CN104110940A - Efficient air separation device utilizing liquefied natural gas cold energy - Google Patents
Efficient air separation device utilizing liquefied natural gas cold energy Download PDFInfo
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- CN104110940A CN104110940A CN201410277359.3A CN201410277359A CN104110940A CN 104110940 A CN104110940 A CN 104110940A CN 201410277359 A CN201410277359 A CN 201410277359A CN 104110940 A CN104110940 A CN 104110940A
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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
- F25J3/04—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 for air
- F25J3/04406—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 for air using a dual pressure main column system
- F25J3/04412—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 for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure 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
- 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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams 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
- 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
- F25J3/04—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 for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
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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
- F25J3/04—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 for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
- F25J3/04224—Cores associated with a liquefaction or 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
- 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
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
- F25J3/0426—The cryogenic component does not participate in the fractionation
- F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
- F25J3/04272—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons and comprising means for reducing the risk of pollution of hydrocarbons into the air fractionation
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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
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
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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
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
Abstract
The invention discloses an efficient air separation device utilizing liquefied natural gas cold energy. The efficient air separation device utilizing the liquefied natural gas cold energy comprises a heat exchanger between low-temperature NG and an ethylene glycol water solution, an LNG heat exchanger, a main heat exchanger, a supercooling heat exchanger, a first nitrogen compressor, a second nitrogen compressor, a third nitrogen compressor, a raw material air compressor, a lower tower, an upper tower, an air cooler, an ethylene glycol water solution circulating pump, a gas-liquid separator and a condensation evaporator. According to the efficient air separation device utilizing the liquefied natural gas cold energy, after low-temperature cold energy of LNG is applied to an air separation system, the unit power consumption of a liquid air separation product can be reduced to be just about one third that of a liquid air separation product produced according to the conventional process; due to the fact that an ethylene glycol water solution is used for cooling, the shaft power of the air compressor can be effectively reduced; due to the fact that high-temperature cold energy of NG is used, the utilization rate of cold energy of the LNG is fully increased, and the NG from the air separation system meets the pipe delivery requirement.
Description
Technical field
The present invention relates to natural gas field, in particular to a kind of efficient air separation unit that utilizes cold energy of liquefied natural gas.
Background technology
LNG (Liquefied Natural Gas) is that natural gas processes through dehydration, desulfurization and cryogenic technique liquefaction the cryogenic liquid mixture forming.Its storing temperature is-162 ℃, and storage density is generally 430～470kg/m
3.During use, LNG need to be converted into the gas of normal temperature, in vaporescence, liberated heat is about 830kJ/kg.If do not recycled, will be great waste.At present, the mode of utilizing of LNG cold energy mainly contains: cold energy generation, air separation, food product refrigeration low-temperature receiver, manufacture liquid CO
2and low-temperature grinding etc.According to the cryogenic cold energy principle that low temperature utilizes as far as possible, air separation is the most a kind of mode of utilizing of LNG cold energy use.
The air separating method that air separating method is particularly produced the liquid space division products such as liquid oxygen, liquid nitrogen and liquid argon needs a large amount of low temperature colds.Conventional way is to be cooled to set point of temperature laggard one or two booster expansion turbine swell refrigerations to provide space division system required cold with one pressure-air or high pressure nitrogen.The compression of gas need to consume a large amount of electric power and cooling water.Therefore the unit power consumption of this conventional its liquid space division product of class space division system is very high.For the current domestic existing LNG cold energy that utilizes for some patented technologies of space division system, its technical characterstic is mainly, adopt normal temperature air inlet low pressure and medium pressure nitrogen press, compressor shaft power is higher, and does not utilize glycol water cooling system, not only makes raw material air compressor machine shaft power higher, the high temperature cold energy of NG is also underused, cause the specific energy consumption of product higher, and the NG that goes out space division system still locates low temperature, can not meet the defeated requirement of pipe.
Summary of the invention
The invention provides a kind of efficient air separation unit that utilizes cold energy of liquefied natural gas, in order to solve at least one problem existing in prior art.
