CN105135820A - Method and system for manufacturing LNG through gas containing air - Google Patents
Method and system for manufacturing LNG through gas containing air Download PDFInfo
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- CN105135820A CN105135820A CN201510603093.1A CN201510603093A CN105135820A CN 105135820 A CN105135820 A CN 105135820A CN 201510603093 A CN201510603093 A CN 201510603093A CN 105135820 A CN105135820 A CN 105135820A
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- 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
- 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
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention provides a method and system for manufacturing LNG through gas containing air. The system comprises a main flow system and a refrigerating system. The main flow system comprises a raw material gas compressor, a water cooler, a purifying unit, a pre-cooling unit, a drying unit, a main heat exchanger and a rectifying tower. The bottom of the rectifying tower is provided with a reboiler and a condensate outlet. The tower top of the rectifying tower is provided with a tower top separator and a nitrogen and oxygen tail gas outlet. The refrigerating system comprises a mixed refrigerant circulating system and a nitrogen circulating system. The method includes the steps of a main process technology A, a mixed refrigerant circulating technology B and a nitrogen circulating technology C. The method and system for manufacturing LNG through gas containing air can independently adjust the natural gas product and the yield; by arranging the pre-cooling unit, the power consumption of the whole process technology can be reduced by more that 5%, the tower top oxygen content can be reduced to beyond explosion limits, and stable and safe operation of the system is guaranteed.
Description
Technical field
The present invention relates to liquefied natural gas industry, particularly relate to a kind of utilization and contain method and the system that air gas produces LNG.
Background technology
Liquefied natural gas (be called for short LNG) be natural gas (being called for short NG) compressed, be cooled to the liquified natural gas that its boiling point (about-161.5 DEG C, with component about) formed afterwards, main component is methane.Its volume is about with amount gaseous natural gas volume 1/625, and its colourless, tasteless, nontoxic and non-corrosiveness, is widely used in the industries such as petrochemical industry, electric power, gas and Automobile Transportation.Use LNG as clean energy resource, there is obvious environmental benefit and social benefit.Can reduce the sulfur dioxide (SO2) emissions of 90% and the discharged nitrous oxides of 80% after replacing fuel oil with LNG, environmental benefit is fairly obvious.
CNG and compressed natural gas (CompressedNaturalGas is called for short CNG) are natural gas pressurization and store with gaseous state to be formed in a reservoir.Compressed natural gas can be compressed by the natural gas via in oil field and gas field and be formed.
Gas is the gas carrying out extraction under the mine carrying out coal mining, also claims coal bed gas.This mode extraction mash gas methane content is out lower, usually between 30% ~ 70%.Methane is the industrial chemicals of clear energy sources and high-quality, and from gas, separating-purifying methane is for expansion with improve effective utilization of gas and economic worth has great importance.China's gas place of production disperses, and well yield is low, and in the gas of major part exploitation, methane concentration is low and containing oxygen, in processing procedure, easily produce blast, must have safety, economic isolation technics could abundant Appropriate application.
The current technology occurring multiple preparing natural gas of purifying in low concentration gas.Such as publication number is that the patent of CN101922850A and CN101929788A individually discloses a kind of utilization and produces the method for liquefied natural gas containing air gas and utilize and produce the device of liquefied natural gas containing air gas, the method and device adopt the cascade refrigeration circulation of azeotrope self, raw material liquefaction after purification is separated, obtains LNG product.There are some shortcomings in above-mentioned prior art: in unstripped gas, methane content fluctuation is comparatively large, affects the stable operation of liquefaction process unavoidably, adopts MRC cascade refrigeration to circulate in the requirement that simultaneously can not meet product purity and the rate of recovery in device adjustment process; Containing air gas after cleaning, temperature, pressure is higher, and comparatively large containing saturated water amount, drying unit energy consumption is higher.
Summary of the invention
The object of this invention is to provide a kind of can independently adjust gas product and yield while, reduce the power consumption of whole technological process, ensure that the utilization that the stability and safety of system is run produces method and the system of LNG containing air gas.
