CN105135820B - LNG method and system is produced using gas containing air - Google Patents
LNG method and system is produced using gas containing air Download PDFInfo
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- CN105135820B CN105135820B CN201510603093.1A CN201510603093A CN105135820B CN 105135820 B CN105135820 B CN 105135820B CN 201510603093 A CN201510603093 A CN 201510603093A CN 105135820 B CN105135820 B CN 105135820B
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/18—External refrigeration with incorporated cascade loop
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
Abstract
The utilization gas containing air of the present invention produces LNG method and system, wherein system includes main flow system and refrigeration system, main flow system includes feed gas compressor, water cooler, clean unit, pre-cooling unit, drying unit, main heat exchanger and rectifying column, the bottom of towe of rectifying column is provided with reboiler and condensate outlet, the tower top of rectifying column is provided with overhead separator and nitrogen oxygen offgas outlet, and refrigeration system includes the azeotrope circulatory system and nitrogen cycle system.The method of the present invention includes：A main flows technique, B azeotropes circulation technology, C nitrogen cycle techniques.While the method and system that the utilization gas containing air of the present invention produces LNG can independently adjust gas product and yield, by setting pre-cooling unit member to reduce the power consumption more than 5% of whole technological process, reduce outside tower top oxygen content to explosion limit, it is ensured that the stable safe operation of system.
Description
Technical field
The present invention relates to liquefied natural gas industry, more particularly to it is a kind of using gas containing air produce LNG method with
And system.
Background technology
Liquefied natural gas (abbreviation LNG) is that natural gas (abbreviation NG) is compressed, be cooled to its boiling point (- 161.5 DEG C or so,
With component about) liquified natural gas that is formed afterwards, main component is methane.Its volume is about the 1/ of same amount gaseous natural gas volume
625, its colourless, tasteless, nontoxic and non-corrosiveness is widely used in the row such as petrochemical industry, electric power, gas and Automobile Transportation
Industry.Using LNG as clean energy resource, with obvious environmental benefit and social benefit.Can be reduced after LNG substitution fuel oils
90% sulfur dioxide (SO2) emissions and 80% discharged nitrous oxides, environmental benefit are fairly obvious.
CNG is that compressed natural gas (Compressed Natural Gas, abbreviation CNG) is that natural gas is pressurizeed and stored up with gaseous state
Deposit what is formed in a reservoir.Compressed natural gas can be formed by the natural gas in oil field and gas field is compressed.
Gas is the gas that extraction has been carried out in the case where having carried out the mine of coal mining, also referred to as coal bed gas.This mode is taken out
The mash gas methane content that extraction comes is relatively low, generally between 30%~70%.Methane is clear energy sources and the industrial chemicals of high-quality,
Separating-purifying methane has great importance for extending and improving the effective of gas using with economic value from gas.China
The gas place of production disperses, and well yield is low, and methane concentration is low and oxygen-containing in the gas of most of exploitation, is easily produced in processing procedure
Raw blast, it is necessary to have safely, the technology of being economically separated fully could utilize rationally.
A variety of technologies that preparing natural gas is purified in low concentration gas are occurred in that at present.Such as Publication No.
CN101922850A and CN101929788A patent individually discloses a kind of utilization gas containing air and produces liquefied natural gas
Method and the device that liquefied natural gas is produced using gas containing air, this method and device use answering for azeotrope itself
SAPMAC method is folded, the raw material after purification is liquefied and separated, LNG product is obtained.There are some shortcomings in above-mentioned prior art：Unstripped gas
Middle methane content fluctuation is larger, the stable operation of unavoidable influence liquefaction process, circulates in device using MRC cascade refrigerations and adjusted
The requirement of product purity and the rate of recovery can not be met in journey simultaneously；After cleaning, temperature, pressure is higher for gas containing air, containing full
Larger with water, drying unit energy consumption is higher.
The content of the invention
While can independently adjusting gas product and yield it is an object of the invention to provide one kind, whole technique is reduced
The power consumption of flow, it is ensured that the utilization gas containing air of the stable safe operation of system produces LNG method and system.
The system that the utilization gas containing air of the present invention produces LNG, including main flow system and refrigeration system, the main flow
Journey system includes filter along unstripped gas flow direction successively, feed gas compressor, water cooler, clean unit, pre-cooling unit, dry
Dry unit, main heat exchanger and rectifying column, the bottom of towe of the rectifying column are provided with reboiler and condensate outlet, the rectifying column
Tower top be provided with overhead separator and nitrogen oxygen offgas outlet, the refrigeration system includes being used to provide cold for main heat exchanger
And provide the azeotrope circulatory system of heat for reboiler and the nitrogen cycle system of cold is provided for rectifying column, so that rectifying
The portion of methane in unstripped gas in tower is condensed into liquid and discharged from condensate outlet, the methane and nitrogen oxygen tail gas in unstripped gas from
Nitrogen oxygen offgas outlet is discharged.
