogen is obtained during ice chest bottom, azeotrope temperature is about -150 DEG C, then by valve expansion throttling, obtains more
The liquid phase azeotrope of low temperature, lower pressure, flowing from bottom to top, and high temperature azeotrope with both sides, unstripped gas enter
Row heat exchange, rises to normal temperature by ice chest Base top contact after azeotrope re-heat, compressor is entered again and completes a kind of refrigeration cycle.
Purification raw natural gas enter from ice chest top, and cold section of extraction, heavy hydrocarbon is separated by cold catch pot from ice chest
After return to ice chest continue cool down, finally obtain LNG product from ice chest bottom, and storage tank is sent to after treatment.
Heavy hydrocarbon and the high pressure liquid phase cryogen of cold catch pot bottom removing are exchanged heat and are reclaimed cold.Sent to after treatment
Storage tank.
In said apparatus start-up process, the thermograde of ice chest has a process for gradually building up.It is cold during foundation
The temperature that the unstripped gas that case middle part is drawn enters before cold catch pot can't drop to required temperature, and heavy hydrocarbon quality will be caused not conform to
The natural gas of lattice introduces the bottom of ice chest heat exchanger, and startup procedure low temperature will be caused to block risk to be increased, therefore, above-mentioned routine is low
Warm separating technology generally also needs to increase by one group of heat exchanger that goes into operation.Such as the removing weight of CN201320066196.5-LNG production equipments
Hydrocarbon device.The heat exchanger that goes into operation is located at (not shown in figure 1) before heavy hydrocarbon separator, it is ensured that cannot initial stage ice chest top is driven
When providing cold, unstripped gas cools to one 60 DEG C or so by the heat exchanger that goes into operation, then by cold catch pot that heavy hydrocarbon is cold again
Separated from unstripped gas after solidifying.
2nd, with the heavy hydrocarbon separating technology of washing：
Such as Fig. 2, azeotrope EGR is compared with technology 1.
Purification raw natural gas lead to heavy hydrocarbon scrubbing tower from ice chest precooling zone, in returning to ice chest after washing cold section it is cold
But ice chest continuation cooling, then after leading to heavy hydrocarbon return tank separation heavy hydrocarbon is returned to, finally LNG product is obtained from ice chest bottom, and
Storage tank is sent to after treatment.
The heavy hydrocarbon for from heavy hydrocarbon return tank separate is squeezed into heavy hydrocarbon scrubbing tower and is washed by heavy hydrocarbon reflux pump, heavy hydrocarbon washing
Heavy hydrocarbon and the high pressure liquid phase cryogen of tower bottom removing are exchanged heat and are reclaimed cold.Storage tank is sent to after treatment.
3rd, normal temperature washing process：Such as Fig. 3, it is solvent that the technique typically uses isopentane, under normal temperature or slightly below normal temperature,
By the similar principle that mixes of isopentane, isopentane flows from the top down in heavy hydrocarbon scrubbing tower, and natural gas flows from bottom to top, passes through
Contact of the natural gas with isopentane and perforated space are exchanged and deviate from the heavy hydrocarbon of natural gas, and the isopentane being rich in more than heavy hydrocarbon directly goes
Storage tank is stored.Heavy hydrocarbon and the isopentane of heavy hydrocarbon scrubbing tower bottom removing are exchanged heat and are reclaimed cold.Storage tank is sent to after treatment.
The shortcoming of above-mentioned prior art is：
Prior art 1 is simple low temperature separating process, and heavy hydrocarbon is separated at low temperature using separator, and device technique is not
Possible absolute stability, by raw natural gas change of component, and azeotrope the influence of component and height pressure difference, make into point
When increasing from the temperature of charge increase of device or pressure, original is dissolved in the restructuring such as benzene, hexamethylene, pungent pentane in the liquid phase of separator
Branch flashes off, and causes the variation of separating effect, is blocked so as to easily cause ice chest low temperature.The de- heavy hydrocarbon result of different temperatures is shown in
Fig. 5.
Secondly, the increased heat exchanger that goes into operation only is used in the stage of going into operation, and is again that the idleness of equipment is wasted in normal operating phase,
Shortage is acted on.
Prior art 2 is to increase the dynamic equipment such as heavy hydrocarbon pump using Conventional cryogenic washing process, increase operation complexity and
Energy ezpenditure, increases the complexity of system.Limited by the performance of pump, so that the adaptability of limits device heavy hydrocarbon.
