CN104864681A - Method and system for recycling pressure energy of natural gas pipeline network - Google Patents

Method and system for recycling pressure energy of natural gas pipeline network Download PDF

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Publication number
CN104864681A
CN104864681A CN201510287903.7A CN201510287903A CN104864681A CN 104864681 A CN104864681 A CN 104864681A CN 201510287903 A CN201510287903 A CN 201510287903A CN 104864681 A CN104864681 A CN 104864681A
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natural gas
heat exchanger
gas
import
compressor
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CN201510287903.7A
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CN104864681B (en
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陈�峰
梁桂玲
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ENN Science and Technology Development Co Ltd
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ENN Coal Gasification Mining Co Ltd
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0232—Coupling of the liquefaction unit to other units or processes, so-called integrated processes integration within a pressure letdown station of a high pressure pipeline system
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage

Abstract

The invention discloses a method and system for recycling the pressure energy of a natural gas pipeline network. The method includes the steps that raw natural gas is purified through pressure swinging adsorption and then enters a first compressor to be compressed, then heavy hydrocarbon separation is carried out after the natural gas enters a first heat exchanger for heat exchange, separated first-gas-phase matter is divided into two ways, the gas in the first way enters a second heat exchanger, and the gas in the second way enters an expansion machine; the natural gas in the first way enters a gas-liquid separator after heat exchanging is carried out, separated second-gas-phase matter is mixed with the natural gas coming from the expansion machine, then the gas is output from the second heat exchanger after heat exchanging is carried out on the gas and the natural gas in the first way, and mixed with first-liquid-phase matter coming from the heavy hydrocarbon separator , then the mixture enters the first heat exchanger, heat exchanging is carried out on the mixture and the raw natural gas, and then the mixture is conveyed outside. By means of the method and system, the fuel consumed by heating natural gas at present is saved, the coldness obtained by conversion is used for producing liquefied natural gas, the yield of the liquefied natural gas is increased, the use efficiency of the pressure energy is improved, and energy saving and cost reducing are achieved.

Description

A kind of natural gas pipe network pressure energy recoverying and utilizing method and system
Technical field
The invention belongs to exploitation of mineral resources and utilize technical field, being specifically related to a kind of natural gas pipe network pressure energy recoverying and utilizing method and system.
Background technology
Natural gas is a kind of clean energy and industrial chemicals, and China's natural gas long distance pipeline adopts high pressure gas transmission, as " distribution pressure such as West-east Gas and "-Jing two wires, Shan " all reaches 10MPa.Natural gas upstream delivers to each urban gate station or large-scale user by high pressure pipe network.Downstream pipe network just can be entered for user after each natural valve station needs that high-pressure natural gas is decompressed to 0.4MPa.Existing voltage regulating mode is generally by choke valve throttling expansion step-down, but this voltage regulating mode causes pipe network pressure energy to be recycled.In addition, in order to eliminate the low temperature produced in pressure reduction, often with the hot water that gas fired-boiler produces, natural gas being heated, causing energy waste.If this part pressure energy can be recycled, the operating cost that energy utilization rate reduces pipe network can be improved on the one hand, the noise in pressure regulation process and the damage to equipment can be reduced on the other hand.
In prior art, pressure energy of natural gas recycles scheme normally reclaims gas distributing system pressure energy by the particular device such as air wave refrigerating device, decompressor, produce mechanical energy and cold by after natural gas expansion step-down, the aspect such as be applied in generating, ice making, air-conditioning, natural gas liquefaction and lighter hydrocarbons are separated.Wherein, flow and the pressure of pressure energy electrification technique as well as requirement natural gas are relatively stable, but there is serious inhomogeneities in the use of natural gas, so the stable operation of generating equipment cannot be met, and the layout at natural gas pressure regulating station is comparatively disperseed, and small electrical system does not possess the condition of online, be unfavorable for building large-scale power recovery system, can only use by oneself in door station, unnecessary electricity can not store and cause waste.Natural gas liquefaction aspect, because natural gas condensing temperature is at ambient pressure-162 DEG C, required cold energy taste is higher, and the cryogenic compressor of employing depends on import, and cost is high, energy consumption is large.
Summary of the invention
The object of the embodiment of the present invention is to provide a kind of natural gas pipe network pressure energy recoverying and utilizing method and system, to utilize the pressure energy in natural gas pressure reduction fully, optimizes pressure regulation method, improves the efficiency of energy utilization of gas industry.
According to an aspect of the present invention, provide a kind of natural gas pipe network pressure energy recoverying and utilizing method, described method comprises the steps:
By pressure-variable adsorption, raw natural gas is purified;
Raw natural gas after described purification enters the first compressor and compresses;
Raw natural gas after described compression enters First Heat Exchanger from the first import of First Heat Exchanger, carries out heat exchange with the natural gas from First Heat Exchanger second import in described First Heat Exchanger;
The natural gas of described First Heat Exchanger first import is after heat exchange completes, and export from First Heat Exchanger first outlet and enter heavy hydrocarbon knockout drum, isolated first liquid phase mixes with the natural gas exported from the second heat exchanger second; Isolated first gas phase is divided into first via natural gas and the second road natural gas, and described first via natural gas enters the second heat exchanger from the first import of the second heat exchanger, and described second road natural gas enters decompressor; The first via natural gas of described second heat exchanger first import carries out heat exchange with the natural gas from the second heat exchanger second import in described second heat exchanger;
The first outlet from the second heat exchanger after described first via natural gas completes heat exchange in described second heat exchanger exports and enter gas-liquid separator after throttling, isolated second liquid phase enters LNG tank after throttling, isolated second gas phase mixes with the natural gas from decompressor, enters the second heat exchanger from the second import of the second heat exchanger; Described decompressor is coaxial with described first compressor;
After the natural gas of described second heat exchanger second import completes heat exchange in described second heat exchanger, export from the second outlet of described second heat exchanger, after mixing with the first liquid phase from heavy hydrocarbon separator, First Heat Exchanger is entered from the second import of described First Heat Exchanger, and complete heat exchange in described First Heat Exchanger after, be transported to out-of-bounds from the second outlet of described First Heat Exchanger.
