CN103994635A - Device and method for recovering light hydrocarbon through cold energy of LNG - Google Patents
Device and method for recovering light hydrocarbon through cold energy of LNG Download PDFInfo
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- CN103994635A CN103994635A CN201410191260.1A CN201410191260A CN103994635A CN 103994635 A CN103994635 A CN 103994635A CN 201410191260 A CN201410191260 A CN 201410191260A CN 103994635 A CN103994635 A CN 103994635A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
- F25J3/0214—Liquefied natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/62—Ethane or ethylene
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
Abstract
The invention discloses a device and method for recovering light hydrocarbon through cold energy of LNG. The LNG in an LNG storage tank is pressurized and pumped out by a first pressure pump to a master LNG output pipe; the LNG is divided into two flows by a first flow distribution device; the two flows flow into a first LNG output pipe and a second LNG output pipe respectively; heat of the LNG flow in the first LNG output pipe is exchanged by a first heat exchanger, and then the LNG flow in the first LNG output pipe flows into the upper portion of a demethanizer through a third heat exchange output pipe; heat of the LNG flow in the second LNG output pipe is exchanged by a second heat exchanger, and then the LNG flow in the second LNG output pipe flows into the middle of the demethanizer through a seventeenth heat exchange output pipe; the demethanizer carries out distillation separation on the LNG flow flowing into the upper area of the demethanizer and the LNG flow flowing into the middle area of the demethanizer, lean gas is generated at the top of the demethanizer, and C2+ is obtained at the bottom of the demethanizer; the lean gas is used for heat exchange output of the first heat exchanger after heat exchange condensation; the C2+ is fed into a deethanizer for distillation separation, the main component of gas generated at the top of the deethanizer is ethane, LPG is obtained at the bottom of the deethanizer, and the LPG is pressurized, pumped out and stored in an LPG storage tank.
Description
Technical field
The present invention relates to lighter hydrocarbons recovery field, in particular to a kind of apparatus and method of utilizing cold energy of liquefied natural gas to reclaim lighter hydrocarbons condensation simultaneously lean gas.
Background technology
Along with the world is day by day vigorous to the demand of the energy, traditional energy resource structure has been difficult to meet multiple demands, natural gas has become the third-largest energy after coal, oil, and as a kind of high-quality, efficient, the clean energy, its ratio shared in Energy Mix improves day by day.The liquefaction accumulating of natural gas is conducive to realize distributing rationally of resource.Liquefied natural gas (LNG, Liquefied Natural Gas), except mainly containing methane, also has a small amount of ethane, propane and butane, also may contain nitrogen in addition.According to the difference of C2+ lighter hydrocarbons content in LNG, LNG can be divided into lean gas and rich gas.At present, on international LNG market, having quite a few is rich gas (contain more than 10% C2, the C3 of mass fraction, and a small amount of C4 hydro carbons).C2+ lighter hydrocarbons in rich gas are a kind of high-quality and widely used industrial chemicals, have very high added value, with it, replace naphtha can reduce investment outlay 30% as the raw material of ethene, ethylene unit Energy Intensity Reduction 30～40%, and integrated cost reduces by 10% left and right.
LNG under normal pressure is the liquid of-161 ℃, has contained a large amount of high-quality cold energy.LNG needs gasification before being transported to pipe network user, and gasification normally utilizes seawater or air heat to realize, although this method is simply direct, has wasted the cold energy of a large amount of preciousnesses of containing in LNG.The cold energy that LNG under 0.1MPa discharges during from-161 ℃ of re-heats to 27 ℃ is about 950KJ/Kg, and the huge high-quality cold energy that LNG contains will be great waste if do not recycled.Therefore, utilize the cold of LNG self, with lower cost by the lighter hydrocarbons resource separation in rich gas out, be conducive to realize the complex optimum utilization of natural gas resource.
Because the LNG industry of China is just at the early-stage, the current domestic report that rarely has relevant LNG lighter hydrocarbons isolation technics, and as far back as the sixties in last century, just had the technical literature of LNG lighter hydrocarbons separation abroad.In the U.S., from LNG, isolating C2+ lighter hydrocarbons has become the important means that regulates heating value of natural gas to make it to meet American National combustion gas standard.In recent years, LNG lighter hydrocarbons isolation technics is in the states such as the U.S., Japan got back significant progress and application, and Zhe Wei China separated lighter hydrocarbons from the LNG rich gas of coastal introduction play good directive function.Along with the foundation of China's relevant criterion and standard and sound, from LNG, reclaim lighter hydrocarbons and certainly will play and increase LNG receiving station operating flexibility, adapt to user's request diversity and improve many-sided demand of factory economy type.
Summary of the invention
The invention provides a kind of apparatus and method of utilizing cold energy of liquefied natural gas to reclaim lighter hydrocarbons, in order to utilize LNG cold energy to reclaim LPG (Liquefied Petroleum Gas, liquefied petroleum gas are called for short LPG, and key component is propane and butane, i.e. lighter hydrocarbons).