The normal temperature isopentane washing process of prior art 3 increases the consumption of isopentane, increased the operating cost of device.
The content of the invention
Present invention aim at：There is provided the liquefaction that a kind of process is simple, equipment are few, flow is compact, operation difficulty is low natural
Qi exhaustion heavy hydrocarbon apparatus and method, using apparatus and method of the present invention, the adaptability under variable working condition or different makings is dramatically increased.
A kind of liquefied natural gas de-heavy hydrocarbon apparatus that the present invention is used, including azeotrope EGR, ice chest, low temperature point
From device, heavy hydrocarbon heat exchanger, and the intake pipeline of unstripped gas first being connected with ice chest, the top of cold catch pot sets one and condenses
Evaporator, cold catch pot constitutes knockout tower with condenser/evaporator；The unstripped gas exit on ice chest top passes through unstripped gas second
Intake pipeline connects the entrance of condenser/evaporator, and the gaseous phase outlet of condenser/evaporator connects cold by the intake pipeline of unstripped gas the 3rd
The unstripped gas arrival end of lower box part；
The liquid-phase outlet of the condenser/evaporator connects the entrance of cold catch pot by reflux pipeline.
Using said apparatus of the invention, by increasing condenser/evaporator, the heavy hydrocarbon removing of unstripped gas is realized, after removing
Heavy hydrocarbon cold catch pot is back to by reflux pipeline, carry out heavy hydrocarbon itself backflow washing, effectively depart from heavy hydrocarbon, and remove
Benzene that may be present, hexamethylene etc. easily block material, it is ensured that the removal effect of heavy hydrocarbon.When operating mode changes, make from ice chest
When the unstripped gas temperature of middle extraction changes, condenser/evaporator (is controlled by adjusting the flow of low-temperature receiver medium (azeotrope)
The liquid level of azeotrope), the cold of heat exchange, the heavy hydrocarbon backflow temperature of gas-liquid separation removing can be carried out with adjust automatically and unstripped gas
Degree can easily be controlled and adjusted, so that it is guaranteed that heavy hydrocarbon enters the stabilization of the heavy hydrocarbon reflux temperature of cold catch pot, be changed automatically
Kind heavy hydrocarbon abjection effect.
Particularly gone into operation the stage in device, when the unstripped gas temperature or normal temperature extracted out from ice chest, suitably increase low-temperature receiver
The flow of medium, condenser/evaporator serves the effect of the heat exchanger that goes into operation, with routinely going into operation compared with heat exchanger, due to will heat exchange from
It is changed into after knockout tower before entering separator, the independent condenser/evaporator can be made in addition to the effect for going into operation heat exchanger is played, also
The effect of the overhead condenser brought into normal play.
After device progresses into normal production, the condenser/evaporator of azeotrope stabilization liquid level is kept to provide stabilization low temperature
Source, when feed gas composition or technological parameter (unstripped gas temperature) fluctuate, heavy hydrocarbon is by immersion condenser/evaporator
The adjustment of azeotrope liquid level, it is ensured that the chilling temperature needed for unstripped gas removing heavy hydrocarbon, it is ensured that from knockout tower raw material out
Gas is pure, is not blocked into ice chest bottom.
Condenser/evaporator is recommended to take the structure of intrusive mood condenser/evaporator, and condenser is made using plate-fin heat exchanger,
Equipment size and weight can be effectively reduced, is easy to the system integration.
Further improvement is that the intake pipeline of the unstripped gas first is also changed by the intake pipeline of unstripped gas the 5th with heavy hydrocarbon
The arrival end connection of hot device, the port of export of heavy hydrocarbon heat exchanger connects the input pipe of unstripped gas second by the intake pipeline of unstripped gas the 6th
Line.
Heavy hydrocarbon exchanges heat with unstripped gas rather than is exchanged heat with liquid refrigerant, is either driven or product flow exception in device cold conditions
In the case of fluctuation, all on the no influence of stabilization heat exchange of heavy hydrocarbon, with conventional liq cryogen compared with the heat exchange of separator bottom heavy hydrocarbon,
Can guarantee that heavy hydrocarbon re-heat is good, downstream process equipment does not have brittle fracture under low temperature risk, is also beneficial to effective recovery of heavy hydrocarbon cold, it is existing
There is technology, when start-up is without liquid phase cryogen, heavy hydrocarbon cannot exchange heat, and can only abandon the recovery of heavy hydrocarbon.Particularly when heat exchanger makes
With plate type heat exchanger, it is easy to integrated with ice chest, heat exchanger is shorter with knockout tower connecting line, and device is compacter.