In such scheme, described method also comprises: described raw natural gas carried out to purification by pressure-variable adsorption after and enter after the first compressor compresses at described raw natural gas, then by Temp .-changing adsorption, described raw natural gas to be purified.
In such scheme, described method also comprises: enter the first compressor at described raw natural gas and to carry out after compression and before being purified by Temp .-changing adsorption or enter the first compressor at described raw natural gas and carry out compression afterwards and after being purified by Temp .-changing adsorption, purified by Irreversible Adsorption to described raw natural gas.
In such scheme, described method also comprises: described raw natural gas purified after, enter First Heat Exchanger before, carry out dedusting through filter.
In such scheme, described method also comprises: the described natural gas exported from second of First Heat Exchanger the outlet, before being transported to out-of-bounds, separates one regeneration gas as pressure-variable adsorption and/or Temp .-changing adsorption.
In such scheme, described method also comprises: the natural gas in described LNG tank and the raw natural gas entered before First Heat Exchanger first import are carried out heat exchange, after heat exchange completes, the natural gas come from described LNG tank is divided into first strand of natural gas and second strand of natural gas, the fuel gas that described first strand of natural gas heats as regeneration gas, after described second strand of natural gas is compressed, as pressure-variable adsorption subsystem and/or Temp .-changing adsorption subsystem regeneration gas or be transported to the external world.
According to another aspect of the present invention, additionally provide a kind of natural gas pipe network pressure energy recycling system, described system comprises: pressure swing adsorption purge subsystem, the first compressor, First Heat Exchanger, the second heat exchanger, heavy hydrocarbon knockout drum, decompressor, gas-liquid separator, LNG tank; Wherein,
Before described pressure swing adsorption purge subsystem is arranged on described first compressor, for being purified raw natural gas by pressure-variable adsorption;
Described first compressor is arranged between described pressure swing adsorption purge subsystem and First Heat Exchanger, the compression before entering First Heat Exchanger for described raw natural gas from the first import of First Heat Exchanger;
Described First Heat Exchanger comprises the first import, the second import, the first outlet, the second outlet, described first import enters for the raw natural gas after compressing, first outlet is used for the output of the first inlet natural gas, described second import is used for the natural gas that exports from the second heat exchanger second and the entering of mixed gas from the first liquid phase of heavy hydrocarbon separator, second outlet is used for the output of the natural gas of the second import, and described second exports and out-of-bounds communicate; Described First Heat Exchanger is used for the heat exchange of the natural gas of the first import and the natural gas of the second import;
Described second heat exchanger comprises the first import, the second import, the first outlet, the second outlet; Described first outlet is used for the output of the first inlet natural gas, and be connected with the import of described gas-liquid separator, described second outlet is used for the output of the second inlet natural gas, and be connected with the second import of described First Heat Exchanger, described second heat exchanger is used for the heat exchange of the natural gas of the first import and the natural gas of the second import;
Described heavy hydrocarbon knockout drum exports with described First Heat Exchanger first and is connected, and comprise the first liquid phase branch road, the first gas phase branch road, described first gas phase branch road is divided into first via gas phase and the second tunnel gas phase; Described first liquid phase branch road exports with second of described second heat exchanger and is connected, and described first via gas phase is connected with the first import of the second heat exchanger, and described second tunnel gas phase is connected with the import of described decompressor;
The outlet of described decompressor is connected with the second import of described second heat exchanger; Described first compressor is coaxial with described decompressor;
Described gas-liquid separator comprises second liquid phase branch road and the second gas phase branch road, and described second liquid phase branch road is connected with described liquified natural gas tank, and described second gas phase branch road is connected with the second import of described second heat exchanger;
Above-mentioned all being connected all is realized by pipeline.
In such scheme, described system also comprises: Temp .-changing adsorption subsystem, be arranged between described first compressor and described First Heat Exchanger, for described raw natural gas carried out to purification by pressure-variable adsorption after and enter after the first compressor compresses at described raw natural gas, then by Temp .-changing adsorption, described raw natural gas to be purified.
In such scheme, described system also comprises: Irreversible Adsorption purifying subsystem, be arranged between the first compressor and Temp .-changing adsorption subsystem or between Temp .-changing adsorption subsystem and First Heat Exchanger, for being purified described raw natural gas by Irreversible Adsorption.
In such scheme, described system also comprises: filter, before being arranged on First Heat Exchanger, is connected with the first import of First Heat Exchanger, for carrying out dedusting to described raw natural gas.
In such scheme, described system also comprises: regeneration gas branch road, described regeneration gas branch road exports with second of described First Heat Exchanger and is connected, and for the natural gas that exports before being transported to out-of-bounds, separates one regeneration gas as pressure-variable adsorption subsystem and/or Temp .-changing adsorption subsystem.
In such scheme, described system also comprises: the 3rd heat exchanger, the second compressor; Wherein,
Described 3rd heat exchanger is connected with regeneration gas branch road, and be connected with the second compressor, for carrying out heat exchange to the natural gas from LNG tank with the raw natural gas entered before First Heat Exchanger first import, after heat exchange first strand natural gas is sent into regeneration gas branch road, strand natural gas of second after heat exchange is sent into the second compressor;
Described second compressor is connected with pressure-variable adsorption subsystem and/or Temp .-changing adsorption subsystem, for compressing described second strand of natural gas; Or described second compressor communicates with the external world, by described second burst of natural gas transport to out-of-bounds.