The system that the utilization gas containing air of the present invention produces LNG, wherein, the azeotrope circulatory system is cold along mixing
Agent flow direction includes azeotrope compensator, for the mixing of the azeotrope compression exported to azeotrope compensator successively
Refrigerant compressor, cooler, gas-liquid separator, the gas phase azeotrope outlet of the gas-liquid separator pass through the first pipeline connection
In the gas phase azeotrope entrance of the reboiler, the gas phase azeotrope outlet of the reboiler passes through the second pipeline and first
Choke valve is connected, and the gas phase azeotrope provides heat, the liquid phase azeotrope outlet of the gas-liquid separator for reboiler
Connected by the 3rd pipeline with second throttle, the mixing after the cooling that throttled respectively by the first throttle valve, second throttle
Cryogen is back to azeotrope compensator after converging by the 4th pipeline, and the azeotrope is in azeotrope compressor with mixing
Circulated between cryogen compensator, the first pipeline, the second pipeline, the 3rd pipeline, the 4th pipeline are respectively through the main heat exchanger, institute
The azeotrope stated in the first pipeline, the 3rd pipeline is cooled down in the main heat exchanger, in second pipeline, the 4th pipeline
Azeotrope provides cold in the main heat exchanger.
The system that the utilization gas containing air of the present invention produces LNG, wherein, stream of the nitrogen cycle system along nitrogen cooling agent
Dynamic direction includes nitrogen balance tank successively, the nitrogen compressor compressed for the nitrogen that export to nitrogen balance tank, cold to nitrogen
But nitrogen cooler, for making nitrogen throttling cooling be the 3rd choke valve of liquid nitrogen, the nitrogen cooler is connected by the 5th pipeline
Lead to the 3rd choke valve, the outlet of the 3rd choke valve is in the nitrogen entrance of the rectifying column, the nitrogen of the rectifying column
Outlet, in the entrance of the nitrogen balance tank, is turned by the 6th pipeline connection so that liquid nitrogen is provided in the rectifying column after cold
It is changed into nitrogen and nitrogen balance tank is back to by the 6th pipeline, the 5th pipeline, the 6th pipeline is respectively through the main heat exchanger, institute
State the nitrogen in the 5th pipeline to cool down in the main heat exchanger, the nitrogen in the 6th pipeline is carried in the main heat exchanger
Semen donors.
The system that the utilization gas containing air of the present invention produces LNG, wherein, it is provided with the 6th pipeline for removing oxygen
Nitrogen clean unit, the nitrogen clean unit is located between the main heat exchanger and nitrogen balance tank.
The system that the utilization gas containing air of the present invention produces LNG, wherein, nitrogen oxygen offgas outlet passes through the 7th pipeline connection
The overhead separator, the overhead separator is by pipeline connection expanding machine, and the expanding machine, which expands nitrogen oxygen tail gas, to cool
Nitrogen oxygen tail gas is discharged by the 8th pipeline afterwards, the 8th pipeline sequentially passes through subcooler, main heat exchanger by the expanding machine,
So that the nitrogen oxygen tail gas in the 8th pipeline provides cold and is warming up to normal temperature.
The system that the utilization gas containing air of the present invention produces LNG, wherein, the condensate outlet and the 9th pipeline connect
Logical, the 9th pipeline passes through the subcooler, so as to be condensed into the methane cooling of liquid in the 9th pipeline, forms LNG.
The system that the utilization gas containing air of the present invention produces LNG, wherein, condensate outlet and the tenth pipeline connection, the
Ten pipelines pass through main heat exchanger, so as to be condensed into the methane rewarming gasification of liquid in the tenth pipeline, form CNG.