Further improvement is that the separator liquid-phase outlet in the azeotrope EGR passes through azeotrope second
Intake pipeline connection ice chest top, and passed from the high pressure liquid phase cryogen exit from ice chest middle part side by pipeline, pass through
First throttle valve, is again introduced into ice chest bottom and is connected with the intake pipeline of azeotrope the 6th；Separator gaseous phase outlet is by mixing
The intake pipeline of cryogen the 3rd connection ice chest top, and passed from ice chest bottom by pipeline, by second throttle, by mixing
The intake pipeline of cryogen the 5th is again introduced into ice chest and is connected with the intake pipeline of azeotrope the 6th from ice chest bottom；Azeotrope
Six intake pipelines are passed from ice chest top and connect compressor by the intake pipeline of azeotrope first；Ice chest middle part side high pressure liquid
Phase cryogen exit also connects the low-temperature receiver entrance of condenser/evaporator, the steaming of condenser/evaporator by the intake pipeline of azeotrope the 7th
Hair side outlet connects reflux azeotrope intake pipeline by the intake pipeline of azeotrope the 8th；The reflux azeotrope input
Pipeline includes the intake pipeline of azeotrope the 5th, the intake pipeline of azeotrope the 6th, the intake pipeline of azeotrope first.
Low-pressure vapor phase azeotrope from evaporation side out after, can according under different working temperatures select enter reflux mix it is cold
The diverse location of agent intake pipeline, effectively to reclaim cold.
Used as the replacement of apparatus of the present invention, above-mentioned separator liquid-phase outlet connects condensation and steams by azeotrope intake pipeline
Send out the low-temperature receiver entrance of device.
Present invention additionally comprises a kind of de- heavy hydrocarbon method of liquefied natural gas, including azeotrope circulation stream；With unstripped gas
Liquefaction stream, specifically includes following steps：
A purification unstripped gas enters ice chest, is extracted out from the unstripped gas exit on ice chest top；
The unstripped gas that B is extracted out enters the condensing evaporator on knockout tower top, carries out gas-liquid separation removing heavy hydrocarbon；
The heavy hydrocarbon that C from unstripped gas separate enters separation from the liquid-phase outlet of condensing evaporator by the heavy hydrocarbon pipeline that flows back
The cold catch pot of tower bottom is washed；
Heavy hydrocarbon after D washings is extracted out from cold catch pot bottom, and after reclaiming cold through the heat exchange of heavy hydrocarbon heat exchanger, pipeline draws
Go out.
Further improving is, the purification unstripped gas of the step A also enters the cooling of heavy hydrocarbon heat exchanger by pipeline
Passage, the heavy hydrocarbon heat exchange obtained with step D, is absorbed the unstripped gas after cold and is drawn with step A ice chests top unstripped gas by pipeline
Go out the unstripped gas mixing extracted out at end.
Further improving is, the azeotrope circulation stream comprises the following steps：
Low-pressure vapor phase azeotropes of a from ice chest top out enters compressor boost；
Then b carries out gas-liquid separation by separator；
High pressure liquid after c is separated mixes cryogen by pipeline into ice chest cooling, and the high pressure liquid after cooling mixes cold
Agent is drawn from ice chest, and a part obtains low pressure liquid phase azeotrope through choke valve expenditure and pressure, and ice chest is again introduced into by pipeline；
Another part enters the low-temperature receiver passage of the condensing evaporator described in step B by pipeline, and the unstripped gas with step B carries out hot friendship
Rear re-heat is changed, low-pressure vapor phase azeotrope is drawn from the evaporation side outlet of condensing evaporator by pipeline；
High pressure vapor azeotrope after d is separated is cooled down by pipeline into ice chest, is drawn from ice chest bottom, through choke valve
After expenditure and pressure, ice chest is again introduced into from ice chest bottom, and converge by pipeline with the low pressure liquid phase azeotrope of step c；
E low pressure liquid phase azeotropes flow from bottom to top, and enter azeotrope, the step A entrance of ice chest with step c, d
The unstripped gas of ice chest is carried out after heat exchange by ice chest Base top contact, compressor is entered again and completes a kind of refrigeration cycle stream.