The natural gas pipe network pressure energy recoverying and utilizing method that the embodiment of the present invention provides, is purified raw natural gas by pressure-variable adsorption, raw natural gas after described purification enters the first compressor and compresses, raw natural gas enters First Heat Exchanger from the first import of First Heat Exchanger and carries out heat exchange, and then export from First Heat Exchanger first outlet and enter heavy hydrocarbon knockout drum, isolated first liquid phase mixes with the natural gas exported from the second heat exchanger second, isolated first gas phase is divided into first via natural gas and the second road natural gas, and described first via natural gas enters the second heat exchanger from the first import of the second heat exchanger, and described second road natural gas enters decompressor, first via natural gas carries out heat exchange with the natural gas from the second heat exchanger second import in described second heat exchanger, then export from the first outlet of the second heat exchanger and enter gas-liquid separator after throttling, isolated second liquid phase enters LNG tank after throttling, isolated second gas phase mixes with the natural gas from decompressor, the second heat exchanger is entered from the second import of the second heat exchanger, after then described mist and first via natural gas complete heat exchange, export from the second outlet of described second heat exchanger, after mixing with the first liquid phase from heavy hydrocarbon separator, First Heat Exchanger is entered from the second import of described First Heat Exchanger, and complete heat exchange in described First Heat Exchanger after, be transported to out-of-bounds from the second outlet of described First Heat Exchanger.The pressure energy recoverying and utilizing method of the embodiment of the present invention, instead of the step-down technique of existing voltage regulating station, save existing natural gas to heat up the fuel consumed, effectively reclaim pressure energy, meanwhile, cold conversion obtained, for the production of liquefied natural gas, improves the output of liquefied natural gas, effectively improve the utilization ratio of pressure energy, reach energy-saving and cost-reducing object.
Accompanying drawing explanation
In order to be illustrated more clearly in the technical scheme of the embodiment of the present invention, below the accompanying drawing used required in describing embodiment is briefly described, apparently, accompanying drawing in the following describes is only some embodiments of the present invention, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
Fig. 1 is the pressure energy recoverying and utilizing method flow chart of the gas distributing system of the embodiment of the present invention 1;
Fig. 2 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 2;
Fig. 3 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 3;
Fig. 4 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 4;
Fig. 5 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 5;
Fig. 6 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 6;
Fig. 7 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 7;
Fig. 8 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 8;
Fig. 9 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 9;
Figure 10 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 10;
Figure 11 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 11;
Figure 12 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 12;
Figure 13 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 13;
Figure 14 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 14;
Figure 15 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 15;
Figure 16 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 16;
Figure 17 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 17;
Figure 18 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 18;
Figure 19 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 19.
Description of reference numerals:
1-pressure swing adsorption purge subsystem; 2-Temp .-changing adsorption purifying subsystem; 3-Irreversible Adsorption purifying subsystem; 4-first compressor; 5-First Heat Exchanger; 6-heavy hydrocarbon knockout drum; 7-second heat exchanger; 8-decompressor; 9-gas-liquid separator; 10-LNG tank; 11-the 3rd heat exchanger; 12-second compressor; 13-water cooler; 14-filter.
Detailed description of the invention
Those skilled in the art of the present technique are appreciated that unless expressly stated, and singulative used herein " ", " one ", " described " and " being somebody's turn to do " also can comprise plural form.Should be further understood that, the wording used in description of the present invention " comprises " and refers to there is described feature, integer, step, operation, element and/or assembly, but does not get rid of and exist or add other features one or more, integer, step, operation, element, assembly and/or their group.Wording "and/or" used herein comprises one or more arbitrary unit listing item be associated and all combinations.
Those skilled in the art of the present technique are appreciated that unless otherwise defined, and all terms used herein (comprising technical term and scientific terminology) have the meaning identical with the general understanding of the those of ordinary skill in field belonging to the present invention.Should also be understood that those terms defined in such as general dictionary should be understood to have the meaning consistent with the meaning in the context of prior art, unless and define as here, can not explain by idealized or too formal implication.
For ease of the understanding to the embodiment of the present invention, be described below in detail embodiments of the present invention, the embodiment described by reference to accompanying drawing is exemplary, only for explaining the present invention, and can not be interpreted as limitation of the present invention.
The present invention, by exchanging the optimization of compression technology, has effectively reclaimed pressure energy, and meanwhile, cold conversion obtained, for the production of liquefied natural gas, improves the output of liquefied natural gas, effectively improves the utilization ratio of pressure energy, reach energy-saving and cost-reducing object.Below in conjunction with drawings and the specific embodiments, the present invention will be further described.
Fig. 1 is the pressure energy recoverying and utilizing method flow chart of the gas distributing system of the embodiment of the present invention one.
As shown in Figure 1, the natural gas pipe network pressure energy recoverying and utilizing method of the present embodiment, comprises the steps:
Step S101, is purified raw natural gas by pressure-variable adsorption.
Here pressure-variable adsorption, can be realized by pressure-variable adsorption subsystem.The process of pressure-variable adsorption, according to the component content determination technique of natural gas, as dehydration, depickling gas, demercuration, decarburization, takes off heavy hydrocarbon.Under normal circumstances, employing pressure swing adsorption technique removes water, sour gas and the mercury in natural gas.
Above-mentioned purification process, after pressure-variable adsorption, can also carry out Temp .-changing adsorption and/or Irreversible Adsorption.H in natural gas after general purified treatment 2o " 1ppm, CO2 " 50ppm, Hg<0.01ug/Nm 3.Molecular sieve adsorption can also be adopted to remove carbon.Two-stage molecular sieve can be adopted under normal circumstances.
Step S102, the raw natural gas after described purification enters the first compressor and compresses.
Described raw natural gas enters the first compressor and compresses.Here the first compressor, coaxial with the decompressor in the present embodiment, between the first compressor and decompressor, can also speed changer be set.When the power output of decompressor is enough to drive the first compressor operating, control system controls the output shaft of decompressor and is connected with the input of speed changer, and the output of speed changer is connected with the first compressor, drives the first compressor operating by decompressor.When front end tolerance is unstable, when the underpower of decompressor is to drive the first compressor operating, control system controls to disconnect, and the first compressor does not work.