The method that the utilization gas containing air of the present invention produces LNG, including：
A main flow techniques：By unstripped gas after filtering, compression, purification, water cooling, 35~45 DEG C are obtained, absolute pressure is
0.5~0.7MPa, the unstripped gas containing saturation water is cooled to after 3~7 DEG C and dried, makes unstripped gas depoint depression again to unstripped gas
To -50~-70 DEG C；Dried unstripped gas is exchanged heat by main heat exchanger to cool, and the formation gas-liquid two after choke valve throttles
The gas-liquid mixture of phase, gas-liquid mixture enters rectifying column in the middle part of rectifying column, and liquid phase is downwardly towards bottom of towe, passes through rectifying tower
The reboiler heating evaporation at bottom flows out after going out the nitrogen oxygen tail gas of carrying from condensate outlet, obtains the LNG of methane concentration >=99%,
Gas phase in gas-liquid mixture flows upwardly toward rectifying column tower top, after the liquid nitrogen with rectifying column tower top is sufficiently mixed cooling, gas phase
In the methane liquefaction condensation that contains flow to bottom of towe, a part of nitrogen is extracted out from tower top, net by nitrogen after main heat exchanger rewarming
Nitrogen balance tank is returned to after changing unit deoxygenation, remaining nitrogen oxygen tail gas sequentially passes through supercooling after expander cools
Device, main heat exchanger re-heat to normal temperature；
B azeotrope circulation technologies：It is gas-liquid two that azeotrope enters gas-liquid separator separates after overcompression, cooling
Phase, gas phase is cooled by main heat exchanger, and the liquid phase of the gas-liquid mixture at rectifying tower bottom is heated into reboiler, and itself is cooled
To -135~-155 DEG C, -150~-170 DEG C then are cooled to by first throttle valve throttling, liquid phase is formed, passed sequentially through master and change
Hot device is exported after the part that the liquid phase in cold, azeotrope passes through main heat exchanger from main heat exchanger extraction, azeotrope
Liquid phase after main heat exchanger cools by second throttle throttle cool, with by first throttle valve throttle cooling liquid phase mix
After closing cryogen mixing azeotrope compensator is back into main heat exchanger rewarming；
C nitrogen cycle techniques：Nitrogen in nitrogen balance tank passes through after nitrogen compressor is compressed to 3.2~3.5MPa
Main heat exchanger cool, after being throttled by choke valve turn into liquid nitrogen enter rectifying column in, with the gas mixing after tower top rectifying there is provided
Cold needed for rectifying, condenses out the methane of tower top, while oxygen concentration is reduced to outside explosion limit, liquid nitrogen fully exchanges heat
Turn into nitrogen afterwards and then from overhead reflux, nitrogen balance tank is returned after main heat exchanger rewarming, nitrogen clean unit deoxygenation.
The utilization gas containing air of the present invention produces LNG method and system, can independently adjust gas product and
While yield, by setting filter, water cooler, clean unit, pre-cooling unit, drying unit to reduce whole technological process
Power consumption, while rectifying column tower top reaches that methane purpose is reclaimed in condensation by liquid nitrogen cooling, reduction tower top oxygen content to blast
Outside the limit, it is ensured that the stable safe operation of system.
Brief description of the drawings
Fig. 1 produces the structural representation of LNG system for the utilization gas containing air of the present invention.
Embodiment
As shown in figure 1, the system that the utilization gas containing air of the present invention produces LNG, including main flow system and refrigeration system
System, main flow system along unstripped gas flow direction successively include filter 1, feed gas compressor 2, water cooler 3, clean unit 4,
Pre-cooling unit 5, drying unit 6, main heat exchanger 7 and rectifying column 8, the bottom of towe of rectifying column 8 is provided with reboiler 9 and condensate liquid goes out
Mouthful, the tower top of rectifying column is provided with overhead separator 10 and nitrogen oxygen offgas outlet.Refrigeration system includes being used for being main heat exchanger
There is provided cold and be reboiler 9 provide heat the azeotrope circulatory system and be rectifying column 8 provide cold nitrogen cycle system
Unite, so that most of methane in the unstripped gas in rectifying column is condensed into liquid and discharged from condensate outlet, lacking in unstripped gas
Methane and nitrogen oxygen tail gas is measured to discharge from nitrogen oxygen offgas outlet.
Utilization gas containing the air system of producing LNG of the present invention, wherein, the azeotrope circulatory system is along azeotrope stream
The mixing that dynamic direction includes azeotrope compensator 20 successively, the azeotrope for being exported to azeotrope compensator compresses is cold
Agent compressor 17, cooler 18, gas-liquid separator 19, the gas phase azeotrope outlet of gas-liquid separator 19 pass through the first pipeline 31
The gas phase azeotrope entrance of reboiler 9 is communicated in, the gas phase azeotrope outlet of reboiler 9 passes through the second pipeline 32 and first
Choke valve 41 is connected, and gas phase azeotrope is used to provide heat, the liquid phase azeotrope outlet of gas-liquid separator 19 for reboiler 9
Connected by the 3rd pipeline 33 with second throttle 42, after the cooling that throttled respectively by first throttle valve 41, second throttle 42
Azeotrope is back to azeotrope compensator 20 after converging by the 4th pipeline 34, azeotrope azeotrope compressor with
Circulated between azeotrope compensator, the first pipeline, the second pipeline, the 3rd pipeline, the 4th pipeline are respectively through main heat exchanger, the
Azeotrope in one pipeline 31, the 3rd pipeline 33 is cooled down in main heat exchanger 7, mixed in the second pipeline 32, the 4th pipeline 34
Close cryogen and provide cold in main heat exchanger 7.