For achieving the above object, the invention provides a kind of efficient air separation unit that utilizes cold energy of liquefied natural gas, comprising: the heat exchanger of low temperature NG and glycol water, LNG heat exchanger, main heat exchanger, crosses cold heat exchanger, the first nitrogen compressor, the second nitrogen compressor, the 3rd nitrogen compressor, raw material air compressor machine, lower tower, upper tower, aerial cooler, the circulating pump of glycol water, gas-liquid separator, and condenser/evaporator, wherein:
Described raw material air compressor machine is arranged in air conveyance lines, after described air conveyance lines, pass successively described aerial cooler, described main heat exchanger, the described cold heat exchanger of crossing, and be connected with described lower tower, air after the compression of described raw material air compressor machine in described aerial cooler the spent glycol aqueous solution cooling, and then through described main heat exchanger and described mistake after cold heat exchanger is lowered the temperature, send into described lower tower again, at described lower tower, after initial gross separation, at described lower tower bottom, obtain oxygen-enriched liquid air, at described lower top of tower, obtain low temperature pure nitrogen gas and liquid nitrogen, wherein, described condenser/evaporator is arranged between described lower tower and described upper tower, the opening of described condenser/evaporator communicates with described lower top of tower,
The circulating pump of described glycol water is arranged on the glycol circulation pipeline of sealing, described glycol circulation pipeline passes respectively heat exchanger and the described aerial cooler of described low temperature NG and glycol water, under the circulating pump ringing of described glycol water, the glycol water in described glycol circulation pipeline provides air cooling required cold energy for described aerial cooler;
The the first pure nitrogen gas feed-line being connected with described lower top of tower is successively through described cold heat exchanger and the described main heat exchanger crossed, low temperature pure nitrogen gas is wherein crossed cold heat exchanger and described main heat exchanger provides cold energy for described, afterwards with the entrance that enters described the first nitrogen compressor together with low-temp low-pressure nitrogen air shooter line from described gas-liquid separator;
The liquid nitrogen feed-line being connected with described upper top of tower is sent the liquid nitrogen after decompression cooling into described upper tower, as the phegma of described upper tower; The oxygen-enriched liquid air feed-line being connected with described lower tower enters described upper tower by the oxygen-enriched liquid air after throttling cooling and carries out rectifying, and from described, top of tower obtains pure nitrogen gas, and from described, tower top obtains dirty nitrogen, and from described, tower bottom obtains pure liquid oxygen product;
The the second pure nitrogen gas feed-line being connected with described upper top of tower is successively through described cold heat exchanger and the described main heat exchanger crossed, and low temperature pure nitrogen gas is wherein crossed cold heat exchanger and described main heat exchanger provides cold energy for described;
The dirty nitrogen feed-line being connected with described upper tower top is successively through described cold heat exchanger and the described main heat exchanger crossed, and the dirty nitrogen of low temperature is wherein crossed cold heat exchanger and described main heat exchanger provides cold energy for described;
The pipeline being connected with the outlet of described the first nitrogen compressor is through described LNG heat exchanger, pure nitrogen gas is after compression sent into described LNG heat exchanger cooling, and then be connected with the entrance of described the second nitrogen compressor, the pipeline being connected with the outlet of described the second nitrogen compressor is through described LNG heat exchanger, pure nitrogen gas wherein is further cooling, and then be connected with the entrance of described the 3rd nitrogen compressor, the gas-liquid separator intake pipeline being connected with the outlet of described the 3rd nitrogen compressor is through described LNG heat exchanger, and pure nitrogen gas wherein is further cooling;
The end of described gas-liquid separator intake pipeline is connected with described gas-liquid separator, described gas-liquid separator carries out gas-liquid separation by the liquid nitrogen entering wherein, in described gas-liquid separator bottom, obtain liquid nitrogen product, at described gas-liquid separator top, obtain low-pressure low-temperature nitrogen, wherein, the entrance of described the first nitrogen compressor sent into the low-pressure low-temperature nitrogen after separated by the pipeline connected with described gas-liquid separator top;
LNG pipeline is successively through the heat exchanger of described LNG heat exchanger and described low temperature NG and glycol water, and the heat exchanger that the ducted liquefied natural gas of described LNG is described LNG heat exchanger and described low temperature NG and glycol water enters natural gas pipeline after providing cold energy gasification for natural gas.
Further, the dirty nitrogen of the low temperature in described dirty nitrogen feed-line provides cold energy re-heat to emptying after the dirty nitrogen of normal temperature for described cold heat exchanger and the described main heat exchanger crossed.
Further, the low temperature pure nitrogen gas in described the second pure nitrogen gas feed-line for described cross cold heat exchanger and described main heat exchanger provide cold energy re-heat to the low-pressure nitrogen of normal temperature for collection.
Further, on described oxygen-enriched liquid air feed-line, be provided with valve.
Further, on described liquid nitrogen feed-line, be provided with valve.
Further, the end of described gas-liquid separator intake pipeline is provided with valve.
Accompanying drawing explanation
In order to be illustrated more clearly in the embodiment of the present invention or technical scheme of the prior art, to the accompanying drawing of required use in embodiment or description of the Prior Art be briefly described below, apparently, accompanying drawing in the following describes is only some embodiments of the present invention, for those of ordinary skills, do not paying under the prerequisite of creative work, can also obtain according to these accompanying drawings other accompanying drawing.