For achieving the above object, the invention provides a kind of device that utilizes cold energy of liquefied natural gas to reclaim lighter hydrocarbons, comprise LNG storage tank, LPG storage tank, First Heat Exchanger, the second heat exchanger, domethanizing column, dethanizer, lean gas compressor, knockout drum, surge tank, first flow distributor, the first force (forcing) pump, the second force (forcing) pump, the 3rd force (forcing) pump, the 4th force (forcing) pump, slender acanthopanax press pump, LNG delivery trunk line, LNG exports the first pipeline, LNG exports the second pipeline, heat exchange output the 3rd pipeline, methane gas phase output the 4th pipeline, methane gas-liquid mixed output the 5th pipeline, gas phase methane output the 6th pipeline, liquid phase methane output the 7th pipeline, compressed methane output the 8th pipeline, gas phase heat exchange output the 9th pipeline, outer defeated the tenth pipeline, heat exchange output the 17 pipeline, C2+ exports the 11 pipeline, C2 exports the 12 pipeline, C2 heat exchange output the 13 pipeline, C2 the 14 pipeline that refluxes, LPG stores into tank the 16 pipeline, wherein
Described the first force (forcing) pump is located in described LNG storage tank, described LNG delivery trunk line one end is connected with described the first force (forcing) pump, the other end is connected with described first flow distributor, described first flow distributor and described LNG export the first pipeline and described LNG and export the second pipeline and be connected, described the first force (forcing) pump pumps the LNG pressurization in described LNG storage tank to described LNG delivery trunk line, and LNG is divided into two plumes by described first flow distributor and flows into respectively that described LNG exports the first pipeline and described LNG exports the second pipeline;
Described LNG exports the first pipeline and is connected with the first pipeline of described First Heat Exchanger, the first pipeline of described First Heat Exchanger is connected with described heat exchange output the 3rd pipeline, described heat exchange output the 3rd pipeline is connected with the top of described domethanizing column, and the LNG plume that described LNG exports in the first pipeline is flowed into the top of described domethanizing column after described First Heat Exchanger heat exchange by described heat exchange output the 3rd pipeline;
Described LNG exports the second pipeline and is connected with the first pipeline of described the second heat exchanger, the first pipeline of described the second heat exchanger is connected with described heat exchange output the 17 pipeline, described heat exchange output the 17 pipeline is connected with the middle part of described domethanizing column, and the LNG plume that described LNG exports in the second pipeline is flowed into the middle part of described domethanizing column after described the second heat exchanger heat exchange by described heat exchange output the 17 pipeline;
Described domethanizing column carries out rectifying separation to flowing into the LNG plume of its upper area and central region, and after multi-stage gas-liquid mass transfer, the tower top of described domethanizing column obtains C2+ (the above gas of C2) at the bottom of producing lean gas, tower;
The top of described domethanizing column connects described methane gas phase output the 4th pipeline, described methane gas phase output the 4th pipeline is connected with the second pipe of described First Heat Exchanger, the second pipe of described First Heat Exchanger is connected with one end of described methane gas-liquid mixed output the 5th pipeline, the other end of described methane gas-liquid mixed output the 5th pipeline is connected in described knockout drum, the liquid-phase outlet of described knockout drum is connected with one end of described liquid phase methane output the 7th pipeline, the gaseous phase outlet of described knockout drum is connected with one end of described gas phase methane output the 6th pipeline, described liquid phase methane output the 7th pipeline is connected with the top of described domethanizing column, and described the second force (forcing) pump is located on described liquid phase methane output the 7th pipeline, the other end of described gas phase methane output the 6th pipeline is connected with described lean gas compressor, described lean gas compressor is connected with one end of described compressed methane output the 8th pipeline, the described compressed methane output other end of the 8th pipeline and the 3rd pipeline of described First Heat Exchanger are connected, and the 3rd pipeline of described First Heat Exchanger is connected with described gas phase heat exchange output the 9th pipeline, described gas phase heat exchange output the 9th pipeline is connected with described outer defeated the tenth pipeline, and described the 3rd force (forcing) pump is located on described outer defeated the tenth pipeline,
Described lean gas enters described First Heat Exchanger along described methane gas phase output the 4th pipeline and carries out heat exchange rear section condensation formation gas-liquid two-phase, and the described lean gas of gas-liquid two-phase enters described knockout drum through described methane gas-liquid mixed output the 5th pipeline and carries out gas phase and liquid phase separation; The top formation that the described lean gas of liquid phase enters described domethanizing column through described liquid phase methane output the 7th pipeline refluxes and provides described domethanizing column to carry out the separated required liquid phase plume of rectifying; The described lean gas of gas phase enters described lean gas compressor through described gas phase methane output the 6th pipeline, described lean gas compressor is by the described lean gas pressurization of gas phase, described lean gas after pressurization enters described First Heat Exchanger the 3rd pipeline heat exchange through described compressed methane output the 8th pipeline exports described outer defeated the tenth pipeline to liquid phase and by described gas phase heat exchange output the 9th pipeline, and described the 3rd force (forcing) pump is defeated by user beyond its pressurization is pumped;
At the bottom of the tower of described domethanizing column, be connected by described C2+ output the 11 pipeline with described dethanizer, for being sent into described dethanizer, the C2+ obtaining at the bottom of the tower of described domethanizing column carries out rectifying separation, after multi-stage gas-liquid mass transfer, the gas main component that the tower top of described dethanizer produces is to obtain LPG at the bottom of ethane, tower;
The tower top of described dethanizer is connected with one end of the second pipe of described the second heat exchanger by described C2 output the 12 pipeline, the other end of the second pipe of described the second heat exchanger is connected with described surge tank by C2 heat exchange output the 13 pipeline, described surge tank is connected with the tower top of described dethanizer by described C2 backflow the 14 pipeline, described the 4th force (forcing) pump is located at described C2 and refluxes on the 14 pipeline, the gas that the tower top of described dethanizer produces is condensed into liquid phase and enters described surge tank after described the second heat exchanger heat exchange, it forms and to reflux and to provide described dethanizer to carry out the required liquid phase plume of rectifying separation through pressurized the pumping to the top that the tower top of described dethanizer enters described dethanizer of described the 4th force (forcing) pump,
At the bottom of the tower of described dethanizer, by described LPG, store into tank the 16 pipeline and be connected with described LPG storage tank, described slender acanthopanax press pump is located at described LPG and stores on tank the 16 pipeline, and described LPG storage tank is pumped and is stored in the lighter hydrocarbons pressurization that described slender acanthopanax press pump produces at the bottom of by the tower of described dethanizer.