For preferably using the cold of azeotrope, the saving energy, improving production efficiency, first throttle valve 41 passes through the tenth
One pipeline 310 connects azeotrope point, and the azeotrope after the cooling that throttled by first throttle valve 41 passes through the 11st pipeline
310 flow to azeotrope point, and the azeotrope that the 11st pipeline 310 passes through in main heat exchanger 7, the 11st pipeline 310 exists
Cold is provided in main heat exchanger 7.
The system that the utilization gas containing air of the present invention produces LNG, wherein, flowing side of the nitrogen cycle system along nitrogen cooling agent
To the nitrogen compressor 15 for including nitrogen balance tank 14 successively, compressing for the nitrogen that export to nitrogen balance tank 14, to nitrogen
The nitrogen cooler 16 of cooling, the 3rd choke valve 43 cooled for making nitrogen throttle as liquid nitrogen, nitrogen cooler 16 pass through the 5th pipe
Road 35 connects the 3rd choke valve 43, and the outlet of the 3rd choke valve 43 is in the nitrogen entrance of rectifying column, and the nitrogen outlet of rectifying column 8 is logical
The entrance that the 6th pipeline 36 is communicated in nitrogen balance tank 14 is crossed, so that liquid nitrogen is changed into nitrogen after providing cold in rectifying column 8
And nitrogen balance tank 14 is back to by the 6th pipeline 36, the 5th pipeline 35, the 6th pipeline 36 are respectively through main heat exchanger 7, the 5th
Nitrogen in pipeline 35 is cooled down in main heat exchanger 7, and the nitrogen in the 6th pipeline 36 provides cold in main heat exchanger 7.
The system that the utilization gas containing air of the present invention produces LNG, wherein, it is provided with the 6th pipeline 36 for removing oxygen
Nitrogen clean unit 13, nitrogen clean unit 13 be located between main heat exchanger 7 and nitrogen balance tank 14.
The system that the utilization gas containing air of the present invention produces LNG, wherein, nitrogen oxygen offgas outlet is connected by the 7th pipeline 37
Logical overhead separator 10, overhead separator 10 is by pipeline connection expanding machine 11, and expanding machine 11 is by after the expansion cooling of nitrogen oxygen tail gas
Nitrogen oxygen tail gas is discharged by the 8th pipeline 38, the 8th pipeline 38 sequentially passes through subcooler 12, main heat exchanger 7 by expanding machine 11,
So that the nitrogen oxygen tail gas in the 8th pipeline 38 provides cold and is warming up to normal temperature.
The system that the utilization gas containing air of the present invention produces LNG, wherein, condensate outlet is connected with the 9th pipeline 39,
9th pipeline 39 passes through subcooler 12, so as to be condensed into the methane cooling of liquid in the 9th pipeline 39, forms LNG.
The system that the utilization gas containing air of the present invention produces LNG, wherein, condensate outlet is connected with the tenth pipeline 40,
Tenth pipeline 40 passes through main heat exchanger 7, so as to be condensed into the methane rewarming gasification of liquid in the tenth pipeline 40, forms CNG.
The system that the utilization gas containing air of the present invention produces LNG, wherein, a small amount of methane and nitrogen oxygen tail gas in unstripped gas
Overhead separator 10 is expelled to from nitrogen oxygen offgas outlet, methane is back to rectifying column 8 after overhead separator 10 is condensed into liquid.