Fig. 1 is the efficient air separation unit schematic diagram that utilizes cold energy of liquefied natural gas of one embodiment of the invention.
The specific embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is clearly and completely described, obviously, described embodiment is only the present invention's part embodiment, rather than whole embodiment.Embodiment based in the present invention, those of ordinary skills, not paying the every other embodiment obtaining under creative work prerequisite, belong to the scope of protection of the invention.
Fig. 1 is the efficient air separation unit schematic diagram that utilizes cold energy of liquefied natural gas of one embodiment of the invention.In figure, equipment serial number is as follows: 1 is the heat exchanger of low temperature NG and glycol water, 2 is LNG heat exchanger, and 3 is main heat exchanger, and 4 was cold heat exchanger, 5,6 and 7 be respectively first, second, and third nitrogen compressor, 8 is raw material air compressor machine, and 9 is lower tower, and 10 is upper tower, 11 is aerial cooler, 12 is the circulating pump of glycol water, and 13 is gas-liquid separator, and 14 is condenser/evaporator.Relevant logistics numbering is as follows: 101 is raw air, 102 is low temperature approaches saturated mode gaseous air, 103 is the liquid air that lower tower, 104 is the dirty nitrogen that upper tower, and 105 is the pure nitrogen gas that upper tower, and 106 is the middle pressure low temperature nitrogen that lower tower, 107 is the dirty nitrogen of re-heat to normal temperature, 108 is the gas nitrogen of re-heat to normal temperature, and 109 is liquid oxygen product, and 110 is liquid nitrogen.201 is the low temperature nitrogen of the first nitrogen compressor outlet, and 202 is the low temperature nitrogen of the second nitrogen compressor outlet, and 203 is the low temperature nitrogen of the 3rd nitrogen compressor outlet, and 204 is highly pressurised liquid nitrogen, and 205 is low-pressure low-temperature nitrogen, and 206 is liquid nitrogen product.301 is glycol water, 302 be with NG heat exchange after glycol water, 401 for entering the liquefied natural gas of space division system, 402 for removing the natural gas of gas pipeline.
As shown in the figure, raw material air compressor machine 8 is arranged in air conveyance lines, after air conveyance lines, pass successively aerial cooler 11, main heat exchanger 3, cross cold heat exchanger 4, and be connected with lower tower 9, originally air 101 is more than overcompression reaches 0.5MPa, the spent glycol aqueous solution is cooling, and air is sent into lower tower 9 at main heat exchanger 3 and after cold heat exchanger 4 cools to 1 ℃～5 ℃ (274～278K) excessively.Air obtains oxygen-enriched liquid air 103 (170 ℃～-175 ℃) after initial gross separation in bottom at lower tower 9, at lower top of tower, obtain pure nitrogen gas 106 (170 ℃～-175 ℃) and liquid nitrogen 110.Wherein, condenser/evaporator 14 is arranged between lower tower 9 and upper tower 10, and the opening of condenser/evaporator 14 communicates with lower tower 9 tops.
The circulating pump 12 of glycol water is arranged on the glycol circulation pipeline of sealing, glycol circulation pipeline passes respectively heat exchanger 1 and the aerial cooler 11 of low temperature NG and glycol water, under circulating pump 12 ringings of glycol water, the glycol water in glycol circulation pipeline is the aerial cooler 11 cooling required cold energy of air of supplying raw materials;
The the first pure nitrogen gas feed-line being connected with lower tower 9 tops passed cold heat exchanger 4 and main heat exchanger 3 successively, and pure nitrogen gas wherein with low-pressure low-temperature nitrogen 205 (100 ℃～-150 ℃) together with enters the entrance of first nitrogen compressor 7 after cold is provided through crossing cold heat exchanger 4 and main heat exchanger 3 for these two heat exchangers.
The liquid nitrogen feed-line being connected with upper tower 10 tops is sent the liquid nitrogen after decompression cooling into upper tower 10, as the phegma of upper tower 10; The oxygen-enriched liquid air feed-line being connected with lower tower 9 enters upper tower 10 by the oxygen-enriched liquid air after throttling cooling and carries out rectifying, from upper top of tower, obtains pure nitrogen gas 105, and upper tower top obtains dirty nitrogen 104, and upper tower bottom obtains pure liquid oxygen product 109.Then, low-pressure low-temperature pure nitrogen gas 105 and dirty nitrogen 104 all respectively by the second pure nitrogen gas feed-line and dirty nitrogen feed-line for main heat exchanger 3 with cross cold heat exchanger 4 cold is provided.In addition, re-heat can be emptying to the dirty nitrogen 107 of normal temperature, and re-heat is available to the low normal pressure and temperature nitrogen 108 of normal temperature.