Utilization of the present invention produces the system of LNG containing air gas, comprise main flow system and refrigeration system, described main flow system comprises filter successively along unstripped gas flow direction, feed gas compressor, water cooler, clean unit, pre-cooling unit, drying unit, main heat exchanger and rectifying column, reboiler and condensate outlet is provided with at the bottom of the tower of described rectifying column, the tower top of described rectifying column is provided with overhead separator and nitrogen oxygen offgas outlet, described refrigeration system comprises for providing cold for main heat exchanger and providing the azeotrope circulatory system of heat for reboiler and provide the nitrogen cycle system of cold for rectifying column, be condensed into liquid to make the portion of methane in the unstripped gas in rectifying column to discharge from condensate outlet, methane in unstripped gas and nitrogen oxygen tail gas are discharged from nitrogen oxygen offgas outlet.
Utilization of the present invention produces the system of LNG containing air gas, wherein, the described azeotrope circulatory system comprises azeotrope compensator successively along azeotrope flow direction, for the azeotrope compressor that the azeotrope exported azeotrope compensator compresses, cooler, gas-liquid separator, the gas phase azeotrope outlet of described gas-liquid separator is by the gas phase azeotrope entrance of the first pipeline connection in described reboiler, the gas phase azeotrope outlet of described reboiler is communicated with first throttle valve by the second pipeline, described gas phase azeotrope provides heat for reboiler, the liquid phase azeotrope outlet of described gas-liquid separator is communicated with second throttle by the 3rd pipeline, by described first throttle valve, second throttle respectively throttling cooling after azeotrope converge after be back to azeotrope compensator by the 4th pipeline, described azeotrope circulates between azeotrope compressor and azeotrope compensator, first pipeline, second pipeline, 3rd pipeline, 4th pipeline is respectively through described main heat exchanger, described first pipeline, azeotrope in 3rd pipeline cools in described main heat exchanger, described second pipeline, azeotrope in 4th pipeline provides cold in described main heat exchanger.
Utilization of the present invention produces the system of LNG containing air gas, wherein, described nitrogen cycle system comprises nitrogen balance tank successively along the flow direction of nitrogen cooling agent, for the nitrogen compressor that the nitrogen exported nitrogen balance tank compresses, to the nitrogen cooler of nitrogen cooling, lower the temperature as the 3rd choke valve of liquid nitrogen for making nitrogen throttling, described nitrogen cooler is by the 3rd choke valve described in the 5th pipeline connection, the outlet of described 3rd choke valve is in the nitrogen entrance of described rectifying column, the nitrogen outlet of described rectifying column is by the entrance of the 6th pipeline connection in described nitrogen balance tank, change nitrogen into after providing cold to make liquid nitrogen in described rectifying column and be back to nitrogen balance tank by the 6th pipeline, 5th pipeline, 6th pipeline is respectively through described main heat exchanger, nitrogen in described 5th pipeline cools in described main heat exchanger, nitrogen in described 6th pipeline provides cold in described main heat exchanger.
Utilization of the present invention produces the system of LNG containing air gas, and wherein, the 6th pipeline is provided with the nitrogen purge unit for removing oxygen, described nitrogen purge unit is between described main heat exchanger and nitrogen balance tank.
Utilization of the present invention produces the system of LNG containing air gas, wherein, nitrogen oxygen offgas outlet is by overhead separator described in the 7th pipeline connection, described overhead separator is by pipeline connection decompressor, nitrogen oxygen tail gas expands by described decompressor, and cooling is rear is discharged nitrogen oxygen tail gas by the 8th pipeline, described 8th pipeline successively through subcooler, main heat exchanger by described decompressor, is provided cold to make the nitrogen oxygen tail gas in described 8th pipeline and is warming up to normal temperature.
Utilization of the present invention produces the system of LNG containing air gas, and wherein, described condensate outlet and the 9th pipeline connection, the 9th pipeline, through described subcooler, to make the methane cooling being condensed into liquid in the 9th pipeline, forms LNG.
Utilization of the present invention produces the system of LNG containing air gas, and wherein, condensate outlet and the tenth pipeline connection, the tenth pipeline, through main heat exchanger, to make the methane rewarming gasification being condensed into liquid in the tenth pipeline, forms CNG.