For step S101 and step S102, under normal circumstances, purification process and compression process can exchange order.Before pressure-variable adsorption is arranged on compression process by the present embodiment, is because the process of pressure-variable adsorption can cause natural gas temperature to reduce, then natural gas is compressed, natural gas temperature is raised, thus the waste of the energy can not be caused.
Preferably, at pressure-variable adsorption and compression process complete, before natural gas enters First Heat Exchanger, again Temp .-changing adsorption and/or Irreversible Adsorption are carried out to described natural gas.
Preferably, after pressure-variable adsorption, before compression process, Temp .-changing adsorption is carried out to described raw natural gas; Temp .-changing adsorption and after compression process, then Irreversible Adsorption is carried out to described raw natural gas.
Preferably, after pressure-variable adsorption, before former compression process, Temp .-changing adsorption and Irreversible Adsorption are carried out to described raw natural gas, after Irreversible Adsorption completes, then compress.
Step S103, raw natural gas enters First Heat Exchanger from the first import of First Heat Exchanger, carries out heat exchange with the natural gas from First Heat Exchanger second import in described First Heat Exchanger.
Here raw natural gas can be the natural gas from door station.
Preferably, raw natural gas before entering First Heat Exchanger, through water cooler.Through filter, dedusting can also be carried out.
Step S104, the natural gas of described First Heat Exchanger first import is after heat exchange completes, and export from First Heat Exchanger first outlet and enter heavy hydrocarbon knockout drum, isolated first liquid phase mixes with the natural gas exported from the second heat exchanger second; Isolated first gas phase is divided into first via natural gas and the second road natural gas, and described first via natural gas enters the second heat exchanger from the first import of the second heat exchanger, and described second road natural gas enters decompressor; The first via natural gas of described second heat exchanger first import carries out heat exchange with the natural gas from the second heat exchanger second import in described second heat exchanger.
Preferably, decompressor work in this step coaxially drives the first compressor operating, and the mechanical energy produced expanding becomes the kinetic energy of the first compressor, to the natural gas boosting that upstream high pipeline comes, improve the admission pressure of system, effectively improve the utilization ratio of pressure energy.Meanwhile, cold conversion obtained, for the production of liquefied natural gas (Liquefied natural gas, LNG), improves LNG output.Described decompressor is one-stage expansion machine or multiple expansion engine.
Preferably, in this step the operating temperature of heavy hydrocarbon knockout drum at-30 DEG C to-70 DEG C.
Step S105, the first outlet from the second heat exchanger after described first via natural gas completes heat exchange in described second heat exchanger exports and enter gas-liquid separator after throttling, isolated second liquid phase enters LNG tank after throttling, isolated second gas phase mixes with the natural gas from decompressor, enters the second heat exchanger from the second import of the second heat exchanger.
Preferably, in this step, natural gas in described LNG tank and the raw natural gas entered before First Heat Exchanger first import are carried out heat exchange, after heat exchange completes, the natural gas come from described LNG tank is divided into first strand of natural gas and second strand of natural gas, the fuel gas that described first strand of natural gas heats as regeneration gas; After described second strand of natural gas is compressed, as pressure-variable adsorption subsystem and/or Temp .-changing adsorption subsystem regeneration gas or be transported to out-of-bounds.Here out-of-bounds, can be the downstream gas distributing system of standing corresponding with described door.Here compression, is further: described second strand of natural gas is introduced into the first paragraph of the second compressor, exports, carry out heat exchange, then enter the second segment of the second compressor with described regeneration gas after having compressed from described second compressor first paragraph outlet.In this step, the operating pressure that described gas-liquid separator is arranged is not less than outlet pressure of expansion machine.Preferably, the operating pressure of described gas-liquid separator setting is than outlet pressure of expansion machine height 0.1-0.01Mpa.
Preferably, in this step, natural gas in described LNG tank is entered the second heat exchanger and carries out heat exchange, output after heat exchange completes, then enter First Heat Exchanger and carry out heat exchange, after heat exchange completes, the raw natural gas entered before First Heat Exchanger first import carries out heat exchange, after heat exchange completes, the natural gas come from described LNG tank is divided into first strand of natural gas and second strand of natural gas, the fuel gas that described first strand of natural gas heats as regeneration gas; After described second strand of natural gas is compressed, as pressure-variable adsorption subsystem and/or Temp .-changing adsorption subsystem regeneration gas or be transported to out-of-bounds.Here out-of-bounds, can be the downstream gas distributing system of standing corresponding with described door.Here compression, is further: described second strand of natural gas is introduced into the first paragraph of the second compressor, exports, carry out heat exchange, then enter the second segment of the second compressor with described regeneration gas after having compressed from described second compressor first paragraph outlet.In this step, the operating pressure that described gas-liquid separator is arranged is not less than outlet pressure of expansion machine.Preferably, the operating pressure of described gas-liquid separator setting is than outlet pressure of expansion machine height 0.1-0.01Mpa.
It should be noted that, the purifying subsystem mentioned in the present embodiment and other embodiments refers to pressure-variable adsorption subsystem and/or Temp .-changing adsorption subsystem and/or Irreversible Adsorption subsystem.
Step S106, after the natural gas of described second heat exchanger second import completes heat exchange in described second heat exchanger, export from the second outlet of described second heat exchanger, after mixing with the first liquid phase from heavy hydrocarbon separator, First Heat Exchanger is entered from the second import of described First Heat Exchanger, and complete heat exchange in described First Heat Exchanger after, be transported to out-of-bounds from the second outlet of described First Heat Exchanger.
Here out-of-bounds, can be the downstream gas distributing system of standing corresponding with described door.
In this step, the described natural gas exported from second of First Heat Exchanger the outlet, before being transported to the external world, separates one regeneration gas as pressure-variable adsorption subsystem and/or Temp .-changing adsorption subsystem.During to described regeneration gas heating, adopt electricity or natural gas.Preferably, first adopt heat pump source, ground and/or air pump heat source, and then heat with fuel gas.