After the first nitrogen compressor 7 low temperature compressions, from 201 (9～12bar) that export out, enter LNG heat exchanger 2 cooling, and then enter the second nitrogen compressor 5 low temperature compressions, that from the second nitrogen compressor 5, export out is 202 (28～30bar), it is cooling that nitrogen 202 continues to enter LNG heat exchanger 2, after obtaining low temperature, enter the 3rd nitrogen compressor 6 low temperature compressions, the high pressure nitrogen 203 (39～42bar) that exports out from it is cooling by LNG LNG heat exchanger 2, liquefies and crosses cold one-tenth high pressure overfreezing liquid nitrogen 204.
The end of gas-liquid separator intake pipeline is connected with gas-liquid separator 13, gas-liquid separator carries out gas-liquid separation by entering the decompression wherein liquid nitrogen to atmospheric pressure state, in gas-liquid separator bottom, obtain liquid nitrogen product 206, at gas-liquid separator top, obtain low-pressure low-temperature nitrogen 205, wherein, the entrance of the first nitrogen compressor sent into the low-pressure low-temperature nitrogen after separated by the pipeline connected with gas-liquid separator top.
LNG pipeline is successively through the heat exchanger 1 of LNG heat exchanger 2 and low temperature NG and glycol water, and the heat exchanger that the ducted liquefied natural gas of LNG is LNG heat exchanger and low temperature NG and glycol water enters natural gas pipeline after providing cold energy gasification for natural gas.
Wherein, on oxygen-enriched liquid air feed-line, also can be provided with valve.
Wherein, on liquid nitrogen feed-line, also can be provided with valve.
Wherein, the end of gas-liquid separator intake pipeline also can be provided with valve, as being pressure-reducing valve.
In sum, beneficial effect of the present invention is:
1, proposed a kind of air-separating plant of the LNG of utilization cold energy, for after space division system, can make the unit power consumption of liquid space division product only reduce as approximately 1/3 of the liquid space division product of old process production the cryogenic cold energy of LNG.
2, adopt glycol water cooling system, effectively reduce the shaft power of air compressor machine, and the high temperature cold energy of NG is also utilized, fully improved the utilization rate of LNG cold energy, make out the NG of space division system meet the defeated requirement of pipe.
3, adopt the nitrogen compressor of three sections of low temperature air inlets, utilize the cold energy of LNG, high pressure nitrogen is cooled to liquid nitrogen product, and this technology is compared and in rectifying column, is directly extracted the power consumption that liquid nitrogen product effectively reduces rectifying column, can save energy consumption 30% with the existing air-separating plant comparison of same size.
4, at upper top of tower, extract one pure gas nitrogen out, with air generation heat exchange, not only utilized the low temperature of gas nitrogen, and made space division system can produce the nitrogen product of giving vent to anger.
One of ordinary skill in the art will appreciate that: accompanying drawing is the schematic diagram of an embodiment, the module in accompanying drawing or flow process might not be that enforcement the present invention is necessary.
One of ordinary skill in the art will appreciate that: the module in the device in embodiment can be described and be distributed in the device of embodiment according to embodiment, also can carry out respective change and be arranged in the one or more devices that are different from the present embodiment.The module of above-described embodiment can be merged into a module, also can further split into a plurality of submodules.
Finally it should be noted that: above embodiment only, in order to technical scheme of the present invention to be described, is not intended to limit; Although the present invention is had been described in detail with reference to previous embodiment, those of ordinary skill in the art is to be understood that: its technical scheme that still can record previous embodiment is modified, or part technical characterictic is wherein equal to replacement; And these modifications or replacement do not make the essence of appropriate technical solution depart from the spirit and scope of embodiment of the present invention technical scheme.