Utilization of the present invention produces the method for LNG containing air gas, comprising:
A main flow technique: by unstripped gas after filtration, compression, purification, water-cooled, obtain 35 ~ 45 DEG C, absolute pressure is 0.5 ~ 0.7MPa, the unstripped gas containing saturation water, dry after 3 ~ 7 DEG C are cooled to again to unstripped gas, make unstripped gas depoint depression to-50 ~-70 DEG C, dried unstripped gas is lowered the temperature by main heat exchanger heat exchange, and after choke valve throttling, form the gas-liquid mixture of gas-liquid two-phase, gas-liquid mixture enters rectifying column in the middle part of rectifying column, liquid phase flows to downwards at the bottom of tower, flow out from condensate outlet after the nitrogen oxygen tail gas going out to carry by the reboiler heating evaporation at the bottom of rectifying tower, obtain the LNG of methane concentration >=99%, gas phase in gas-liquid mixture upwards flows to rectifying column tower top, with the abundant hybrid cooling of the liquid nitrogen of rectifying column tower top after, the methane liquefaction condensate flow contained in gas phase is at the bottom of tower, part nitrogen is extracted out from tower top, after main heat exchanger rewarming, nitrogen balance tank is got back to by after the deoxygenation of nitrogen purge unit, remaining nitrogen oxygen tail gas after expander cooling successively through subcooler, main heat exchanger re-heat is to normal temperature,
B azeotrope circulation technology: azeotrope is through overcompression, entering gas-liquid separator separates after cooling is gas-liquid two-phase, gas phase is lowered the temperature by main heat exchanger, enter the liquid phase of the gas-liquid mixture of reboiler heating at the bottom of rectifying tower, self be cooled to-135 ~-155 DEG C, then-150 ~-170 DEG C are cooled to through the throttling of first throttle valve, form liquid phase, cold is exported successively by main heat exchanger, liquid phase in azeotrope is by extracting out from main heat exchanger after a part for main heat exchanger, liquid phase in azeotrope is lowered the temperature through second throttle throttling after main heat exchanger cooling, mix with the liquid phase azeotrope of being lowered the temperature by the throttling of first throttle valve laggard enter main heat exchanger rewarming be back to azeotrope compensator,
C nitrogen cycle technique: the nitrogen in nitrogen balance tank is compressed to after 3.2 ~ 3.5MPa through nitrogen compressor, lower the temperature through main heat exchanger, enter in rectifying column by becoming liquid nitrogen after choke valve throttling, with the gas and vapor permeation after tower top rectifying, cold needed for rectifying is provided, the methane condensation of tower top is got off, oxygen concentration is reduced to outside explosion limit simultaneously, become nitrogen then from overhead reflux after the abundant heat exchange of liquid nitrogen, after main heat exchanger rewarming, the deoxygenation of nitrogen purge unit, return nitrogen balance tank.
Utilization of the present invention produces method and the system of LNG containing air gas, while can independently adjusting gas product and yield, by the power consumption arranging filter, water cooler, clean unit, pre-cooling unit, drying unit reduce whole technological process, while rectifying column tower top reaches condensation recovery methane object by liquid nitrogen cooling, reduce tower top oxygen content to outside explosion limit, ensure that the stability and safety of system is run.
Accompanying drawing explanation
Fig. 1 is that utilization of the present invention produces the structural representation of the system of LNG containing air gas.
Detailed description of the invention
As shown in Figure 1, utilization of the present invention produces the system of LNG containing air gas, comprise main flow system and refrigeration system, main flow system comprises 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 successively along unstripped gas flow direction, be provided with reboiler 9 and condensate outlet at the bottom of the tower of rectifying column 8, the tower top of rectifying column is provided with overhead separator 10 and nitrogen oxygen offgas outlet.Refrigeration system comprises for providing cold for main heat exchanger and providing the azeotrope circulatory system of heat for reboiler 9 and provide the nitrogen cycle system of cold for rectifying column 8, be condensed into liquid to make the most of methane in the unstripped gas in rectifying column to discharge from condensate outlet, a small amount of methane in unstripped gas and nitrogen oxygen tail gas are discharged from nitrogen oxygen offgas outlet.