The pressure energy recoverying and utilizing method of the embodiment of the present invention, instead of the step-down technique of existing voltage regulating station, the setting of first pressure-variable adsorption recompression, when considering that pressure-variable adsorption gasinlet temperature is lower, adsorption effect is better, therefore recompress after selecting pressure-variable adsorption, otherwise the gas temperature first after compression is higher, the clean-up effect that can affect pressure-variable adsorption has been saved existing natural gas and have been heated up the fuel consumed, effectively reclaim pressure energy, save existing natural gas to heat up the fuel consumed, effectively reclaim pressure energy, simultaneously, decompressor work concentric zones moves compressor operating, the mechanical energy produced expanding becomes the kinetic energy of compressor, to the natural gas boosting that upstream high pipeline comes, improve the admission pressure of system, effectively improve the utilization ratio of pressure energy, in addition, cold conversion obtained is for the production of liquefied natural gas, improve the output of liquefied natural gas, effectively improve the utilization ratio of pressure energy, reach energy-saving and cost-reducing object.
Fig. 2 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 2.
As shown in Figure 2, the pressure energy recycling system of the gas distributing system of the present embodiment, comprising: pressure swing adsorption purge subsystem 1, first compressor 4, First Heat Exchanger 5, second heat exchanger 7, heavy hydrocarbon knockout drum 6, decompressor 8, gas-liquid separator 9, LNG tank 10; Wherein,
Before described pressure swing adsorption purge subsystem (PSA) 1 is arranged on described first compressor 4, for being purified raw natural gas by pressure-variable adsorption;
Described first compressor 4 is arranged between described pressure swing adsorption purge subsystem 1 and First Heat Exchanger 5, enters compression before First Heat Exchanger 5 for described raw natural gas from the first import of First Heat Exchanger;
Described First Heat Exchanger 5 comprises the first import, the second import, the first outlet, the second outlet, described first import enters for the raw natural gas after compressing, first outlet is used for the output of the first inlet natural gas, described second import is used for the natural gas that exports from the second heat exchanger second and the entering of mixed gas from the first liquid phase of heavy hydrocarbon separator, second outlet is used for the output of the natural gas of the second import, and described second exports and out-of-bounds communicate; Described First Heat Exchanger 5 is for the heat exchange of the natural gas of the first import and the natural gas of the second import;
Described second heat exchanger 7 comprises the first import, the second import, the first outlet, the second outlet; Described first outlet is used for the output of the first inlet natural gas, and be connected with the import of described gas-liquid separator, described second outlet is used for the output of the second inlet natural gas, and be connected with the second import of described First Heat Exchanger, described second heat exchanger is used for the heat exchange of the natural gas of the first import and the natural gas of the second import;
Described heavy hydrocarbon knockout drum 6 exports with described First Heat Exchanger 5 first and is connected, and comprise the first liquid phase branch road, the first gas phase branch road, described first gas phase branch road is divided into first via gas phase and the second tunnel gas phase; Described first liquid phase branch road exports with second of described second heat exchanger and is connected, and described first via gas phase is connected with the first import of the second heat exchanger, and described second tunnel gas phase is connected with the import of described decompressor 8;
The outlet of described decompressor 8 is connected with the second import of described second heat exchanger 7; Described first compressor 4 is coaxial with described decompressor 8;
Described gas-liquid separator 9 comprises second liquid phase branch road and the second gas phase branch road, and described second liquid phase branch road is connected with described liquified natural gas tank, and described second gas phase branch road is connected with the second import of described second heat exchanger;
Above-mentioned all being connected all is realized by pipeline.
Preferably, described system also comprises regeneration gas branch road, and described regeneration gas branch road exports with second of described First Heat Exchanger and is connected, and for the natural gas that exports before being transported to out-of-bounds, separates one regeneration gas as pressure-variable adsorption subsystem 1.
Preferably, described system also comprises: the 3rd heat exchanger 11, second compressor 12; Wherein,
Described 3rd heat exchanger 11 is connected with regeneration gas branch road, and be connected with the second compressor 12, for carrying out heat exchange to from the raw natural gas after natural gas and the compression entering before First Heat Exchanger first import of LNG tank, after heat exchange first strand natural gas is sent into regeneration gas branch road, strand natural gas of second after heat exchange is sent into the second compressor 12;
Described second compressor 12 is connected with pressure-variable adsorption subsystem 1, for compressing described second strand of natural gas; Or described second compressor communicates with the external world, by described second burst of natural gas transport to out-of-bounds.
Preferably, the system of the present embodiment can also comprise cooler 13, before being arranged on First Heat Exchanger 5, for the cooling of natural gas.
Preferably, the system of the present embodiment can also comprise filter 14, before being arranged on First Heat Exchanger 5 or between First Heat Exchanger 5 and cooler 13, for dedusting.Filter 14 is shown in Figure 2, and in the other drawings and not shown, but the system shown in other accompanying drawings still can comprise described filter 14.
Below in conjunction with accompanying drawing 2, the workflow of the pressure energy recycling system of the present embodiment is described.
As shown in Figure 2, the pressure energy recycling system of the present embodiment is utilized to carry out in pressure energy recycling process, natural gas A from door station purifies through pressure-variable adsorption subsystem 1, remove water, sour gas, hydro carbons and mercury etc., purified rear natural gas to enter compressor 4 and compress, become high-pressure natural gas B after pressurization, B is through heat exchanger 11 and natural gas (BOG gas) heat exchange from LNG tank, and after 13 cooler coolings, become the high-pressure natural gas C after purification.C enters First Heat Exchanger 5 heat exchange cooling for cryogenic high pressure natural gas E, enter heavy hydrocarbon knockout drum 6, the cryogenic high pressure natural gas removing heavy hydrocarbon divides two-way, one road F enters the heat exchange cooling further of the second heat exchanger 7, one road K enters decompressor 8 and carries out puffing, the Volume Changes that expansion process produces forms mechanical energy, by first compressor 4 coaxial with decompressor 8, is converted into and carries out compression supercharging to the natural gas A from door station.Low-temp low-pressure natural gas S temperature after expanding reduces further, enters the second heat exchanger 7 heat exchange and heats up as low-temp low-pressure natural gas N, enters First Heat Exchanger 5 heat exchange and heats up as Room-temperature low-pressure natural gas O.O is divided into two-way, and a road P enters downstream gas distributing system.The BOG gas R that another road Q and LNG storage tank come 10 mixes, as the regeneration gas Z of cleaning system.