The method that the utilization gas containing air of the present invention produces LNG, including：
A main flow techniques：By unstripped gas after filtering, compression, purification, water cooling, 35~45 DEG C are obtained, absolute pressure is
0.5~0.7MPa, the unstripped gas containing saturation water is cooled to after 3~7 DEG C and dried, makes unstripped gas depoint depression again to unstripped gas
To -50~-70 DEG C；Dried unstripped gas is exchanged heat by main heat exchanger to cool, and the formation gas-liquid two after choke valve throttles
The gas-liquid mixture of phase, gas-liquid mixture enters rectifying column in the middle part of rectifying column, and liquid phase is downwardly towards bottom of towe, passes through rectifying tower
The reboiler heating evaporation at bottom flows out after going out the nitrogen oxygen tail gas of carrying from condensate outlet, obtains the LNG of methane concentration >=99%,
Gas phase in gas-liquid mixture flows upwardly toward rectifying column tower top, after the liquid nitrogen with rectifying column tower top is sufficiently mixed cooling, gas phase
In the methane liquefaction condensation that contains flow to bottom of towe, a part of nitrogen is extracted out from tower top, net by nitrogen after main heat exchanger rewarming
Nitrogen balance tank is returned to after changing unit deoxygenation, remaining nitrogen oxygen tail gas sequentially passes through supercooling after expander cools
Device, main heat exchanger re-heat to normal temperature；
B azeotrope circulation technologies：It is gas-liquid two that azeotrope enters gas-liquid separator separates after overcompression, cooling
Phase, gas phase is cooled by main heat exchanger, and the liquid phase of the gas-liquid mixture at rectifying tower bottom is heated into reboiler, and itself is cooled
To -135~-155 DEG C, -150~-170 DEG C then are cooled to by first throttle valve throttling, liquid phase is formed, passed sequentially through master and change
Hot device is exported after the part that the liquid phase in cold, azeotrope passes through main heat exchanger from main heat exchanger extraction, azeotrope
Liquid phase after main heat exchanger cools by second throttle throttle cool, with by first throttle valve throttle cooling liquid phase mix
After closing cryogen mixing azeotrope compensator is back into main heat exchanger rewarming；
C nitrogen cycle techniques：Nitrogen in nitrogen balance tank passes through after nitrogen compressor is compressed to 3.2~3.5MPa
Main heat exchanger cool, after being throttled by choke valve turn into liquid nitrogen enter rectifying column in, with the gas mixing after tower top rectifying there is provided
Cold needed for rectifying, condenses out the methane of tower top, while oxygen concentration is reduced to outside explosion limit, liquid nitrogen fully exchanges heat
Turn into nitrogen afterwards and then from overhead reflux, nitrogen balance tank is returned after main heat exchanger rewarming, nitrogen clean unit deoxygenation.
The utilization gas containing air of the present invention is produced in LNG method, and gas containing air enters unstripped gas by filter 1
After compressor 2 compresses, dropped after sequentially passing through water cooler 3, clean unit 4, pre-cooling unit 5, drying unit 6 by main heat exchanger 7
Temperature, subsequently into rectifying column 8, in rectifying column 8, most of methane is condensed into liquid and sent out from bottom of towe, and passes through subcooler 12
It is cooled to supercooled state feeding storage tank storage or is gasificated into CNG storages by main heat exchanger rewarming.A small amount of methane and nitrogen oxygen tail
Gas is discharged from tower top, and the liquid phase in tail gas flows back to rectifying column 8 by the bottom of overhead separator 10, and gas phase expands by expanding machine 11
After cooling, then sequentially pass through subcooler 12, the re-heat of main heat exchanger 7 to normal temperature.
The azeotrope circulatory system includes azeotrope compressor 17, cooler 18, gas-liquid separator 19, azeotrope and put down
Weigh tank 20.The azeotrope of azeotrope compensator 20 is cooled down laggard after the compression of refrigerant compressor 17 through subcooler 18
Enter gas-liquid separator 19 to separate, the gas phase of azeotrope passes sequentially through main heat exchanger 7, reboiler 9, throttled and cooled by choke valve
There is provided to unstripped gas after cold, return again to main heat exchanger 7, the liquid phase of azeotrope after cooling after main heat exchanger 7 from master by changing
The hot middle part of device 7 is extracted out, and then being throttled by choke valve cools, and it is multiple to be mixed into the middle part of main heat exchanger 7 with the gas phase cryogen of return
Temperature is back to azeotrope compensator 20.
Nitrogen throttling refrigeration recycle unit (nitrogen cycle system) includes nitrogen clean unit 13, nitrogen balance tank 14, nitrogen
Nitrogen in compressor 15, nitrogen cooler 16, nitrogen balance tank 14 is after the compression of nitrogen compressor 15, by nitrogen cooler
16th, after main heat exchanger 7 cools, liquid nitrogen is turned into by choke valve throttling and entered in rectifying column 8, is mixed with the gas after tower top rectifying
Close there is provided the cold needed for rectifying, condense out the methane of tower top, and reduce tower top oxygen content, fully turn into after heat exchange
Nitrogen returns to nitrogen balance tank 14 from overhead reflux by main heat exchanger 7, nitrogen clean unit 13.