The low-pressure vapor phase azeotrope that step d described in f draws according to different temperatures, selection or with the low pressure described in step c
Liquid phase azeotrope is converged by pipeline, or is converged with the low pressure liquid phase azeotrope pipeline of the entrance ice chest described in step d, or
With converging from the low pressure liquid phase azeotrope pipeline of ice chest Base top contact described in step e.
Brief description of the drawings
The present invention by embodiment and with reference to Figure of description by 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 process chart of the invention.
Fig. 5 is the Comparative result that different temperatures unstripped gas takes off heavy hydrocarbon in separator.
Specific embodiment
All features disclosed in this specification, or disclosed all methods or during the step of, except mutually exclusive
Feature and/or step beyond, can combine by any way.This specification (including any accessory claim, summary and
Accompanying drawing) disclosed in any feature, unless specifically stated otherwise, can alternative features equivalent by other or with similar purpose be subject to
Replace.I.e., unless specifically stated otherwise, each feature is an example in a series of equivalent or similar characteristics.
A kind of embodiment of the present invention MRC liquefied natural gas de-heavy hydrocarbon apparatus as shown in Figure 4, including azeotrope circulation dress
Put, ice chest 1, cold catch pot 2 and the condenser/evaporator at the top of it 3 composition knockout tower, heavy hydrocarbon heat exchanger 4, said apparatus with
Connecting line forms the liquefaction stream of azeotrope circulation stream and unstripped gas.
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, and -50 are cooled to by ice chest
DEG C -- 70 DEG C, extracted out from the unstripped gas exit on ice chest top；
It should be noted that going into operation the stage, the unstripped gas extracted out from the unstripped gas exit of ice chest is normal temperature.
B, unstripped gas enter the condensing evaporator on knockout tower top by the second intake pipeline of unstripped gas NG-2, in condensation
Condensed after evaporator and azeotrope heat exchange, realize that gas-liquid separation removes heavy hydrocarbon, the condensed formula of unstripped gas after removing heavy hydrocarbon is steamed
The gaseous phase outlet for sending out device is again introduced into ice chest lower feed gas arrival end by the intake pipeline NG-3 of unstripped gas the 3rd, in ice chest
Continue to cool down, liquefy, drawn by the 4th intake pipeline NG-4 in ice chest bottom, obtain the LNG that temperature is -155 DEG C or so and produce
Product, LNG storage tank is gone after being throttled through the 3rd choke valve V3.
Go into operation the stage, the appropriate flow for increasing condenser/evaporator low-temperature receiver medium such as increases the liquid level of azeotrope, and it is right to realize
The heavy hydrocarbon removing of normal temperature purification unstripped gas.
The heavy hydrocarbon in C, step B separate enters knockout tower from the liquid-phase outlet of condensing evaporator by the heavy hydrocarbon pipeline that flows back
The cold catch pot of bottom is washed；Cold catch pot pressure general control is in 3-4MPa；
D, the heavy hydrocarbon Cx from after the extraction washing of cold catch pot bottom, after reclaiming cold through the heat exchange of heavy hydrocarbon heat exchanger, pipeline
Lead to heavy hydrocarbon storage tank.
Used as the optimization design of apparatus of the present invention, condenser/evaporator is recommended to take the structure of intrusive mood condenser/evaporator, adopts
Make condenser with plate-fin heat exchanger.
Used as the optimization design of apparatus of the present invention, step A unstripped gas divides one by the intake pipeline NG-5 of unstripped gas the 5th
Stream is connected with the cooling duct arrival end of heavy hydrocarbon heat exchanger, the heavy hydrocarbon heat exchange obtained with step D in heavy hydrocarbon heat exchanger, absorbs cold
The original that shunting unstripped gas after amount is extracted out by the intake pipeline NG-6 of unstripped gas the 6th with step A ice chests top unstripped gas exit
Material gas converges.