It is cryogenic high pressure natural gas H that F enters the further heat exchange cooling of the second heat exchanger 7, enter LNG gas-liquid separator 9 through expenditure and pressure and carry out gas-liquid separation, the low-temp low-pressure natural gas S of cryogenic high pressure natural gas L after decompression with expansion of generation is mixed into the second heat exchanger 7.Mix through the isolated heavy hydrocarbon species G of heavy hydrocarbon knockout drum 6 with through the natural gas N of the second heat exchanger 7 heat exchange, enter First Heat Exchanger 5.Liquefied natural gas I after LNG gas-liquid separator 9 is separated, enters LNG storage tank 10.
The low-pressure low-temperature BOG gas Y of LNG storage tank 10, after heat exchanger 11 with B heat exchange, through compressor 12 supercharging, becomes gas R, enters regeneration gas Z pipeline, as the regeneration gas of PSA.After regeneration ending, regeneration gas W, enters downstream gas distributing system.
The pressure energy recycling system of the embodiment of the present invention, instead of the step-down technique of existing voltage regulating station, the setting of first pressure-variable adsorption recompression, when considering that pressure-variable adsorption gasinlet temperature is lower, adsorption effect is better, therefore recompress after selecting pressure-variable adsorption, otherwise the gas temperature first after compression is higher, the clean-up effect that can affect pressure-variable adsorption has been saved existing natural gas and have been heated up the fuel consumed, effectively reclaim pressure energy, simultaneously, decompressor work concentric zones moves compressor operating, the mechanical energy produced expanding becomes the kinetic energy of compressor, to the natural gas boosting that upstream high pipeline comes, improve the admission pressure of system, effectively improve the utilization ratio of pressure energy, in addition, cold conversion obtained is for the production of liquefied natural gas, improve the output of liquefied natural gas, effectively improve the utilization ratio of pressure energy, reach energy-saving and cost-reducing object.
Fig. 3 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 3.
As shown in Figure 3, the present embodiment is substantially the same manner as Example 2, difference is, do not comprise the 3rd heat exchanger, the BOG gas that exports in natural storage tank of liquefying enters the second heat exchanger and carries out heat exchange, output after heat exchange completes, then enter First Heat Exchanger and carry out heat exchange, enter the second compressor 12 complete heat exchange in First Heat Exchanger after again.
Fig. 4 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 4.
As shown in Figure 4, the present embodiment is substantially the same manner as Example 2, and difference is, the present embodiment system also comprises Temp .-changing adsorption subsystem 2.
Described Temp .-changing adsorption subsystem 2 is arranged between pressure-variable adsorption subsystem 1 and the first compressor 4, for the further purification of natural gas.Accordingly, from the regeneration gas branch road of the natural gas of the second outlet of First Heat Exchanger 5, be divided into two strands, one is as the regeneration gas of Temp .-changing adsorption subsystem 2, and another strand is as the regeneration gas of pressure-variable adsorption subsystem 1; From the BOG gas of the second compressor 12 as the fuel gas of regeneration gas, be also divided into two strands, one is as the fuel gas of the regeneration gas of Temp .-changing adsorption subsystem 2, and another strand is as the fuel gas of the regeneration gas of pressure-variable adsorption subsystem 1.
Fig. 5 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 5.
As shown in Figure 5, the present embodiment is substantially the same manner as Example 4, difference is, do not comprise the 3rd heat exchanger, the BOG gas that exports in natural storage tank of liquefying enters the second heat exchanger and carries out heat exchange, output after heat exchange completes, then enter First Heat Exchanger and carry out heat exchange, enter the second compressor 12 complete heat exchange in First Heat Exchanger after again.
Fig. 6 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 6.
As shown in Figure 6, the present embodiment is substantially the same manner as Example 4, and difference is, after described Temp .-changing adsorption subsystem 2 is arranged on the first compressor 4.
Fig. 7 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 7.
As shown in Figure 7, the present embodiment is substantially the same manner as Example 5, and difference is, after described Temp .-changing adsorption subsystem 2 is arranged on the first compressor 4.
Fig. 8 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 8.
As shown in Figure 8, the present embodiment is substantially the same manner as Example 4, and difference is, the present embodiment system also comprises Irreversible Adsorption subsystem 3.Described Irreversible Adsorption subsystem 3 is arranged between Temp .-changing adsorption subsystem 2 and the first compressor 4, for doing purification further to described raw natural gas.
Fig. 9 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 9.
As shown in Figure 9, the present embodiment is substantially the same manner as Example 8, difference is, do not comprise the 3rd heat exchanger, the BOG gas that exports in natural storage tank of liquefying enters the second heat exchanger and carries out heat exchange, output after heat exchange completes, then enter First Heat Exchanger and carry out heat exchange, enter the second compressor 12 complete heat exchange in First Heat Exchanger after again.
Figure 10 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 10.
As shown in Figure 10, the present embodiment is substantially the same manner as Example 5, and difference is, the present embodiment system also comprises Irreversible Adsorption subsystem 3.Described Irreversible Adsorption subsystem 3 is arranged between Temp .-changing adsorption subsystem 2 and the first compressor 4, for doing purification further to described raw natural gas.
Figure 11 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 11.
As shown in figure 11, the present embodiment is substantially the same manner as Example 10, difference is, do not comprise the 3rd heat exchanger, the BOG gas that exports in natural storage tank of liquefying enters the second heat exchanger and carries out heat exchange, output after heat exchange completes, then enter First Heat Exchanger and carry out heat exchange, enter the second compressor 12 complete heat exchange in First Heat Exchanger after again.