Wherein, also be provided with gas phase output the 9th looped pipeline line and gas phase control valve, one end of described gas phase output the 9th looped pipeline line is connected with described compressed methane output the 8th pipeline, its other end is connected with described gas phase heat exchange output the 9th pipeline, makes the described lean gas part after pressurization flow directly into described outer defeated the tenth pipeline by described gas phase output the 9th looped pipeline line; Described gas phase control valve is located on described gas phase output the 9th looped pipeline line, described gas phase control valve is controlled the flow of the described lean gas that flows through described gas phase output the 9th looped pipeline line, the aperture of described gas phase control valve make the first pipeline of described First Heat Exchanger and the temperature difference of the 3rd pipeline maintain+25 ℃～+ 30 ℃ between.
Wherein, at the bottom of the tower of described domethanizing column and at the bottom of the tower of described dethanizer, be respectively equipped with the first reboiler and the second reboiler, for the liquid of tower reactor in described domethanizing column and described dethanizer is vaporized again.
Wherein, also being provided with ethane storage tank, the second flow distribution device, C2+ stores into tank the 15 pipeline and the 6th force (forcing) pump, described the second flow distribution device is connected to described surge tank and described C2+ backflow the 14 pipeline junction, the flow that enters described de-ethylene column tower top for controlling the liquid phase plume of described surge tank, described the 6th force (forcing) pump is located at described C2+ and stores on tank the 15 pipeline.
Wherein, described First Heat Exchanger and described the second heat exchanger are plate and stick up formula heat exchanger.
The present invention also provides a kind of method of utilizing the device recovery lighter hydrocarbons of above-mentioned cold energy of liquefied natural gas recovery lighter hydrocarbons, comprises the following steps:
By described the first force (forcing) pump, the LNG pressurization in described LNG storage tank is pumped to described LNG delivery trunk line, LNG is divided into two plumes by described first flow distributor and flows into respectively that described LNG exports the first pipeline and described LNG exports the second pipeline;
The LNG plume that described LNG exports in the first pipeline is flowed into the top of described domethanizing column after described First Heat Exchanger heat exchange by described heat exchange output the 3rd pipeline;
The LNG plume that described LNG exports in the second pipeline is flowed into the middle part of described domethanizing column after described the second heat exchanger heat exchange by described heat exchange output the 17 pipeline;
Described domethanizing column carries out rectifying separation to flowing into the LNG plume of its upper area and central region, and after multi-stage gas-liquid mass transfer, the tower top of described domethanizing column obtains C2+ at the bottom of producing lean gas, tower;
Described lean gas enters described First Heat Exchanger along described methane gas phase output the 4th pipeline and carries out heat exchange rear section condensation formation gas-liquid two-phase, and the described lean gas of gas-liquid two-phase enters knockout drum through described methane gas-liquid mixed output the 5th pipeline and carries out gas phase and liquid phase separation; The top formation that the described lean gas of liquid phase enters described domethanizing column through described liquid phase methane output the 7th pipeline refluxes and provides described domethanizing column to carry out the separated required liquid phase plume of rectifying; The described lean gas of gas phase enters described lean gas compressor through described gas phase methane output the 6th pipeline, described lean gas compressor is by the described lean gas pressurization of gas phase, described lean gas after pressurization enters described First Heat Exchanger the 3rd pipeline heat exchange through described compressed methane output the 8th pipeline exports described outer defeated the tenth pipeline to liquid phase and by described gas phase heat exchange output the 9th pipeline, and described the 3rd force (forcing) pump is defeated by user beyond its pressurization is pumped;
The C2+ obtaining at the bottom of the tower of described domethanizing column is sent into described dethanizer and carry out rectifying separation, after multi-stage gas-liquid mass transfer, the gas main component that the tower top of described dethanizer produces is to obtain LPG at the bottom of ethane, tower;
The gas that the tower top of described dethanizer produces is condensed into liquid phase and enters described surge tank after described the second heat exchanger heat exchange, and it forms and reflux and provide described dethanizer to carry out the required liquid phase plume of rectifying separation through pressurized the pumping to the top that the tower top of described dethanizer enters described dethanizer of described the 4th force (forcing) pump;
LPG storage tank is pumped and is stored in the LPG pressurization that described slender acanthopanax press pump produces at the bottom of by the tower of described dethanizer.
Wherein, described LNG exports the first pipeline and described LNG and exports plume mole in the second pipeline than being 7.5:1～9.0:1.
Wherein, the pump discharge pressure of described the first force (forcing) pump is 1.75MPaG～2.25MPaG.
Wherein, the outlet pressure of described lean gas compressor is 2.9MPaG～3.3MPaG.
Wherein, the operating pressure of described dethanizer is 0.45MPaG～0.6MPaG.
Compared with prior art, beneficial effect of the present invention is embodied in:
The apparatus and method of utilizing cold energy of liquefied natural gas to reclaim lighter hydrocarbons provided by the invention, liquefied natural gas being pressurizeed from storage tank pump is conveyed into respectively two cold energy and reclaims in heat exchangers afterwards, respectively with lighter hydrocarbons recovery after lean gas and the gas phase of two column overhead carry out heat exchange; By making liquefied natural gas endothermic gasification, the process of lean gas heat release condensation completes the cold recovery utilization of liquefied natural gas; Condensed lean gas is pressurized to ductwork pressure with pump and is transported in pipe network pipeline after gasifier gasification, and the light hydrocarbon pump that recovery obtains is delivered in corresponding storage tank and stored; The cold that the present invention utilizes LNG self with lower cost by the lighter hydrocarbons resource separation in rich gas out, realize the complex optimum utilization of natural gas resource, increase LNG receiving station operating flexibility, adapt to many-sided demand of user's request diversity and raising factory economy type.
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 utilizing cold energy of liquefied natural gas to reclaim the device of lighter hydrocarbons and utilizing LNG to reclaim the flow chart of LPG of one embodiment of the invention.