The embodiment of LNG method is produced using gas containing air
Main flow technique：
The low pressure gas containing air produced from mine obtains 40 DEG C, absolute pressure after filtering, compression, purification, water cooling
For 0.6MPa, the unstripped gas containing saturation water is cooled by pre-cooling unit 5 and separates out substantial amounts of saturation water, temperature is down to after 5 DEG C
Into drying unit 6, unstripped gas dew point is down to -60 DEG C by drying unit 6, meets the requirement of liquefaction separator, dried
Gas containing air is cooled to -155 DEG C by the heat exchange of main heat exchanger 7, and forms after choke valve throttles the mixing of gas-liquid two-phase
Thing；Gas-liquid mixture enters and enters rectifying column from the middle part of rectifying column 8, and liquid phase is downwardly towards bottom of towe, is heated and steamed by reboiler 9
Send after a small amount of nitrogen oxygen tail gas of carrying from condensate outlet outflow, obtain the LNG of methane concentration >=99%, the LNG passes through mistake
Cooler 11 is cooled to -155 DEG C~-160 DEG C after exchanging heat, the LNG for forming (0.2MPa) with pressure supercooling delivers to storage tank storage or passed through
Cross main heat exchanger rewarming and be gasificated into CNG storages；
Gas phase in gas-liquid mixture flows upwardly toward the tower top of rectifying column 8, and cooling is sufficiently mixed in the liquid nitrogen with rectifying tower top
After to -171 DEG C, a small amount of methane liquefaction condensation contained in gas phase flows to bottom of towe, and a part of nitrogen-rich gas is extracted out from tower top, warp
Main heat exchanger rewarming is crossed to after 35 DEG C, nitrogen balance tank 14, remaining nitrogen oxygen tail are returned to after the deoxygenation of nitrogen clean unit 13
Gas sequentially passes through subcooler 12, the re-heat of main heat exchanger 7 to normal temperature after the expansion of expanding machine 11 is cooled to -178 DEG C；
B azeotrope circulation technologies：Azeotrope is cold through subcooler 18 after refrigerant compressor 17 is compressed to 2MPa
But to being separated into gas-liquid two-phase into gas-liquid separator 19 after 40 DEG C.Gas phase heats essence by main heat exchanger 7 into reboiler 9
The LNG of the bottom of towe of tower 8 is evaporated, -145 DEG C itself are cooled to, then -160 DEG C is cooled to by choke valve throttling, forms gas-liquid two-phase
Mixture pass sequentially through main heat exchanger 7 output cold, azeotrope liquid phase by after part main heat exchanger 7 from main heat exchanger 7
Middle part is extracted out, and the liquid phase cryogen after cooling is cooled to -55 DEG C by choke valve throttling, is mixed into and becomes owner of with the gas phase cryogen of return
The rewarming of heat exchanger 7 is back to azeotrope compensator 20, so as to realize that refrigerant cycle is utilized, by adjusting azeotrope internal circulating load
The refrigeration demand of liquefied natural gas can be met, and controls rectifying tower bottom evaporation capacity；
C nitrogen cycle techniques：Nitrogen throttling refrigeration circulation process equipment include nitrogen clean unit 13, nitrogen balance tank 14,
Nitrogen in nitrogen compressor 15, nitrogen cooler 16, nitrogen balance tank 14 is compressed to 3.2~3.5MPa by nitrogen compressor 15
Afterwards, -171 DEG C are cooled to by main heat exchanger 7, by choke valve throttle (- 180 DEG C of temperature) afterwards turn into liquid nitrogen enter rectifying column 8
It is interior, with the gas mixing after tower top rectifying there is provided the cold needed for rectifying, condense out the methane of tower top, while oxygen is dense
Degree is reduced to outside explosion limit, disclosure satisfy that the refrigeration demand of liquefied natural gas, and controls rectifying column tower top temperature, controls methane
The rate of recovery.Liquid nitrogen turns into nitrogen and then from overhead reflux after fully exchanging heat, by the rewarming of main heat exchanger 7, nitrogen clean unit
Nitrogen balance tank 14 is returned after 13 deoxygenations.
Azeotrope is methane, ethene, iso-butane, the mixture of nitrogen, and methane, ethene, iso-butane, the volume of nitrogen are matched somebody with somebody
Than for 0.3: 0.25: 0.22: 0.13.
The method that the utilization gas containing air of the present invention produces LNG, increases precooler after clean unit, reduces unstripped gas
Temperature so that a large amount of saturation waters condense out and separate discharge, drying unit load are reduced, while can also be dropped by pre-cooling unit
Low whole technological process energy consumption more than 5%；Increase nitrogen kind of refrigeration cycle on the basis of the azeotrope circulatory system, pass through throttling
Cooling is produced liquid nitrogen and added in rectifying column, and liquid nitrogen and rectifying gas are sufficiently mixed there is provided the cold needed for rectifying, and simultaneously by oxygen
Concentration is reduced to outside explosion limit, purifies methane from safe separating in gas containing air so as to realize, and can independently adjust
Gas product amount and yield.
The utilization gas containing air of the present invention produces LNG method and system, can independently adjust gas product and
While yield, the power consumption of whole technological process is reduced, rectifying column tower top reaches that methane purpose is reclaimed in condensation by liquid nitrogen cooling
While, reduce outside tower top oxygen content to explosion limit, it is ensured that the stable safe operation of system.