Utilization of the present invention produces the system of LNG containing air gas, wherein, the azeotrope circulatory system comprises azeotrope compensator 20 successively along azeotrope flow direction, for the azeotrope compressor 17 that the azeotrope exported azeotrope compensator compresses, cooler 18, gas-liquid separator 19, the gas phase azeotrope outlet of gas-liquid separator 19 is communicated in the gas phase azeotrope entrance of reboiler 9 by the first pipeline 31, the gas phase azeotrope outlet of reboiler 9 is communicated with first throttle valve 41 by the second pipeline 32, gas phase azeotrope is used for providing heat for reboiler 9, the liquid phase azeotrope outlet of gas-liquid separator 19 is communicated with second throttle 42 by the 3rd pipeline 33, by first throttle valve 41, second throttle 42 respectively throttling cooling after azeotrope converge after be back to azeotrope compensator 20 by the 4th pipeline 34, azeotrope circulates between azeotrope compressor and azeotrope compensator, first pipeline, second pipeline, 3rd pipeline, 4th pipeline is respectively through main heat exchanger, first pipeline 31, azeotrope in 3rd pipeline 33 cools in main heat exchanger 7, second pipeline 32, azeotrope in 4th pipeline 34 provides cold in main heat exchanger 7.
For better utilizing cold, economize energy, the improving production efficiency of azeotrope, first throttle valve 41 connects azeotrope point by the 11 pipeline 310, azeotrope point is flow to by the 11 pipeline 310 by the azeotrope after first throttle valve 41 throttling cooling, 11 pipeline 310 is through main heat exchanger 7, and the azeotrope in the 11 pipeline 310 provides cold in main heat exchanger 7.
Utilization of the present invention produces the system of LNG containing air gas, wherein, nitrogen cycle system comprises nitrogen balance tank 14 successively along the flow direction of nitrogen cooling agent, for the nitrogen compressor 15 that the nitrogen exported nitrogen balance tank 14 compresses, to the nitrogen cooler 16 of nitrogen cooling, lower the temperature as the 3rd choke valve 43 of liquid nitrogen for making nitrogen throttling, nitrogen cooler 16 is communicated with the 3rd choke valve 43 by the 5th pipeline 35, the outlet of the 3rd choke valve 43 is in the nitrogen entrance of rectifying column, the nitrogen outlet of rectifying column 8 is communicated in the entrance of nitrogen balance tank 14 by the 6th pipeline 36, change nitrogen into after providing cold to make liquid nitrogen in rectifying column 8 and be back to nitrogen balance tank 14 by the 6th pipeline 36, 5th pipeline 35, 6th pipeline 36 is respectively through main heat exchanger 7, nitrogen in 5th pipeline 35 cools in main heat exchanger 7, nitrogen in 6th pipeline 36 provides cold in main heat exchanger 7.
Utilization of the present invention produces the system of LNG containing air gas, and wherein, the 6th pipeline 36 is provided with the nitrogen purge unit 13 for removing oxygen, nitrogen purge unit 13 is between main heat exchanger 7 and nitrogen balance tank 14.
Utilization of the present invention produces the system of LNG containing air gas, wherein, nitrogen oxygen offgas outlet is communicated with overhead separator 10 by the 7th pipeline 37, overhead separator 10 is by pipeline connection decompressor 11, nitrogen oxygen tail gas expands by decompressor 11, and cooling is rear is discharged nitrogen oxygen tail gas by the 8th pipeline 38,8th pipeline 38 successively through subcooler 12, main heat exchanger 7 by decompressor 11, is provided cold to make the nitrogen oxygen tail gas in the 8th pipeline 38 and is warming up to normal temperature.
Utilization of the present invention produces the system of LNG containing air gas, and wherein, condensate outlet is communicated with the 9th pipeline 39, and the 9th pipeline 39, through subcooler 12, to make the methane cooling being condensed into liquid in the 9th pipeline 39, forms LNG.
Utilization of the present invention produces the system of LNG containing air gas, and wherein, condensate outlet is communicated with the tenth pipeline 40, and the tenth pipeline 40, through main heat exchanger 7, to make the methane rewarming gasification being condensed into liquid in the tenth pipeline 40, forms CNG.
Utilization of the present invention produces the system of LNG containing air gas, and wherein, a small amount of methane in unstripped gas and nitrogen oxygen tail gas are expelled to overhead separator 10 from nitrogen oxygen offgas outlet, and methane is back to rectifying column 8 after overhead separator 10 is condensed into liquid state.