Description of reference numerals: T1-LNG storage tank; T2-ethane storage tank; T3-LPG storage tank; E1-First Heat Exchanger; E2-the second heat exchanger; C1-domethanizing column; C2-dethanizer; K1-lean gas compressor; Q1-knockout drum; Q2-surge tank; V1-gas phase control valve; L1-first flow distributor; L2-the second flow distribution device; D1-the first force (forcing) pump; D2-the second force (forcing) pump; D3-the 3rd force (forcing) pump; D4-the 4th force (forcing) pump; D5-slender acanthopanax press pump; D6-the 6th force (forcing) pump; M1-the first reboiler; M2-the second reboiler; 100-LNG delivery trunk line; 101-LNG exports the first pipeline; 102-LNG exports the second pipeline; 103-heat exchange output the 3rd pipeline; 104-methane gas phase output the 4th pipeline; 105-methane gas-liquid mixed output the 5th pipeline; 106-gas phase methane output the 6th pipeline; 107-liquid phase methane output the 7th pipeline; 108-compressed methane output the 8th pipeline; 109-gas phase heat exchange output the 9th pipeline; Outer defeated the tenth pipeline of 110-; 117-heat exchange output the 17 pipeline; 111-C2+ exports the 11 pipeline; 112-C2 exports the 12 pipeline; 113-C2 heat exchange output the 13 pipeline; 114-C2 the 14 pipeline that refluxes; 115-C2+ stores into tank the 15 pipeline; 116-LPG stores into tank the 16 pipeline.
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.
Refer to Fig. 1, what Fig. 1 was one embodiment of the invention utilizes cold energy of liquefied natural gas to reclaim the device of lighter hydrocarbons and utilizes LNG to reclaim the flow chart of LPG.
As shown in Figure 1, the invention provides a kind of device that utilizes cold energy of liquefied natural gas to reclaim lighter hydrocarbons, comprise LNG storage tank T1, LPG storage tank T3, First Heat Exchanger E1, the second heat exchanger E2, domethanizing column C1, dethanizer C2, lean gas compressor K1, knockout drum Q1, surge tank Q2, first flow distributor L1, the first force (forcing) pump D1, the second force (forcing) pump D2, the 3rd force (forcing) pump D3, the 4th force (forcing) pump D4, slender acanthopanax press pump D5, the 6th force (forcing) pump D6, the first reboiler M1, the second reboiler M2, LNG delivery trunk line 100, LNG exports the first pipeline 101, LNG exports the second pipeline 102, heat exchange output the 3rd pipeline 103, methane gas phase output the 4th pipeline 104, methane gas-liquid mixed output the 5th pipeline 105, gas phase methane output the 6th pipeline 106, liquid phase methane output the 7th pipeline 107, compressed methane output the 8th pipeline 108, gas phase heat exchange output the 9th pipeline 109, outer defeated the tenth pipeline 110, heat exchange output the 17 pipeline 117, C2+ exports the 11 pipeline 111, C2 exports the 12 pipeline 112, C2 heat exchange output the 13 pipeline 113, C2 the 14 pipeline 114 that refluxes, LPG stores into tank the 16 pipeline 116, wherein
The first force (forcing) pump D1 is located in LNG storage tank T1, one end of LNG delivery trunk line 100 is connected with the first force (forcing) pump D1, the other end is connected with first flow distributor L1, and first flow distributor L1 and LNG export the first pipeline 101 and LNG and export the second pipeline 102 and be connected;
LNG exports the first pipeline 101 and is connected with the first pipeline of First Heat Exchanger E1, and the first pipeline of First Heat Exchanger E1 is connected with heat exchange output the 3rd pipeline 103, and heat exchange output the 3rd pipeline 103 is connected with the top of domethanizing column C1;
LNG exports the second pipeline 102 and is connected with the first pipeline of the second heat exchanger E2, and the first pipeline of the second heat exchanger E2 is connected with heat exchange output the 17 pipeline 117, and heat exchange output the 17 pipeline 117 is connected with the middle part of domethanizing column C1;
The top of domethanizing column C1 connects methane gas phase output the 4th pipeline 104, the second pipe of methane gas phase output the 4th pipeline 104 First Heat Exchanger E1 connects, the second pipe of First Heat Exchanger E1 is connected with one end of methane gas-liquid mixed output the 5th pipeline 105, the other end of methane gas-liquid mixed output the 5th pipeline 105 is connected in knockout drum Q1, the liquid-phase outlet of knockout drum Q1 is connected with one end of liquid phase methane output the 7th pipeline 107, and the gaseous phase outlet of knockout drum Q1 is connected with one end of gas phase methane output the 6th pipeline 106, liquid phase methane output the 7th pipeline 107 is connected with the top of domethanizing column C1, and the second force (forcing) pump D2 is located on liquid phase methane output the 7th pipeline 107, the other end of gas phase methane output the 6th pipeline 106 is connected with lean gas compressor K1, lean gas compressor K1 is connected with one end of compressed methane output the 8th pipeline 108, the compressed methane output other end of the 8th pipeline 108 and the 3rd pipeline of First Heat Exchanger E1 are connected, the 3rd pipeline of First Heat Exchanger E1 is connected with gas phase heat exchange output the 9th pipeline 109, in one embodiment of the invention, also be provided with gas phase output the 9th looped pipeline line and gas phase control valve V1, one end of described gas phase output the 9th looped pipeline line is connected with compressed methane output the 8th pipeline 108, its other end is connected with gas phase heat exchange output the 9th pipeline 109, make the lean gas part after pressurization flow directly into outer defeated the tenth pipeline 110 by described gas phase output the 9th looped pipeline line, gas phase heat exchange output the 9th pipeline 109 is connected with outer defeated the tenth pipeline 110, and the 3rd force (forcing) pump D3 is located on outer defeated the tenth pipeline,
At the bottom of the tower of domethanizing column C1, exporting the 11 pipeline 110 with dethanizer C2 by C2+ is connected;
The tower top of dethanizer C2 is exported the 12 pipeline 112 by C2 and is connected with one end of the second pipe of the second heat exchanger E2, the other end of the second pipe of the second heat exchanger E2 is connected with surge tank Q2 by C2 heat exchange output the 13 pipeline 113, surge tank Q2 is connected with the tower top of dethanizer C2 by C2 the 14 pipeline 114 that refluxes, and the 4th force (forcing) pump D4 is located at C2 and refluxes on the 14 pipeline 114.In one embodiment of the invention, also be provided with ethane storage tank T2, the second flow distribution device L2, C2+ store into tank the 15 pipeline 115 and the 6th force (forcing) pump D6, the second flow distribution device L2 is connected to surge tank Q2 and C2+ backflow the 14 pipeline 114 junctions, and the 6th force (forcing) pump D6 is located at C2+ and stores on tank the 15 pipeline 115.