Claims (6)
1. an efficient air separation unit that utilizes cold energy of liquefied natural gas, is characterized in that, comprising: the heat exchanger of low temperature NG and glycol water, LNG heat exchanger, main heat exchanger, crosses cold heat exchanger, the first nitrogen compressor, the second nitrogen compressor, the 3rd nitrogen compressor, raw material air compressor machine, lower tower, upper tower, aerial cooler, the circulating pump of glycol water, gas-liquid separator, and condenser/evaporator, wherein:
Described raw material air compressor machine is arranged in air conveyance lines, after described air conveyance lines, pass successively described aerial cooler, described main heat exchanger, the described cold heat exchanger of crossing, and be connected with described lower tower, air after the compression of described raw material air compressor machine in described aerial cooler the spent glycol aqueous solution cooling, and then through described main heat exchanger and described mistake after cold heat exchanger is lowered the temperature, send into described lower tower again, at described lower tower, after initial gross separation, at described lower tower bottom, obtain oxygen-enriched liquid air, at described lower top of tower, obtain low temperature pure nitrogen gas and liquid nitrogen, wherein, described condenser/evaporator is arranged between described lower tower and described upper tower, the opening of described condenser/evaporator communicates with described lower top of tower,
The circulating pump of described glycol water is arranged on the glycol circulation pipeline of sealing, described glycol circulation pipeline passes respectively heat exchanger and the described aerial cooler of described low temperature NG and glycol water, under the circulating pump ringing of described glycol water, the glycol water in described glycol circulation pipeline provides air cooling required cold energy for described aerial cooler;
The the first pure nitrogen gas feed-line being connected with described lower top of tower is successively through described cold heat exchanger and the described main heat exchanger crossed, low temperature pure nitrogen gas is wherein crossed cold heat exchanger and described main heat exchanger provides cold energy for described, afterwards with the entrance that enters described the first nitrogen compressor together with low-temp low-pressure nitrogen air shooter line from described gas-liquid separator;
The liquid nitrogen feed-line being connected with described upper top of tower is sent the liquid nitrogen after decompression cooling into described upper tower, as the phegma of described upper tower; The oxygen-enriched liquid air feed-line being connected with described lower tower enters described upper tower by the oxygen-enriched liquid air after throttling cooling and carries out rectifying, and from described, top of tower obtains pure nitrogen gas, and from described, tower top obtains dirty nitrogen, and from described, tower bottom obtains pure liquid oxygen product;
The the second pure nitrogen gas feed-line being connected with described upper top of tower is successively through described cold heat exchanger and the described main heat exchanger crossed, and low temperature pure nitrogen gas is wherein crossed cold heat exchanger and described main heat exchanger provides cold energy for described;
The dirty nitrogen feed-line being connected with described upper tower top is successively through described cold heat exchanger and the described main heat exchanger crossed, and the dirty nitrogen of low temperature is wherein crossed cold heat exchanger and described main heat exchanger provides cold energy for described;
The pipeline being connected with the outlet of described the first nitrogen compressor is through described LNG heat exchanger, pure nitrogen gas is after compression sent into described LNG heat exchanger cooling, and then be connected with the entrance of described the second nitrogen compressor, the pipeline being connected with the outlet of described the second nitrogen compressor is through described LNG heat exchanger, pure nitrogen gas wherein is further cooling, and then be connected with the entrance of described the 3rd nitrogen compressor, the gas-liquid separator intake pipeline being connected with the outlet of described the 3rd nitrogen compressor is through described LNG heat exchanger, and pure nitrogen gas wherein is further cooling;
The end of described gas-liquid separator intake pipeline is connected with described gas-liquid separator, described gas-liquid separator carries out gas-liquid separation by the liquid nitrogen entering wherein, in described gas-liquid separator bottom, obtain liquid nitrogen product, at described gas-liquid separator top, obtain low-pressure low-temperature nitrogen, wherein, the entrance of described the first nitrogen compressor sent into the low-pressure low-temperature nitrogen after separated by the pipeline connected with described gas-liquid separator top;
LNG pipeline is successively through the heat exchanger of described LNG heat exchanger and described low temperature NG and glycol water, and the heat exchanger that the ducted liquefied natural gas of described LNG is described LNG heat exchanger and described low temperature NG and glycol water enters natural gas pipeline after providing cold energy gasification for natural gas.
2. efficient air separation unit according to claim 1, is characterized in that, the dirty nitrogen of low temperature in described dirty nitrogen feed-line provides cold energy re-heat to emptying after the dirty nitrogen of normal temperature for described cold heat exchanger and the described main heat exchanger crossed.
3. efficient air separation unit according to claim 1, is characterized in that, the low temperature pure nitrogen gas in described the second pure nitrogen gas feed-line for described cross cold heat exchanger and described main heat exchanger provide cold energy re-heat to the low-pressure nitrogen of normal temperature for collection.
4. efficient air separation unit according to claim 1, is characterized in that, on described oxygen-enriched liquid air feed-line, is provided with valve.
5. efficient air separation unit according to claim 1, is characterized in that, on described liquid nitrogen feed-line, is provided with valve.
6. efficient air separation unit according to claim 1, is characterized in that, the end of described gas-liquid separator intake pipeline is provided with valve.
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