Utilization of the present invention produces the method for LNG containing air gas, comprising:
A main flow technique: by unstripped gas after filtration, compression, purification, water-cooled, obtain 35 ~ 45 DEG C, absolute pressure is 0.5 ~ 0.7MPa, the unstripped gas containing saturation water, dry after 3 ~ 7 DEG C are cooled to again to unstripped gas, make unstripped gas depoint depression to-50 ~-70 DEG C, dried unstripped gas is lowered the temperature by main heat exchanger heat exchange, and after choke valve throttling, form the gas-liquid mixture of gas-liquid two-phase, gas-liquid mixture enters rectifying column in the middle part of rectifying column, liquid phase flows to downwards at the bottom of tower, flow out from condensate outlet after the nitrogen oxygen tail gas going out to carry by the reboiler heating evaporation at the bottom of rectifying tower, obtain the LNG of methane concentration >=99%, gas phase in gas-liquid mixture upwards flows to rectifying column tower top, with the abundant hybrid cooling of the liquid nitrogen of rectifying column tower top after, the methane liquefaction condensate flow contained in gas phase is at the bottom of tower, part nitrogen is extracted out from tower top, after main heat exchanger rewarming, nitrogen balance tank is got back to by after the deoxygenation of nitrogen purge unit, remaining nitrogen oxygen tail gas after expander cooling successively through subcooler, main heat exchanger re-heat is to normal temperature,
B azeotrope circulation technology: azeotrope is through overcompression, entering gas-liquid separator separates after cooling is gas-liquid two-phase, gas phase is lowered the temperature by main heat exchanger, enter the liquid phase of the gas-liquid mixture of reboiler heating at the bottom of rectifying tower, self be cooled to-135 ~-155 DEG C, then-150 ~-170 DEG C are cooled to through the throttling of first throttle valve, form liquid phase, cold is exported successively by main heat exchanger, liquid phase in azeotrope is by extracting out from main heat exchanger after a part for main heat exchanger, liquid phase in azeotrope is lowered the temperature through second throttle throttling after main heat exchanger cooling, mix with the liquid phase azeotrope of being lowered the temperature by the throttling of first throttle valve laggard enter main heat exchanger rewarming be back to azeotrope compensator,
C nitrogen cycle technique: the nitrogen in nitrogen balance tank is compressed to after 3.2 ~ 3.5MPa through nitrogen compressor, lower the temperature through main heat exchanger, enter in rectifying column by becoming liquid nitrogen after choke valve throttling, with the gas and vapor permeation after tower top rectifying, cold needed for rectifying is provided, the methane condensation of tower top is got off, oxygen concentration is reduced to outside explosion limit simultaneously, become nitrogen then from overhead reflux after the abundant heat exchange of liquid nitrogen, after main heat exchanger rewarming, the deoxygenation of nitrogen purge unit, return nitrogen balance tank.
Utilization of the present invention is produced in the method for LNG containing air gas, after entering feed gas compressor 2 compression containing air gas by filter 1, lowered the temperature by main heat exchanger 7 after water cooler 3, clean unit 4, pre-cooling unit 5, drying unit 6 successively, then rectifying column 8 is entered, in rectifying column 8, major part methane is condensed into liquid and sends at the bottom of tower, and is cooled to the storage tank storage of supercooled state feeding through subcooler 12 or is gasificated into CNG storage through main heat exchanger rewarming.A small amount of methane and nitrogen oxygen tail gas are discharged from tower top, the liquid phase in tail gas by flowing back to rectifying column 8 bottom overhead separator 10, gas phase through decompressor 11 expand cooling after, more successively through subcooler 12, main heat exchanger 7 re-heat to normal temperature.
The azeotrope circulatory system comprises azeotrope compressor 17, cooler 18, gas-liquid separator 19, azeotrope compensator 20.The azeotrope of azeotrope compensator 20 is after refrigerant compressor 17 compresses, after subcooler 18 cools, enter gas-liquid separator 19 be separated, the gas phase of azeotrope is successively by main heat exchanger 7, reboiler 9, after lowering the temperature and provide cold by choke valve throttling to unstripped gas, return main heat exchanger 7 again, the liquid phase of azeotrope by extracting out after cooling after main heat exchanger 7 in the middle part of main heat exchanger 7, then lowered the temperature by choke valve throttling, be mixed into rewarming in the middle part of main heat exchanger 7 with the gas phase cryogen returned and be back to azeotrope compensator 20.