Used as the optimization design of apparatus of the present invention, the azeotrope circulation stream comprises the following steps：
Low-pressure vapor phase azeotrope MR-1s of a from ice chest top out enters back into compressor 4 and is pressurized into surge tank 6；
Then b carries out gas-liquid separation by separator 5；
It is cold into ice chest by pipeline from separator liquid-phase outlet that high pressure liquid after step c b separation mixes cryogen MR-2
But to -50 DEG C -- 70 DEG C, the high pressure liquid after cooling mixes cryogen and is drawn from ice chest, and a part subtracts through first throttle valve V1 throttlings
It is depressed into 0.3MPa and obtains low pressure liquid phase azeotrope MR-3, ice chest is again introduced into by pipeline；Another part high pressure liquid is mixed
Cryogen MR-7 enters the low-temperature receiver passage of condensing evaporator by the 4th choke valve V4 expenditure and pressures, and the unstripped gas with step B enters
Re-heat after row heat exchange, low-pressure vapor phase azeotrope MR-8 is drawn by pipeline from the evaporation side outlet of condensing evaporator；
High pressure vapor azeotrope MR-3 after Step d b is separated is cold into ice chest by pipeline from separator gaseous phase outlet
But to -150 DEG C to -155 DEG C, drawn from ice chest bottom, obtained after second throttle V2 expenditure and pressures expenditure and pressure to 0.4MPa
Low pressure liquid phase azeotrope MR-5, be again introduced into ice chest from ice chest bottom, and with the low pressure liquid phase azeotrope of step c cold
Acquisition low-pressure vapor phase azeotrope MR-6 is converged by pipeline in case；
Low pressure liquid phase azeotrope in e ice chests flows from bottom to top, and enters the azeotrope of ice chest with step c, d
MR-2, MR-3, step A carry out heat exchange into the unstripped gas of ice chest, and obtaining low-pressure vapor phase by ice chest Base top contact after re-heat mixes
Cryogen MR-1 is closed, is entered compressor again by surge tank and is completed a kind of refrigeration cycle stream.
The low-pressure vapor phase azeotrope MR-8 that step c described in f draws according to different temperatures, selection or with described in step c
Low pressure liquid phase azeotrope is converged by pipeline 1B, or is passed through with the low pressure liquid phase azeotrope of the entrance ice chest described in step d
Pipeline 1C converges, or with being converged by pipeline 1A from the low-pressure vapor phase azeotrope of ice chest Base top contact described in step e.So as to
It is effective to reclaim flow.
By technical scheme, MRC technique LNG devices are only by increased compact immersion condensation evaporation
Device and the trickle change of technological process, but make whole technique reduce heavy hydrocarbon return tank, heavy hydrocarbon scrubbing tower, low temperature heavy hydrocarbon pump, open
The equipment such as work heat exchanger, substantially reduce technological process, improve the stability and operability of device.Have the characteristics that：
1 takes off heavy hydrocarbon using the ingenious MRC technique LNG devices that are used in of combination of immersion condenser/evaporator and cold catch pot
In technique, flowing back certainly for heavy hydrocarbon, stable heavy hydrocarbon effect are realized；
2 the immersion condenser/evaporator is in the stage of going into operation as going into operation heat exchanger simultaneously, and it is cold to make tower top in normal production
Condenser；
The heavy hydrocarbon of 3 separator bottoms with carry out entering hydrocarbon mixture storage tank after re-heat heat exchange with partial raw gas, and after cooling down
Natural gas enter heavy hydrocarbon separator before.
The technique compared with the prior art, using the technique of itself condensing reflux of the heavy hydrocarbon in natural gas, with system from
Regulatory function is strong, strong adaptability；Heavy hydrocarbon reflux pump, heavy hydrocarbon reflux accumulator etc. are reduced simultaneously, investment is advantageously reduced, and increase
System operability；Flowed back by heavy hydrocarbon and washed, increase the control of the heavy hydrocarbons content to the natural gas into ice chest bottom, had
Beneficial to the stability for improving operation.It is more and need the situation of de- heavy hydrocarbon that the technique is particularly adapted to heavy hydrocarbons content in natural gas.
Above-mentioned steps c leads to also dependent on the cooling that actual conditions draw high pressure liquid phase cryogen MR-2 to immersion condenser/evaporator
Road, for condenser/evaporator provides low-temperature receiver.
Although having carried out example and description to the present invention according to preferred embodiment, it is to be understood that the present invention is not
It is confined to foregoing specific embodiment.Illustrated in without departing substantially from claims it is of the invention in the case of, can to this work
Go out alterations and modifications, the present invention expands to any new feature for disclosing in this manual or any new combination, and discloses
Any new method or process the step of or any new combination.