Figure 12 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 12.
As shown in figure 12, the present embodiment is substantially the same manner as Example 5, and difference is, the present embodiment system also comprises Irreversible Adsorption subsystem 3.After described Irreversible Adsorption subsystem 3 is arranged at the first compressor 4, before First Heat Exchanger 5, for doing purification further to described raw natural gas.
Figure 13 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 13.
As shown in figure 13, the present embodiment is substantially the same manner as Example 12, difference is, do not comprise the 3rd heat exchanger, the BOG gas that exports in natural storage tank of liquefying enters the second heat exchanger and carries out heat exchange, output after heat exchange completes, then enter First Heat Exchanger and carry out heat exchange, enter the second compressor 12 complete heat exchange in First Heat Exchanger after again.
Figure 14 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 14.
As shown in figure 14, the present embodiment is substantially the same manner as Example 4, unlike, the present embodiment also comprises Irreversible Adsorption subsystem 3, and described Irreversible Adsorption subsystem is arranged between pressure-variable adsorption subsystem 1 and Temp .-changing adsorption subsystem 2.
Figure 15 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 15.
As shown in figure 15, the present embodiment is substantially the same manner as Example 14, difference is, do not comprise the 3rd heat exchanger, the BOG gas that exports in natural storage tank of liquefying enters the second heat exchanger and carries out heat exchange, output after heat exchange completes, then enter First Heat Exchanger and carry out heat exchange, enter the second compressor 12 complete heat exchange in First Heat Exchanger after again.
Figure 16 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 16.
As shown in figure 16, the present embodiment is substantially the same manner as Example 2, and difference is, the present embodiment system also comprises Irreversible Adsorption subsystem 3.
Described Irreversible Adsorption subsystem 3 is arranged between pressure-variable adsorption subsystem 1 and the first compressor 4, for the further purification of natural gas.Accordingly, from the regeneration gas branch road of the natural gas of the second outlet of First Heat Exchanger 5, as the regeneration gas of pressure-variable adsorption subsystem 1; BOG gas from the second compressor 12 separates the fuel gas of a branch road as the regeneration gas of pressure-variable adsorption subsystem 1.
Figure 17 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 17.
As shown in figure 17, the present embodiment is substantially the same manner as Example 16, difference is, do not comprise the 3rd heat exchanger, the BOG gas that exports in natural storage tank of liquefying enters the second heat exchanger and carries out heat exchange, output after heat exchange completes, then enter First Heat Exchanger and carry out heat exchange, enter the second compressor 12 complete heat exchange in First Heat Exchanger after again.
Figure 18 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 18.
As shown in figure 18, the present embodiment is substantially the same manner as Example 16, and difference is, after described Irreversible Adsorption subsystem 3 is arranged on the first compressor 4.
Figure 19 is the pressure energy recycling system structural representation of the gas distributing system of the embodiment of the present invention 19.
As shown in figure 19, the present embodiment is substantially the same manner as Example 17, and difference is, after described Irreversible Adsorption subsystem 3 is arranged on the first compressor 4.
The pressure energy recycling system of above-described embodiment, instead of the step-down technique of existing voltage regulating station, the setting of first pressure-variable adsorption recompression, when considering that pressure-variable adsorption gasinlet temperature is lower, adsorption effect is better, therefore recompress after selecting pressure-variable adsorption, otherwise the gas temperature first after compression is higher, the clean-up effect that can affect pressure-variable adsorption has been saved existing natural gas and have been heated up the fuel consumed, effectively reclaim pressure energy, simultaneously, decompressor work concentric zones moves compressor operating, the mechanical energy produced expanding becomes the kinetic energy of compressor, to the natural gas boosting that upstream high pipeline comes, improve the admission pressure of system, effectively improve the utilization ratio of pressure energy, in addition, cold conversion obtained is for the production of liquefied natural gas, improve the output of liquefied natural gas, effectively improve the utilization ratio of pressure energy, reach energy-saving and cost-reducing object.
The above; be only the present invention's preferably detailed description of the invention, but protection scope of the present invention is not limited thereto, is anyly familiar with those skilled in the art in the technical scope that the present invention discloses; the change that can expect easily or replacement, all should be encompassed within protection scope of the present invention.Therefore, protection scope of the present invention should be as the criterion with the protection domain of claim.

Claims (12)

1. a natural gas pipe network pressure energy recoverying and utilizing method, is characterized in that, described method comprises the steps:
By pressure-variable adsorption, raw natural gas is purified;
Raw natural gas after described purification enters the first compressor and compresses;
Raw natural gas after described compression enters First Heat Exchanger from the first import of First Heat Exchanger, carries out heat exchange with the natural gas from First Heat Exchanger second import in described First Heat Exchanger;
The natural gas of described First Heat Exchanger first import is after heat exchange completes, and export from First Heat Exchanger first outlet and enter heavy hydrocarbon knockout drum, isolated first liquid phase mixes with the natural gas exported from the second heat exchanger second; Isolated first gas phase is divided into first via natural gas and the second road natural gas, and described first via natural gas enters the second heat exchanger from the first import of the second heat exchanger, and described second road natural gas enters decompressor; The first via natural gas of described second heat exchanger first import carries out heat exchange with the natural gas from the second heat exchanger second import in described second heat exchanger;
The first outlet from the second heat exchanger after described first via natural gas completes heat exchange in described second heat exchanger exports and enter gas-liquid separator after throttling, isolated second liquid phase enters LNG tank after throttling, isolated second gas phase mixes with the natural gas from decompressor, enters the second heat exchanger from the second import of the second heat exchanger; Described decompressor is coaxial with described first compressor;
After the natural gas of described second heat exchanger second import completes heat exchange in described second heat exchanger, export from the second outlet of described second heat exchanger, after mixing with the first liquid phase from heavy hydrocarbon separator, First Heat Exchanger is entered from the second import of described First Heat Exchanger, and complete heat exchange in described First Heat Exchanger after, be transported to out-of-bounds from the second outlet of described First Heat Exchanger.