Nitrogen throttling refrigeration recycle unit (nitrogen cycle system) comprises nitrogen purge unit 13, nitrogen balance tank 14, nitrogen compressor 15, nitrogen cooler 16, nitrogen in nitrogen balance tank 14 is after nitrogen compressor 15 compresses, through nitrogen cooler 16, after main heat exchanger 7 is lowered the temperature, becoming liquid nitrogen by choke valve throttling enters in rectifying column 8, with the gas and vapor permeation after tower top rectifying, cold needed for rectifying is provided, the methane condensation of tower top is got off, and reduce tower top oxygen content, nitrogen is become from overhead reflux after abundant heat exchange, through main heat exchanger 7, nitrogen purge unit 13 returns nitrogen balance tank 14.
Utilize the embodiment producing the method for LNG containing air gas
Main flow technique:
Air gas is contained after filtration, compression, purification, water-cooled from the low pressure of mine extraction, obtain 40 DEG C, absolute pressure is 0.6MPa, unstripped gas containing saturation water, lowered the temperature by pre-cooling unit 5 and separate out a large amount of saturation waters, temperature enters drying unit 6 after being down to 5 DEG C, drying unit 6 is by unstripped gas depoint depression extremely-60 DEG C, meet the requirement of liquefaction separator, the dried air gas that contains is cooled to-155 DEG C by main heat exchanger 7 heat exchange, and forms the mixture of gas-liquid two-phase after choke valve throttling; Gas-liquid mixture enters and enters rectifying column from the middle part of rectifying column 8, liquid phase flows to downwards at the bottom of tower, flow out from condensate outlet after a small amount of nitrogen oxygen tail gas going out to carry by reboiler 9 heating evaporation, obtain the LNG of methane concentration >=99%, this LNG, by being cooled to-155 DEG C ~-160 DEG C after subcooler 11 heat exchange, forming (0.2MPa) with pressure excessively cold LNG and delivers to storage tank storage or be gasificated into CNG storage through main heat exchanger rewarming;
Gas phase in gas-liquid mixture upwards flows to rectifying column 8 tower top, with the abundant hybrid cooling of the liquid nitrogen of rectifying tower top to after-171 DEG C, the a small amount of methane liquefaction condensate flow contained in gas phase is at the bottom of tower, part nitrogen-rich gas is extracted out from tower top, after main heat exchanger rewarming to 35 DEG C, after nitrogen purge unit 13 deoxygenation, get back to nitrogen balance tank 14, remaining nitrogen oxygen tail gas through decompressor 11 expand be cooled to-178 DEG C after successively through subcooler 12, main heat exchanger 7 re-heat to normal temperature;
B azeotrope circulation technology: azeotrope, after refrigerant compressor 17 is compressed to 2MPa, enters gas-liquid separator 19 and is separated into gas-liquid two-phase after subcooler 18 is cooled to 40 DEG C.Gas phase is by main heat exchanger 7, enter reboiler 9 and heat LNG at the bottom of rectifying column 8 tower, self is cooled to-145 DEG C, then-160 DEG C are cooled to through choke valve throttling, the mixture forming gas-liquid two-phase exports cold by main heat exchanger 7 successively, azeotrope liquid phase by extracting out after part main heat exchanger 7 in the middle part of main heat exchanger 7, liquid phase cryogen after cooling is cooled to-55 DEG C through choke valve throttling, be mixed into main heat exchanger 7 rewarming with the gas phase cryogen returned and be back to azeotrope compensator 20, thus realize refrigerant cycle utilization, by the refrigeration demand regulating azeotrope internal circulating load can meet liquefied natural gas, and control evaporation capacity at the bottom of rectifying tower,
C nitrogen cycle technique: nitrogen throttling refrigeration circulation process equipment comprises nitrogen purge unit 13, nitrogen balance tank 14, nitrogen compressor 15, nitrogen cooler 16, nitrogen in nitrogen balance tank 14 is after nitrogen compressor 15 is compressed to 3.2 ~ 3.5MPa,-171 DEG C are cooled to through main heat exchanger 7, enter in rectifying column 8 by becoming liquid nitrogen after choke valve throttling (temperature-180 DEG C), with the gas and vapor permeation after tower top rectifying, cold needed for rectifying is provided, the methane condensation of tower top is got off, oxygen concentration is reduced to outside explosion limit simultaneously, the refrigeration demand of liquefied natural gas can be met, and control rectifying column tower top temperature, control the rate of recovery of methane.Become nitrogen then from overhead reflux after the abundant heat exchange of liquid nitrogen, after main heat exchanger 7 rewarming, nitrogen purge unit 13 deoxygenation, return nitrogen balance tank 14.