Described above is only the preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
For member, under the premise without departing from the principles of the invention, some improvements and modifications can also be made, these improvements and modifications also should
It is considered as protection scope of the present invention.
Claims (7)
1. a kind of system for producing LNG using gas containing air, it is characterised in that including main flow system and refrigeration system, institute
State main flow system includes filter, feed gas compressor, water cooler, clean unit, precooling successively along unstripped gas flow direction
Unit, drying unit, main heat exchanger and rectifying column, the bottom of towe of the rectifying column are provided with reboiler and condensate outlet, institute
The tower top for stating rectifying column is provided with overhead separator and nitrogen oxygen offgas outlet, and the refrigeration system includes being used for being main heat exchanger
Cold is provided and provides the azeotrope circulatory system of heat for reboiler and the nitrogen cycle system of cold is provided for rectifying column,
So that the portion of methane in unstripped gas in rectifying column is condensed into liquid and discharged from condensate outlet, methane and nitrogen in unstripped gas
Oxygen tail gas is discharged from nitrogen oxygen offgas outlet, and the azeotrope circulatory system includes mixing cold successively along azeotrope flow direction
Agent compensator, azeotrope compressor, cooler, gas-liquid point for the azeotrope compression that is exported to azeotrope compensator
From device, the gas phase azeotrope outlet of the gas-liquid separator mixes cold by the first pipeline connection in the gas phase of the reboiler
Agent entrance, the gas phase azeotrope outlet of the reboiler is connected by the second pipeline with first throttle valve, the gas phase mixing
Cryogen provides heat for reboiler, and the liquid phase azeotrope outlet of the gas-liquid separator passes through the 3rd pipeline and second throttle
Connection, the azeotrope after the cooling that throttled respectively by the first throttle valve, second throttle is returned after converging by the 4th pipeline
Azeotrope compensator is flow to, the azeotrope is circulated between azeotrope compressor and azeotrope compensator, first
Pipeline, the second pipeline, the 3rd pipeline, the 4th pipeline are respectively through the main heat exchanger, in first pipeline, the 3rd pipeline
Azeotrope is cooled down in the main heat exchanger, and the azeotrope in second pipeline, the 4th pipeline is in the main heat exchanger
Middle offer cold.
2. the system according to claim 1 for producing LNG using gas containing air, it is characterised in that the nitrogen cycle system
Unite includes nitrogen balance tank along the flow direction of nitrogen cooling agent, for the nitrogen of the nitrogen compression exported to nitrogen balance tank successively
Compressor, the nitrogen cooler cooled down to nitrogen, the 3rd choke valve cooled for making nitrogen throttle as liquid nitrogen, the nitrogen cooler
By the 3rd choke valve described in the 5th pipeline connection, the outlet of the 3rd choke valve in the nitrogen entrance of the rectifying column,
The nitrogen outlet of the rectifying column passes through the 6th pipeline connection in the entrance of the nitrogen balance tank, so that liquid nitrogen is in the rectifying column
Nitrogen is provided after middle offer cold and nitrogen balance tank is back to by the 6th pipeline, the 5th pipeline, the 6th pipeline respectively through
Nitrogen in the main heat exchanger, the 5th pipeline is cooled down in the main heat exchanger, and the nitrogen in the 6th pipeline exists
Cold is provided in the main heat exchanger.
3. the system according to claim 2 for producing LNG using gas containing air, it is characterised in that pacify on the 6th pipeline
Equipped with the nitrogen clean unit for removing oxygen, the nitrogen clean unit be located at the main heat exchanger and nitrogen balance tank it
Between.
4. the system according to claim 3 for producing LNG using gas containing air, it is characterised in that nitrogen oxygen offgas outlet
By overhead separator described in the 7th pipeline connection, the overhead separator is by pipeline connection expanding machine, and the expanding machine will
Nitrogen oxygen tail gas is discharged by the 8th pipeline after the expansion cooling of nitrogen oxygen tail gas, the 8th pipeline is sequentially passed through by the expanding machine
Subcooler, main heat exchanger, so that the nitrogen oxygen tail gas in the 8th pipeline provides cold and is warming up to normal temperature.
5. the system according to claim 4 for producing LNG using gas containing air, it is characterised in that the condensate liquid goes out
Mouth and the 9th pipeline connection, the 9th pipeline pass through the subcooler, so as to be condensed into the methane cooling of liquid, shape in the 9th pipeline
Into LNG.