At the bottom of the tower of dethanizer C2, by LPG, stored into tank the 16 pipeline 116 and be connected with LPG storage tank T3, slender acanthopanax press pump D5 is located at LPG and stores on tank the 16 pipeline 116.
During concrete enforcement, the first force (forcing) pump D1 pumps the LNG pressurization in LNG storage tank T1 to LNG delivery trunk line 100, and wherein, the pump discharge pressure of the first force (forcing) pump D1 is 1.75MPaG～2.25MPaG (MPaG, meter reading pressure).LNG is divided into two plumes by first flow distributor L1 and flows into respectively that LNG exports the first pipeline 101 and LNG exports the second pipeline 102.Wherein, LNG exports the first pipeline and LNG and exports plume mole in the second pipeline than being 7.5:1～9.0:1.The LNG plume that LNG exports in the first pipeline 101 is flowed into the top of domethanizing column C1 after First Heat Exchanger E1 heat exchange by heat exchange output the 3rd pipeline 103; Wherein, the plume of heat exchange output the 3rd pipeline 103 is with the temperature of-85 ℃ of left and right, and approximately 0.75～0.85 rate of gasification enters the top of domethanizing column C1.The LNG plume that LNG exports in the second pipeline 102 is flowed into the middle part of domethanizing column C1 after the second heat exchanger E2 heat exchange by heat exchange output the 17 pipeline 117.Domethanizing column C1 carries out rectifying separation to flowing into the LNG plume of its upper area and central region, and after multi-stage gas-liquid mass transfer, the tower top of domethanizing column C1 obtains C2+ at the bottom of producing lean gas, tower.Lean gas enters First Heat Exchanger E1 along methane gas phase output the 4th pipeline 104 and carries out heat exchange rear section condensation formation gas-liquid two-phase, and the lean gas of gas-liquid two-phase enters knockout drum Q1 through methane gas-liquid mixed output the 5th pipeline 105 and carries out gas phase and liquid phase separation; The top formation that the lean gas of liquid phase enters domethanizing column C1 through liquid phase methane output the 7th pipeline 107 refluxes and provides domethanizing column C1 to carry out the separated required liquid phase plume of rectifying; The lean gas of gas phase enters lean gas compressor K1 through gas phase methane output the 6th pipeline 106, and lean gas compressor K1 is by the lean gas pressurization of gas phase, and wherein, the outlet pressure of lean gas compressor K1 is 2.9MPaG～3.3MPaG.The 3rd pipeline heat exchange that the compressed methane output of lean gas the 8th pipeline 108 after pressurization enters First Heat Exchanger E1 exports outer defeated the tenth pipeline 110 to liquid phase and by gas phase heat exchange output the 9th pipeline 109, gas phase control valve V1 is located on described gas phase output the 9th looped pipeline line, gas phase control valve V1 controls the flow of the lean gas flow through described gas phase output the 9th looped pipeline line, the aperture of gas phase control valve V1 make the first pipeline of First Heat Exchanger E1 and the temperature difference of the 3rd pipeline maintain+25 ℃～+ 30 ℃ between; The 3rd force (forcing) pump D3 is defeated by user beyond the LNG pressurization that flows to outer defeated the tenth pipeline 110 is pumped.The C2+ that the 11 pipeline 110 obtains at the bottom of by the tower of domethanizing column C1 sends into dethanizer C2 and carries out rectifying separation, wherein, the operating pressure of dethanizer C2 is 0.45MPaG～0.6MPaG, after multi-stage gas-liquid mass transfer, the gas main component that the tower top of dethanizer C2 produces is to obtain LPG at the bottom of ethane, tower.The gas that the tower top of dethanizer C2 produces is condensed into liquid phase and enters surge tank Q2 after the second heat exchanger E2 heat exchange, and it forms and reflux and provide dethanizer C2 to carry out the required liquid phase plume of rectifying separation through pressurized the pumping to the top that the tower top of dethanizer C2 enters dethanizer C2 of the 4th force (forcing) pump D4; The liquid phase plume that the second flow distribution device L2 controls surge tank Q2 enters the flow that takes off ethylene column C2 tower top, the liquid phase plume of surge tank Q2 is separated to dethanizer C2 and carry out the redundance importing ethane storage tank T2 storage after the separated required liquid phase plume of rectifying.The lighter hydrocarbons that produce at the bottom of the tower of dethanizer C2 are pumped and are stored in LPG storage tank T3 by slender acanthopanax press pump D5 pressurization, realize lighter hydrocarbons recovery and store.The molar concentration of the LPG product obtaining in one embodiment of the invention, is not less than 98%.
In one embodiment of the invention, at the bottom of the tower of domethanizing column C1, be provided with the first reboiler M1,, at the bottom of the tower of dethanizer C2, be provided with the second reboiler M2, be respectively used to make the liquid of tower reactor in domethanizing column C1 and dethanizer C2 again to vaporize.
Wherein, in order to make maximum heat transfer, in one embodiment of the invention, First Heat Exchanger E1 and the second heat exchanger E2 are plate and stick up formula heat exchanger.