Azeotrope is the mixture of methane, ethene, iso-butane, nitrogen, and the volume proportion of methane, ethene, iso-butane, nitrogen is 0.3: 0.25: 0.22: 0.13.
Utilization of the present invention produces the method for LNG containing air gas, after clean unit, increase precooler, reduce unstripped gas temperature, make a large amount of saturation water condensation get off and be separated discharge, reduce drying unit load, also reduce whole technological process energy consumption more than 5% by pre-cooling unit simultaneously; The basis of the azeotrope circulatory system increases nitrogen kind of refrigeration cycle, producing liquid nitrogen by throttling cooling adds in rectifying column, liquid nitrogen and rectifying gas fully mix, cold needed for rectifying is provided, and oxygen concentration is reduced to outside explosion limit simultaneously, thus realize from containing safe separating purification methane air gas, and can independently adjust gas product amount and yield.
Utilization of the present invention produces method and the system of LNG containing air gas, while can independently adjusting gas product and yield, reduce the power consumption of whole technological process, while rectifying column tower top reaches condensation recovery methane object by liquid nitrogen cooling, reduce tower top oxygen content to outside explosion limit, ensure that the stability and safety of system is run.
The above is only the preferred embodiment of the present invention; it should be pointed out that for those skilled in the art, under the premise without departing from the principles of the invention; can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
Claims (8)
1. one kind utilizes the system producing LNG containing air gas, it is characterized in that, comprise main flow system and refrigeration system, described main flow system comprises filter successively along unstripped gas flow direction, feed gas compressor, water cooler, clean unit, pre-cooling unit, drying unit, main heat exchanger and rectifying column, reboiler and condensate outlet is provided with at the bottom of the tower of described rectifying column, the tower top of described rectifying column is provided with overhead separator and nitrogen oxygen offgas outlet, described refrigeration system comprises for providing cold for main heat exchanger and providing the azeotrope circulatory system of heat for reboiler and provide the nitrogen cycle system of cold for rectifying column, be condensed into liquid to make the portion of methane in the unstripped gas in rectifying column to discharge from condensate outlet, methane in unstripped gas and nitrogen oxygen tail gas are discharged from nitrogen oxygen offgas outlet.
2. the system of LNG is produced in utilization according to claim 1 containing air gas, it is characterized in that, the described azeotrope circulatory system comprises azeotrope compensator successively along azeotrope flow direction, for the azeotrope compressor that the azeotrope exported azeotrope compensator compresses, cooler, gas-liquid separator, the gas phase azeotrope outlet of described gas-liquid separator is by the gas phase azeotrope entrance of the first pipeline connection in described reboiler, the gas phase azeotrope outlet of described reboiler is communicated with first throttle valve by the second pipeline, described gas phase azeotrope provides heat for reboiler, the liquid phase azeotrope outlet of described gas-liquid separator is communicated with second throttle by the 3rd pipeline, by described first throttle valve, second throttle respectively throttling cooling after azeotrope converge after be back to azeotrope compensator by the 4th pipeline, described azeotrope circulates between azeotrope compressor and azeotrope compensator, first pipeline, second pipeline, 3rd pipeline, 4th pipeline is respectively through described main heat exchanger, described first pipeline, azeotrope in 3rd pipeline cools in described main heat exchanger, described second pipeline, azeotrope in 4th pipeline provides cold in described main heat exchanger.
3. the system of LNG is produced in utilization according to claim 2 containing air gas, it is characterized in that, described nitrogen cycle system comprises nitrogen balance tank successively along the flow direction of nitrogen cooling agent, for the nitrogen compressor that the nitrogen exported nitrogen balance tank compresses, to the nitrogen cooler of nitrogen cooling, lower the temperature as the 3rd choke valve of liquid nitrogen for making nitrogen throttling, described nitrogen cooler is by the 3rd choke valve described in the 5th pipeline connection, the outlet of described 3rd choke valve is in the nitrogen entrance of described rectifying column, the nitrogen outlet of described rectifying column is by the entrance of the 6th pipeline connection in described nitrogen balance tank, change nitrogen into after providing cold to make liquid nitrogen in described rectifying column and be back to nitrogen balance tank by the 6th pipeline, 5th pipeline, 6th pipeline is respectively through described main heat exchanger, nitrogen in described 5th pipeline cools in described main heat exchanger, nitrogen in described 6th pipeline provides cold in described main heat exchanger.