Claims (8)
1. a kind of liquefied natural gas de-heavy hydrocarbon apparatus, including azeotrope EGR, ice chest, cold catch pot, heavy hydrocarbon heat exchange
Device, and the intake pipeline of unstripped gas first being connected with ice chest；
The azeotrope EGR includes ice chest low-pressure vapor phase azeotrope passage, and refrigerant compressor, separator, heavy hydrocarbon is changed
Hot device high pressure liquid mixes coolant channel, ice chest high pressure mixing coolant channel, choke valve；Ice chest low-pressure vapor phase azeotrope passage
Outlet is connected by pipeline with refrigerant compressor, and refrigerant compressor connects separator by pipeline, and separator is distinguished by pipeline
Connection heavy hydrocarbon heat exchanger high-voltage liquid phase azeotrope passage and ice chest high pressure mixing coolant channel, heavy hydrocarbon heat exchanger high-voltage liquid phase are mixed
Close coolant channel connection ice chest high pressure mixing coolant channel；Ice chest high pressure mixing coolant channel connects choke valve, choke valve connection
Ice chest low-pressure vapor phase azeotrope feeder connection；
It is characterized in that：
The top of cold catch pot sets a condenser/evaporator, and cold catch pot constitutes knockout tower with condenser/evaporator；On ice chest
The unstripped gas exit in portion connects the entrance of condenser/evaporator by the intake pipeline of unstripped gas second, and the gas phase of condenser/evaporator goes out
Mouth connects the unstripped gas arrival end of ice chest bottom by the intake pipeline of unstripped gas the 3rd；
The liquid-phase outlet of the condenser/evaporator connects the entrance of cold catch pot by reflux pipeline.
2. MRC liquefied natural gas de-heavy hydrocarbon apparatus according to claim 1, it is characterised in that：The unstripped gas first is defeated
Enter pipeline to be also connected with the arrival end of heavy hydrocarbon heat exchanger by the intake pipeline of unstripped gas the 5th, the port of export of heavy hydrocarbon heat exchanger passes through
The intake pipeline of unstripped gas the 6th connects the intake pipeline of unstripped gas second.
3. liquefied natural gas de-heavy hydrocarbon apparatus according to claim 1 and 2, it is characterised in that：The azeotrope circulation
Separator liquid-phase outlet in device connects ice chest top by the intake pipeline of azeotrope second, and by pipeline from from ice chest
The high pressure liquid phase cryogen exit of middle part side is passed, and by first throttle valve, is again introduced into ice chest bottom and azeotrope the
Six intake pipelines are connected；
Separator gaseous phase outlet connects ice chest top by the intake pipeline of azeotrope the 3rd, and is worn from ice chest bottom by pipeline
Go out, by second throttle, ice chest and and azeotrope are again introduced into from ice chest bottom by the intake pipeline of azeotrope the 5th
6th intake pipeline is connected；
The intake pipeline of azeotrope the 6th is passed from ice chest top and connects compressor by the intake pipeline of azeotrope first；
Ice chest middle part side high pressure liquid phase cryogen exit also connects condenser/evaporator by the intake pipeline of azeotrope the 7th
Low-temperature receiver entrance, the evaporation side outlet of condenser/evaporator connects reflux azeotrope input pipe by the intake pipeline of azeotrope the 8th
Line；
The reflux azeotrope intake pipeline includes the intake pipeline of azeotrope the 5th, the intake pipeline of azeotrope the 6th, mixes
Close the intake pipeline of cryogen first.
4. liquefied natural gas de-heavy hydrocarbon apparatus according to claim 3, it is characterised in that：Separator liquid-phase outlet is by mixed
Close the low-temperature receiver entrance that cryogen intake pipeline connects condenser/evaporator.
5. liquefied natural gas de-heavy hydrocarbon apparatus according to claim 3, it is characterised in that：The condenser/evaporator is intrusion
Formula condenser/evaporator.