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 (10)
1. a device that utilizes cold energy of liquefied natural gas to reclaim lighter hydrocarbons, it is characterized in that, comprise LNG storage tank, LPG storage tank, First Heat Exchanger, the second heat exchanger, domethanizing column, dethanizer, lean gas compressor, knockout drum, surge tank, first flow distributor, the first force (forcing) pump, the second force (forcing) pump, the 3rd force (forcing) pump, the 4th force (forcing) pump, slender acanthopanax press pump, LNG delivery trunk line, LNG exports the first pipeline, LNG exports the second pipeline, heat exchange output the 3rd pipeline, methane gas phase output the 4th pipeline, methane gas-liquid mixed output the 5th pipeline, gas phase methane output the 6th pipeline, liquid phase methane output the 7th pipeline, compressed methane output the 8th pipeline, gas phase heat exchange output the 9th pipeline, outer defeated the tenth pipeline, heat exchange output the 17 pipeline, C2+ exports the 11 pipeline, C2 exports the 12 pipeline, C2 heat exchange output the 13 pipeline, C2 the 14 pipeline that refluxes, LPG stores into tank the 16 pipeline, wherein
Described the first force (forcing) pump is located in described LNG storage tank, described LNG delivery trunk line one end is connected with described the first force (forcing) pump, the other end is connected with described first flow distributor, described first flow distributor and described LNG export the first pipeline and described LNG and export the second pipeline and be connected, described the first force (forcing) pump pumps the LNG pressurization in described LNG storage tank to described LNG delivery trunk line, and LNG is divided into two plumes by described first flow distributor and flows into respectively that described LNG exports the first pipeline and described LNG exports the second pipeline;
Described LNG exports the first pipeline and is connected with the first pipeline of described First Heat Exchanger, the first pipeline of described First Heat Exchanger is connected with described heat exchange output the 3rd pipeline, described heat exchange output the 3rd pipeline is connected with the top of described domethanizing column, and the LNG plume that described LNG exports in the first pipeline is flowed into the top of described domethanizing column after described First Heat Exchanger heat exchange by described heat exchange output the 3rd pipeline;
Described LNG exports the second pipeline and is connected with the first pipeline of described the second heat exchanger, the first pipeline of described the second heat exchanger is connected with described heat exchange output the 17 pipeline, described heat exchange output the 17 pipeline is connected with the middle part of described domethanizing column, and the LNG plume that described LNG exports in the second pipeline is flowed into the middle part of described domethanizing column after described the second heat exchanger heat exchange by described heat exchange output the 17 pipeline;
Described domethanizing column carries out rectifying separation to flowing into the LNG plume of its upper area and central region, and after multi-stage gas-liquid mass transfer, the tower top of described domethanizing column obtains C2+ at the bottom of producing lean gas, tower;
The top of described domethanizing column connects described methane gas phase output the 4th pipeline, described methane gas phase output the 4th pipeline is connected with the second pipe of described First Heat Exchanger, the second pipe of described First Heat Exchanger is connected with one end of described methane gas-liquid mixed output the 5th pipeline, the other end of described methane gas-liquid mixed output the 5th pipeline is connected in described knockout drum, the liquid-phase outlet of described knockout drum is connected with one end of described liquid phase methane output the 7th pipeline, the gaseous phase outlet of described knockout drum is connected with one end of described gas phase methane output the 6th pipeline, described liquid phase methane output the 7th pipeline is connected with the top of described domethanizing column, and described the second force (forcing) pump is located on described liquid phase methane output the 7th pipeline, the other end of described gas phase methane output the 6th pipeline is connected with described lean gas compressor, described lean gas compressor is connected with one end of described compressed methane output the 8th pipeline, the described compressed methane output other end of the 8th pipeline and the 3rd pipeline of described First Heat Exchanger are connected, and the 3rd pipeline of described First Heat Exchanger is connected with described gas phase heat exchange output the 9th pipeline, described gas phase heat exchange output the 9th pipeline is connected with described outer defeated the tenth pipeline, and described the 3rd force (forcing) pump is located on described outer defeated the tenth pipeline,
Described lean gas enters described First Heat Exchanger along described methane gas phase output the 4th pipeline and carries out heat exchange rear section condensation formation gas-liquid two-phase, and the described lean gas of gas-liquid two-phase enters described knockout drum through described methane gas-liquid mixed output the 5th pipeline and carries out gas phase and liquid phase separation; The top formation that the described lean gas of liquid phase enters described domethanizing column through described liquid phase methane output the 7th pipeline refluxes and provides described domethanizing column to carry out the separated required liquid phase plume of rectifying; The described lean gas of gas phase enters described lean gas compressor through described gas phase methane output the 6th pipeline, described lean gas compressor is by the described lean gas pressurization of gas phase, described lean gas after pressurization enters described First Heat Exchanger the 3rd pipeline heat exchange through described compressed methane output the 8th pipeline exports described outer defeated the tenth pipeline to liquid phase and by described gas phase heat exchange output the 9th pipeline, and described the 3rd force (forcing) pump is defeated by user beyond its pressurization is pumped;
At the bottom of the tower of described domethanizing column, be connected by described C2+ output the 11 pipeline with described dethanizer, for being sent into described dethanizer, the C2+ obtaining at the bottom of the tower of described domethanizing column carries out rectifying separation, after multi-stage gas-liquid mass transfer, the gas main component that the tower top of described dethanizer produces is to obtain LPG at the bottom of ethane, tower;
The tower top of described dethanizer is connected with one end of the second pipe of described the second heat exchanger by described C2 output the 12 pipeline, the other end of the second pipe of described the second heat exchanger is connected with described surge tank by C2 heat exchange output the 13 pipeline, described surge tank is connected with the tower top of described dethanizer by described C2 backflow the 14 pipeline, described the 4th force (forcing) pump is located at described C2 and refluxes on the 14 pipeline, the gas that the tower top of described dethanizer produces is condensed into liquid phase and enters described surge tank after described the second heat exchanger heat exchange, it forms and to reflux and to provide described dethanizer to carry out the required liquid phase plume of rectifying separation through pressurized the pumping to the top that the tower top of described dethanizer enters described dethanizer of described the 4th force (forcing) pump,
At the bottom of the tower of described dethanizer, by described LPG, store into tank the 16 pipeline and be connected with described LPG storage tank, described slender acanthopanax press pump is located at described LPG and stores on tank the 16 pipeline, and described LPG storage tank is pumped and is stored in the lighter hydrocarbons pressurization that described slender acanthopanax press pump produces at the bottom of by the tower of described dethanizer.