4. the system of LNG is produced in utilization according to claim 3 containing air gas, and it is characterized in that, the 6th pipeline is provided with the nitrogen purge unit for removing oxygen, described nitrogen purge unit is between described main heat exchanger and nitrogen balance tank.
5. the system of LNG is produced in utilization according to claim 4 containing air gas, it is characterized in that, nitrogen oxygen offgas outlet is by overhead separator described in the 7th pipeline connection, described overhead separator is by pipeline connection decompressor, nitrogen oxygen tail gas expands by described decompressor, and cooling is rear is discharged nitrogen oxygen tail gas by the 8th pipeline, described 8th pipeline successively through subcooler, main heat exchanger by described decompressor, is provided cold to make the nitrogen oxygen tail gas in described 8th pipeline and is warming up to normal temperature.
6. the system of LNG is produced in utilization according to claim 5 containing air gas, it is characterized in that, described condensate outlet and the 9th pipeline connection, and the 9th pipeline, through described subcooler, to make the methane cooling being condensed into liquid in the 9th pipeline, forms LNG.
7. the system of LNG is produced in utilization according to claim 6 containing air gas, it is characterized in that, condensate outlet and the tenth pipeline connection, and the tenth pipeline, through main heat exchanger, to make the methane rewarming gasification being condensed into liquid in the tenth pipeline, forms CNG.
8. utilize the method producing LNG containing air gas, it is characterized in that, comprising:
A main flow technique: by unstripped gas after filtration, compression, purification, water-cooled, obtain 35 ~ 45 DEG C, absolute pressure is 0.5 ~ 0.7MPa, the unstripped gas containing saturation water, dry after 3 ~ 7 DEG C are cooled to again to unstripped gas, make unstripped gas depoint depression to-50 ~-70 DEG C, dried unstripped gas is lowered the temperature by main heat exchanger heat exchange, and after choke valve throttling, form the gas-liquid mixture of gas-liquid two-phase, gas-liquid mixture enters rectifying column in the middle part of rectifying column, liquid phase flows to downwards at the bottom of tower, flow out from condensate outlet after the nitrogen oxygen tail gas going out to carry by the reboiler heating evaporation at the bottom of rectifying tower, obtain the LNG of methane concentration >=99%, gas phase in gas-liquid mixture upwards flows to rectifying column tower top, with the abundant hybrid cooling of the liquid nitrogen of rectifying column tower top after, the methane liquefaction condensate flow contained in gas phase is at the bottom of tower, part nitrogen is extracted out from tower top, after main heat exchanger rewarming, nitrogen balance tank is got back to by after the deoxygenation of nitrogen purge unit, remaining nitrogen oxygen tail gas after expander cooling successively through subcooler, main heat exchanger re-heat is to normal temperature,
B azeotrope circulation technology: azeotrope is through overcompression, entering gas-liquid separator separates after cooling is gas-liquid two-phase, gas phase is lowered the temperature by main heat exchanger, enter the liquid phase of the gas-liquid mixture of reboiler heating at the bottom of rectifying tower, self be cooled to-135 ~-155 DEG C, then-150 ~-170 DEG C are cooled to through the throttling of first throttle valve, form liquid phase, cold is exported successively by main heat exchanger, liquid phase in azeotrope is by extracting out from main heat exchanger after a part for main heat exchanger, liquid phase in azeotrope is lowered the temperature through second throttle throttling after main heat exchanger cooling, mix with the liquid phase azeotrope of being lowered the temperature by the throttling of first throttle valve laggard enter main heat exchanger rewarming be back to azeotrope compensator,
C nitrogen cycle technique: the nitrogen in nitrogen balance tank is compressed to after 3.2 ~ 3.5MPa through nitrogen compressor, lower the temperature through main heat exchanger, enter in rectifying column by becoming liquid nitrogen after choke valve throttling, with the gas and vapor permeation after tower top rectifying, cold needed for rectifying is provided, the methane condensation of tower top is got off, oxygen concentration is reduced to outside explosion limit simultaneously, become nitrogen then from overhead reflux after the abundant heat exchange of liquid nitrogen, after main heat exchanger rewarming, the deoxygenation of nitrogen purge unit, return nitrogen balance tank.
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