6. a kind of de- heavy hydrocarbon method of liquefied natural gas, including azeotrope circulation stream, specifically includes following steps：
Normal temperature, the low-pressure vapor phase cryogen that ice chest low-pressure vapor phase azeotrope channel outlet from the top of ice chest is obtained are through cryogen compression
After machine compression, high pressure vapor cryogen and high pressure liquid phase cryogen two-way are divided into by separator, high pressure liquid phase cryogen is through heavy hydrocarbon heat exchanger
High pressure liquid is mixed and mixes acquisition high pressure mixing cryogen after coolant channel is exchanged with heavy hydrocarbon exchanger heat with high pressure vapor cryogen, so
Enter ice chest high pressure mixing coolant channel from the top of ice chest afterwards, and enter with reflux azeotrope from bottom to top from top to down
Row heat exchange, to low temperature liquid phase cryogen is obtained during ice chest bottom, azeotrope temperature is about -150 DEG C, then is expanded by choke valve
Throttling, obtains lower temperature, the liquid phase azeotrope of lower pressure, enters into ice chest low-pressure vapor phase azeotrope passage from bottom
Mouthful, flowing from bottom to top, and high temperature azeotrope with both sides, unstripped gas carry out heat exchange, are risen to after azeotrope re-heat
Normal temperature is entered compressor and is completed a kind of refrigeration cycle again by ice chest Base top contact；
Characterized in that, also including the liquefaction stream of unstripped gas, following steps are specifically included：
A purification unstripped gas enters ice chest, is extracted out from the unstripped gas exit on ice chest top；
The unstripped gas that B is extracted out enters the condensing evaporator on knockout tower top, carries out gas-liquid separation removing heavy hydrocarbon；
The heavy hydrocarbon that C from unstripped gas separate is entered under knockout tower from the liquid-phase outlet of condensing evaporator by the heavy hydrocarbon pipeline that flows back
The cold catch pot in portion is washed；
Heavy hydrocarbon after D washings is extracted out from cold catch pot bottom, and after reclaiming cold through the heat exchange of heavy hydrocarbon heat exchanger, pipeline is drawn.
7. a kind of liquefied natural gas as claimed in claim 6 takes off heavy hydrocarbon method, it is characterised in that：
The purification unstripped gas of the step A also enters the cooling duct of heavy hydrocarbon heat exchanger, the heavy hydrocarbon obtained with step D by pipeline
Heat exchange, is absorbed the unstripped gas after cold and is mixed by the unstripped gas that pipeline is extracted out with step A ice chests top unstripped gas exit.
8. a kind of liquefied natural gas as claimed in claims 6 or 7 takes off heavy hydrocarbon method, it is characterised in that：The azeotrope is followed
Circulation road comprises the following steps：
Low-pressure vapor phase azeotropes of a from ice chest top out enters compressor boost；
Then b carries out gas-liquid separation by separator；
C separate after high pressure liquid mix cryogen by pipeline into ice chest cool down, the high pressure liquid after cooling mix cryogen from
Ice chest is drawn, and a part obtains low pressure liquid phase azeotrope through choke valve expenditure and pressure, and ice chest is again introduced into by pipeline；It is another
Part enters the low-temperature receiver passage of the condensing evaporator described in step B by pipeline, after carrying out heat exchange with the unstripped gas of step B
Re-heat, low-pressure vapor phase azeotrope is drawn by pipeline from the evaporation side outlet of condensing evaporator；
High pressure vapor azeotrope after d is separated is cooled down by pipeline into ice chest, is drawn from ice chest bottom, is throttled through choke valve
After decompression, ice chest is again introduced into from ice chest bottom, and converge by pipeline with the low pressure liquid phase azeotrope of step c；
E low pressure liquid phase azeotropes flow from bottom to top, and enter the azeotrope of ice chest, step A with step c, d and enter ice chest
Unstripped gas carry out after heat exchange by ice chest Base top contact, compressor is entered again and completes a kind of refrigeration cycle stream；
The low-pressure vapor phase azeotrope that step d described in f draws according to different temperatures, selection or with the low pressure liquid phase described in step c
Azeotrope is converged by pipeline, or is converged with the low pressure liquid phase azeotrope pipeline of the entrance ice chest described in step d, or with step
Converging from the low pressure liquid phase azeotrope pipeline of ice chest Base top contact described in rapid e.
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Effective date of registration: 20201014 Address after: No. 16, ande Road, Dongcheng District, Beijing 100010 Patentee after: PetroChina Company Limited Address before: 610100 Sichuan city of Chengdu province Tianfu Huayang Road No. 152 days. Patentee before: PetroChina Company Limited |