2. the device that utilizes cold energy of liquefied natural gas to reclaim lighter hydrocarbons according to claim 1, it is characterized in that, also be provided with gas phase output the 9th looped pipeline line and gas phase control valve, one end of described gas phase output the 9th looped pipeline line is connected with described compressed methane output the 8th pipeline, its other end is connected with described gas phase heat exchange output the 9th pipeline, makes the described lean gas part after pressurization flow directly into described outer defeated the tenth pipeline by described gas phase output the 9th looped pipeline line; Described gas phase control valve is located on described gas phase output the 9th looped pipeline line, described gas phase control valve is controlled the flow of the described lean gas that flows through described gas phase output the 9th looped pipeline line, the aperture of described gas phase control valve make the first pipeline of described First Heat Exchanger and the temperature difference of the 3rd pipeline maintain+25 ℃～+ 30 ℃ between.
3. the device that utilizes cold energy of liquefied natural gas to reclaim lighter hydrocarbons according to claim 1, it is characterized in that, at the bottom of the tower of described domethanizing column and at the bottom of the tower of described dethanizer, be respectively equipped with the first reboiler and the second reboiler, for the liquid of tower reactor in described domethanizing column and described dethanizer is vaporized again.
4. the device that utilizes cold energy of liquefied natural gas to reclaim lighter hydrocarbons according to claim 1, it is characterized in that, also being provided with ethane storage tank, the second flow distribution device, C2+ stores into tank the 15 pipeline and the 6th force (forcing) pump, described the second flow distribution device is connected to described surge tank and described C2+ backflow the 14 pipeline junction, the flow that enters described de-ethylene column tower top for controlling the liquid phase plume of described surge tank, described the 6th force (forcing) pump is located at described C2+ and stores on tank the 15 pipeline.
5. the device that utilizes cold energy of liquefied natural gas to reclaim lighter hydrocarbons according to claim 1, is characterized in that, described First Heat Exchanger and described the second heat exchanger are plate and stick up formula heat exchanger.
6. the device that utilizes the cold energy of liquefied natural gas of claim 1～5 any one to reclaim lighter hydrocarbons reclaims a method for lighter hydrocarbons, it is characterized in that, comprises the following steps:
By described the first force (forcing) pump, the LNG pressurization in described LNG storage tank is pumped to described LNG delivery trunk line, LNG is divided into two plumes by described first flow distributor and flows into respectively that described LNG exports the first pipeline and described LNG exports the second pipeline;
The LNG plume that described LNG exports in the first pipeline is flowed into the top of described domethanizing column after described First Heat Exchanger heat exchange by described heat exchange output the 3rd pipeline;
The LNG plume that described LNG exports in the second pipeline is flowed into the middle part of described domethanizing column after described the second heat exchanger heat exchange by described heat exchange output the 17 pipeline;
Described domethanizing column carries out rectifying separation to flowing into the LNG plume of its upper area and central region, and after multi-stage gas-liquid mass transfer, the tower top of described domethanizing column obtains C2+ at the bottom of producing lean gas, tower;
Described lean gas enters described First Heat Exchanger along described methane gas phase output the 4th pipeline and carries out heat exchange rear section condensation formation gas-liquid two-phase, and the described lean gas of gas-liquid two-phase enters knockout drum through described methane gas-liquid mixed output the 5th pipeline and carries out gas phase and liquid phase separation; The top formation that the described lean gas of liquid phase enters described domethanizing column through described liquid phase methane output the 7th pipeline refluxes and provides described domethanizing column to carry out the separated required liquid phase plume of rectifying; The described lean gas of gas phase enters described lean gas compressor through described gas phase methane output the 6th pipeline, described lean gas compressor is by the described lean gas pressurization of gas phase, described lean gas after pressurization enters described First Heat Exchanger the 3rd pipeline heat exchange through described compressed methane output the 8th pipeline exports described outer defeated the tenth pipeline to liquid phase and by described gas phase heat exchange output the 9th pipeline, and described the 3rd force (forcing) pump is defeated by user beyond its pressurization is pumped;
The C2+ obtaining at the bottom of the tower of described domethanizing column is sent into described dethanizer and carry out rectifying separation, after multi-stage gas-liquid mass transfer, the gas main component that the tower top of described dethanizer produces is to obtain LPG at the bottom of ethane, tower;
The gas that the tower top of described dethanizer produces is condensed into liquid phase and enters described surge tank after described the second heat exchanger heat exchange, and it forms and reflux and provide described dethanizer to carry out the required liquid phase plume of rectifying separation through pressurized the pumping to the top that the tower top of described dethanizer enters described dethanizer of described the 4th force (forcing) pump;
LPG storage tank is pumped and is stored in the LPG pressurization that described slender acanthopanax press pump produces at the bottom of by the tower of described dethanizer.
7. the method for recovery lighter hydrocarbons according to claim 6, is characterized in that, it is 7.5:1～9.0:1 with the plume mole ratio that described LNG exports in the second pipeline that described LNG exports the first pipeline.
8. the method for recovery lighter hydrocarbons according to claim 6, is characterized in that, the pump discharge pressure of described the first force (forcing) pump is 1.75MPaG～2.25MPaG.
9. the method for recovery lighter hydrocarbons according to claim 6, is characterized in that, the outlet pressure of described lean gas compressor is 2.9MPaG～3.3MPaG.