6. the system according to claim 5 for producing LNG using gas containing air, it is characterised in that condensate outlet with
Tenth pipeline connection, the tenth pipeline passes through main heat exchanger, so as to be condensed into the methane rewarming gasification of liquid in the tenth pipeline, is formed
CNG。
7. a kind of utilization gas system containing air using the system as claimed in claim 1 that LNG is produced using gas containing air
The method for taking LNG, it is characterised in that including：
A main flow techniques：By unstripped gas after filtering, compression, purification, water cooling, 35~45 DEG C are obtained, absolute pressure is 0.5
~0.7MPa, the unstripped gas containing saturation water, unstripped gas is cooled to again after 3~7 DEG C dry, make unstripped gas dew point be down to-
50~-70 DEG C；Dried unstripped gas is exchanged heat by main heat exchanger to cool, and the formation gas-liquid two-phase after choke valve throttles
Gas-liquid mixture, gas-liquid mixture enters rectifying column in the middle part of rectifying column, and liquid phase is downwardly towards bottom of towe, passes through rectifying tower bottom
Reboiler heating evaporation flows out after going out the nitrogen oxygen tail gas of carrying from condensate outlet, obtains the LNG of methane concentration >=99%, gas-liquid
Gas phase in mixture flows upwardly toward rectifying column tower top, after the liquid nitrogen with rectifying column tower top is sufficiently mixed cooling, contains in gas phase
Some methane liquefaction condensations flow to bottom of towe, and a part of nitrogen is extracted out from tower top, after main heat exchanger rewarming, are purified by nitrogen single
Nitrogen balance tank is returned to after first deoxygenation, remaining nitrogen oxygen tail gas sequentially passes through subcooler, master after expander cools
Heat exchanger re-heat is to normal temperature；
B azeotrope circulation technologies：It is gas-liquid two-phase, gas that azeotrope enters gas-liquid separator separates after overcompression, cooling
Cooled by main heat exchanger, the liquid phase of the gas-liquid mixture at rectifying tower bottom is heated into reboiler, itself be cooled to-
135~-155 DEG C, -150~-170 DEG C then are cooled to by first throttle valve throttling, liquid phase is formed, passes sequentially through main heat exchange
Device is exported after the part that the liquid phase in cold, azeotrope passes through main heat exchanger from main heat exchanger extraction, azeotrope
Liquid phase throttles after main heat exchanger cools by second throttle to cool, and the liquid phase cooled is mixed with being throttled by first throttle valve
After cryogen mixing azeotrope compensator is back into main heat exchanger rewarming；
C nitrogen cycle techniques：Nitrogen in nitrogen balance tank is changed after nitrogen compressor is compressed to 3.2~3.5MPa by master
Hot device cooling, turns into liquid nitrogen and enters in rectifying column, there is provided rectifying with the gas mixing after tower top rectifying after being throttled by choke valve
Required cold, condenses out the methane of tower top, while oxygen concentration is reduced to outside explosion limit, liquid nitrogen fully exchange heat after into
For nitrogen and then from overhead reflux, nitrogen balance tank is returned after main heat exchanger rewarming, nitrogen clean unit deoxygenation.
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| CN108131895B (en) * | 2018-01-30 | 2023-04-25 | 四川蜀道装备科技股份有限公司 | Safe device and process for producing LNG or CNG by extracting partial methane from coal mine gas |
| CN109405413B (en) * | 2018-11-17 | 2024-01-30 | 杭州宏盛中弘新能源有限公司 | Oxygen-containing coal bed gas cryogenic rectification system and method avoiding explosion limit |
| CN116987536B (en) * | 2023-06-15 | 2024-03-08 | 英德市西洲气体有限公司 | Argon removal process for methane tower |
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| JPS5843640B2 (en) * | 1979-07-17 | 1983-09-28 | 千代田化工建設株式会社 | LNG processing method |
| US6978638B2 (en) * | 2003-05-22 | 2005-12-27 | Air Products And Chemicals, Inc. | Nitrogen rejection from condensed natural gas |
| CN100404988C (en) * | 2006-07-03 | 2008-07-23 | 中国科学院理化技术研究所 | Air-contained coal gas gasification and separation process and equipment |
| US8627681B2 (en) * | 2009-03-04 | 2014-01-14 | Lummus Technology Inc. | Nitrogen removal with iso-pressure open refrigeration natural gas liquids recovery |
| CN101929788B (en) * | 2010-09-15 | 2012-01-04 | 中国科学院理化技术研究所 | Device for preparing liquefied natural gas by oxygen-bearing coal mine methane |
| US20120324943A1 (en) * | 2011-06-21 | 2012-12-27 | Butts Rayburn C | Two Step Nitrogen and Methane Separation Process |
| CN204944041U (en) * | 2015-09-22 | 2016-01-06 | 北京中科瑞奥能源科技股份有限公司 | Utilize the system producing LNG containing air gas |
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