2. pressure energy recoverying and utilizing method according to claim 1, it is characterized in that, described method also comprises: described raw natural gas carried out to purification by pressure-variable adsorption after and enter after the first compressor compresses at described raw natural gas, then by Temp .-changing adsorption, described raw natural gas to be purified.
3. pressure energy recoverying and utilizing method according to claim 2, it is characterized in that, described method also comprises: enter the first compressor at described raw natural gas and to carry out after compression and before being purified by Temp .-changing adsorption or enter the first compressor at described raw natural gas and carry out compression afterwards and after being purified by Temp .-changing adsorption, purified by Irreversible Adsorption to described raw natural gas.
4. pressure energy recoverying and utilizing method according to claim 1, is characterized in that, described method also comprises: described raw natural gas purified after, enter First Heat Exchanger before, carry out dedusting through filter.
5. the pressure energy recoverying and utilizing method according to any one of Claims 1-4, it is characterized in that, described method also comprises: the described natural gas exported from second of First Heat Exchanger the outlet, before being transported to out-of-bounds, separates one regeneration gas as pressure-variable adsorption and/or Temp .-changing adsorption.
6. pressure energy recoverying and utilizing method according to claim 5, it is characterized in that, described method also comprises: the natural gas in described LNG tank and the raw natural gas entered before First Heat Exchanger first import are carried out heat exchange, after heat exchange completes, the natural gas come from described LNG tank is divided into first strand of natural gas and second strand of natural gas, the fuel gas that described first strand of natural gas heats as regeneration gas, after described second strand of natural gas is compressed, as pressure-variable adsorption subsystem regeneration gas or be transported to the external world.
7. a natural gas pipe network pressure energy recycling system, it is characterized in that, described system comprises: pressure swing adsorption purge subsystem, the first compressor, First Heat Exchanger, the second heat exchanger, heavy hydrocarbon knockout drum, decompressor, gas-liquid separator, LNG tank; Wherein,
Before described pressure swing adsorption purge subsystem is arranged on described first compressor, for being purified raw natural gas by pressure-variable adsorption;
Described first compressor is arranged between described pressure swing adsorption purge subsystem and First Heat Exchanger, the compression before entering First Heat Exchanger for described raw natural gas from the first import of First Heat Exchanger;
Described First Heat Exchanger comprises the first import, the second import, the first outlet, the second outlet, described first import enters for the raw natural gas after compressing, first outlet is used for the output of the first inlet natural gas, described second import is used for the natural gas that exports from the second heat exchanger second and the entering of mixed gas from the first liquid phase of heavy hydrocarbon separator, second outlet is used for the output of the natural gas of the second import, and described second exports and out-of-bounds communicate; Described First Heat Exchanger is used for the heat exchange of the natural gas of the first import and the natural gas of the second import;
Described second heat exchanger comprises the first import, the second import, the first outlet, the second outlet; Described first outlet is used for the output of the first inlet natural gas, and be connected with the import of described gas-liquid separator, described second outlet is used for the output of the second inlet natural gas, and be connected with the second import of described First Heat Exchanger, described second heat exchanger is used for the heat exchange of the natural gas of the first import and the natural gas of the second import;
Described heavy hydrocarbon knockout drum exports with described First Heat Exchanger first and is connected, and comprise the first liquid phase branch road, the first gas phase branch road, described first gas phase branch road is divided into first via gas phase and the second tunnel gas phase; Described first liquid phase branch road exports with second of described second heat exchanger and is connected, and described first via gas phase is connected with the first import of the second heat exchanger, and described second tunnel gas phase is connected with the import of described decompressor;
The outlet of described decompressor is connected with the second import of described second heat exchanger; Described first compressor is coaxial with described decompressor;
Described gas-liquid separator comprises second liquid phase branch road and the second gas phase branch road, and described second liquid phase branch road is connected with described liquified natural gas tank, and described second gas phase branch road is connected with the second import of described second heat exchanger;
Above-mentioned all being connected all is realized by pipeline.
8. pressure energy recycling system according to claim 7, it is characterized in that, described system also comprises: Temp .-changing adsorption subsystem, be arranged between described first compressor and described First Heat Exchanger, for described raw natural gas carried out to purification by pressure-variable adsorption after and enter after the first compressor compresses at described raw natural gas, then by Temp .-changing adsorption, described raw natural gas to be purified.
9. pressure energy recycling system according to claim 8, it is characterized in that, described system also comprises: Irreversible Adsorption purifying subsystem, be arranged between the first compressor and Temp .-changing adsorption subsystem or between Temp .-changing adsorption subsystem and First Heat Exchanger, for being purified described raw natural gas by Irreversible Adsorption.
10. pressure energy recycling system according to claim 7, is characterized in that, described system also comprises: filter, before being arranged on First Heat Exchanger, is connected with the first import of First Heat Exchanger, for carrying out dedusting to described raw natural gas.
11. pressure energy recycling systems according to any one of claim 7 to 10, it is characterized in that, described system also comprises: regeneration gas branch road, described regeneration gas branch road exports with second of described First Heat Exchanger and is connected, for the natural gas that exports before being transported to out-of-bounds, separate one regeneration gas as pressure-variable adsorption subsystem and/or Temp .-changing adsorption subsystem.
12. pressure energy recycling systems according to claim 11, it is characterized in that, described system also comprises: the 3rd heat exchanger, the second compressor; Wherein,
Described 3rd heat exchanger is connected with regeneration gas branch road, and be connected with the second compressor, for carrying out heat exchange to the natural gas from LNG tank with the raw natural gas entered before First Heat Exchanger first import, after heat exchange first strand natural gas is sent into regeneration gas branch road, strand natural gas of second after heat exchange is sent into the second compressor;
Described second compressor is connected with pressure-variable adsorption subsystem and/or Temp .-changing adsorption subsystem, for compressing described second strand of natural gas; Or described second compressor communicates with the external world, by described second burst of natural gas transport to out-of-bounds.
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