10. the method for recovery lighter hydrocarbons according to claim 6, is characterized in that, the operating pressure of described dethanizer is 0.45MPaG～0.6MPaG.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105733721A (en) * | 2016-04-14 | 2016-07-06 | 北京安珂罗工程技术有限公司 | Method and system for removing heavy hydrocarbon from natural gas |
| CN105783421A (en) * | 2016-04-07 | 2016-07-20 | 成都赛普瑞兴科技有限公司 | Natural gas light hydrocarbon recovery method and device |
| CN105779052A (en) * | 2016-04-14 | 2016-07-20 | 北京安珂罗工程技术有限公司 | Method and system for recovering heavy hydrocarbon in liquefied natural gas production |
| CN106247759A (en) * | 2016-08-15 | 2016-12-21 | 中国海洋石油总公司 | A kind of LNG receiving station reclaims the method for lighter hydrocarbons |
| CN108507277A (en) * | 2018-04-28 | 2018-09-07 | 中国石油工程建设有限公司 | A kind of the cold comprehensive utilization device and method of natural gas ethane recovery |
| CN110144238A (en) * | 2019-05-24 | 2019-08-20 | 西南石油大学 | A kind of liquefied natural gas methods of light hydrocarbon recovery |
| CN110590490A (en) * | 2018-06-13 | 2019-12-20 | 中国石化工程建设有限公司 | System and method for recovering hydrocarbons in liquefied natural gas |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1737087A (en) * | 2005-06-10 | 2006-02-22 | 华南理工大学 | Method for separating light hydrocarbon from liquified natural gas |
| CN1821352A (en) * | 2006-01-20 | 2006-08-23 | 华南理工大学 | Light hydrocarbon separating method for liquefied natural gas with peak regulating function |
| CN101160498A (en) * | 2004-08-27 | 2008-04-09 | 阿梅克帕拉贡公司 | Process for extracting ethane and heavier hydrocarbons from lng |
| CN101815915A (en) * | 2007-08-14 | 2010-08-25 | 氟石科技公司 | Configurations and methods for improved natural gas liquids recovery |
| CA2805450A1 (en) * | 2012-02-22 | 2013-08-22 | Black & Veatch Corporation | Ngl recovery from natural gas using a mixed refrigerant |
| CN103398546A (en) * | 2013-07-26 | 2013-11-20 | 华南理工大学 | Method of cryogenic separation for light hydrocarbons on the basis of LNG (liquefied natural gas) cold energy |
| CN103453730A (en) * | 2013-08-29 | 2013-12-18 | 杭州福斯达实业集团有限公司 | Natural gas liquefying method and device with light hydrocarbon recovery function |
-
2014
- 2014-05-07 CN CN201410191260.1A patent/CN103994635B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101160498A (en) * | 2004-08-27 | 2008-04-09 | 阿梅克帕拉贡公司 | Process for extracting ethane and heavier hydrocarbons from lng |
| CN1737087A (en) * | 2005-06-10 | 2006-02-22 | 华南理工大学 | Method for separating light hydrocarbon from liquified natural gas |
| CN1821352A (en) * | 2006-01-20 | 2006-08-23 | 华南理工大学 | Light hydrocarbon separating method for liquefied natural gas with peak regulating function |
| CN101815915A (en) * | 2007-08-14 | 2010-08-25 | 氟石科技公司 | Configurations and methods for improved natural gas liquids recovery |
| CA2805450A1 (en) * | 2012-02-22 | 2013-08-22 | Black & Veatch Corporation | Ngl recovery from natural gas using a mixed refrigerant |
| CN103398546A (en) * | 2013-07-26 | 2013-11-20 | 华南理工大学 | Method of cryogenic separation for light hydrocarbons on the basis of LNG (liquefied natural gas) cold energy |
| CN103453730A (en) * | 2013-08-29 | 2013-12-18 | 杭州福斯达实业集团有限公司 | Natural gas liquefying method and device with light hydrocarbon recovery function |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105783421A (en) * | 2016-04-07 | 2016-07-20 | 成都赛普瑞兴科技有限公司 | Natural gas light hydrocarbon recovery method and device |
| CN105733721A (en) * | 2016-04-14 | 2016-07-06 | 北京安珂罗工程技术有限公司 | Method and system for removing heavy hydrocarbon from natural gas |
| CN105779052A (en) * | 2016-04-14 | 2016-07-20 | 北京安珂罗工程技术有限公司 | Method and system for recovering heavy hydrocarbon in liquefied natural gas production |
| CN105733721B (en) * | 2016-04-14 | 2018-09-25 | 北京安珂罗工程技术有限公司 | A kind of method and system removing heavy hydrocarbon from natural gas |
| CN105779052B (en) * | 2016-04-14 | 2019-01-04 | 北京安珂罗工程技术有限公司 | The method and system of heavy hydrocarbon is recycled in a kind of liquefied natural gas (LNG) production |
| CN106247759A (en) * | 2016-08-15 | 2016-12-21 | 中国海洋石油总公司 | A kind of LNG receiving station reclaims the method for lighter hydrocarbons |
| CN106247759B (en) * | 2016-08-15 | 2019-04-16 | 中国海洋石油集团有限公司 | A kind of method of LNG receiving station recycling lighter hydrocarbons |
| CN108507277A (en) * | 2018-04-28 | 2018-09-07 | 中国石油工程建设有限公司 | A kind of the cold comprehensive utilization device and method of natural gas ethane recovery |
| CN110590490A (en) * | 2018-06-13 | 2019-12-20 | 中国石化工程建设有限公司 | System and method for recovering hydrocarbons in liquefied natural gas |
| CN110144238A (en) * | 2019-05-24 | 2019-08-20 | 西南石油大学 | A kind of liquefied natural gas methods of light hydrocarbon recovery |
| CN110144238B (en) * | 2019-05-24 | 2021-03-16 | 西南石油大学 | Liquefied natural gas light hydrocarbon recovery method |
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