CN202432825U - Device adopting single refrigeration of mixed working mediums to liquefy natural gas - Google Patents
Device adopting single refrigeration of mixed working mediums to liquefy natural gas Download PDFInfo
- Publication number
- CN202432825U CN202432825U CN 201120459035 CN201120459035U CN202432825U CN 202432825 U CN202432825 U CN 202432825U CN 201120459035 CN201120459035 CN 201120459035 CN 201120459035 U CN201120459035 U CN 201120459035U CN 202432825 U CN202432825 U CN 202432825U
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- gas
- exchanger channels
- liquid separator
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model relates to a device adopting single refrigeration of mixed working mediums to liquefy natural gas. The device comprises a three-segment type or two-segment type mixed working medium compressor, three or four coolers, four or three gas-liquid separators, a heavy hydrocarbon separator, five or four throttling devices, a plate-fin heat exchanger group and a liquefied natural gas (LNG) storage tank. The three-segment type or two-segment type mixed refrigerant compressor is adopted, mixed refrigerants are compressed step by step and separated step by step, and liquid separated in each step directly enters heat exchangers to carry out heat exchange without requiring a pump to provide power. Besides, heat exchange curves of both cold fluid and hot fluid in the whole heat exchange process are matched with each other, the flow of the mixed refrigerants is effectively reduced, and accordingly energy consumption of the device is reduced.
Description
Technical field
The utility model relates to the liquefaction production of being rich in hydrocarbon gas, is specifically related to a kind of device of single mixed working fluid refrigeration liquefying natural gas.
Background technology
Natural gas is owing to its feature of environmental protection becomes the optimisation substance that replaces other fuel, and its application expands aspects such as generating, automobile usefulness gas, industrial gas, city dweller's usefulness gas, chemical industry usefulness gas gradually to.
Along with the growth of natural gas consumption amount, the most effectively supply with one of form as natural gas, the volume of trade of liquefied natural gas has also become one of fastest-rising field of energy market.The continuous development of liquefied natural gas industry is then had higher requirement at aspects such as energy consumption, investment and efficient to natural gas liquefaction and device.
At present, the natural gas liquefaction process of comparative maturity mainly contains: stepwise refrigeration process, swell refrigeration technology and mixed working fluid refrigeration process.Single mixed working fluid refrigeration process wherein then relatively receives the favor of medium-sized LNG device.
In the natural gas liquefaction of existing single mixed working fluid refrigeration, the cryogen compressibility is the secondary compression, and the one-level heat exchange is adopted in natural gas liquefaction.
Existing technology: as shown in Figure 1, the device of its use comprises a motor-driven two-period form mixed working fluid compressor, two coolers, two gas-liquid separators, two liquid pumps, a platen fin heat exchanger and a LNG storage tank; The mixed working fluid of being made up of C1～C5 and N2 is through getting into the inlet of compressor behind the rational proportion; Be compressed to 0.6～1MPa through one section; Get into the one-level cooler and be cooled to 30～40 ℃; Get into the one-level knockout drum again and carry out gas-liquid separation, the isolated gas in one-level knockout drum top continues to get into two sections inlets of compressor, is compressed to 1.6～2.5MPa through two sections; One-level is separated the bottom and is separated the liquid that the obtains gas through liquid pump pressurization back and two sections compressor outlets and be mixed into secondary coolers and be cooled to 30～40 ℃; Cooled mixed working fluid gets into the secondary knockout drum subsequently and carries out gas-liquid separation, and the liquid after the separation mixes the laggard plate-fin heat exchanger of going into through secondary liquid pump pressurization back and gas that this separator top obtains, and this plate-fin heat exchanger is returned in throttling again after precooling to the uniform temperature; For whole heat transfer process provides cold, natural gas is through getting in the LNG storage tank behind the plate-fin heat exchanger.
In above-mentioned technology; For guaranteeing that liquids and gases get into same plate-fin heat exchanger passage and participate in heat exchange; The liquid of final stage gas-liquid separator bottom must pressurize to overcome the head of liquid that difference in height that the separator bottom liquid exports to plate-fin heat exchanger top cryogen inlet is brought, and must realize through increasing final stage liquid pump.Cryogen and the natural gas heat transfer process in plate-fin heat exchanger is the one-level heat exchange, and the optimization of heat transfer temperature difference receives certain limitation between the stream thigh, and plant energy consumption is higher, in addition, the varying duty running of installing is not had excellent adaptability.
In addition; One Chinese patent application publication No. CN 101967413A discloses and a kind ofly adopted single mixed working fluid to freeze to come the method and apparatus of liquefied natural gas, and is as shown in Figure 2, and this device comprises syllogic mixed working fluid compressor 1, three coolers 21,22,23; Five gas- liquid separators 31,32,33,71,72; 51,52,53 and LNG storage tanks of two liquid pumps, 41,42, three throttling arrangements, 61,62,63, three platen fin heat exchangers; The shortcoming of this device is to need to use liquid pump 41,42, and energy requirement is high.
The utility model content
The utility model adopts single mixed working fluid refrigeration to make natural gas liquefaction.
The utility model provides a kind of device that adopts single mixed working fluid refrigeration liquefying natural gas; It comprises azeotrope compressibility and ice chest system; Wherein the azeotrope compressibility adopts syllogic or two-period form mixed working fluid compressor compresses; And when the azeotrope compressibility adopts syllogic mixed working fluid compressor compresses; This compressibility comprises syllogic mixed working fluid compressor, three coolers that are connected with each section of syllogic mixed working fluid compressor respectively and three gas-liquid separators that are connected with said three coolers respectively; The ice chest system comprises one group of plate-fin heat exchanger group being connected with the liquid phase end of said three gas-liquid separators, five throttling arrangements that are connected with the heat exchanger channels of said plate-fin heat exchanger group and two gas-liquid separators that are connected with an independent heat exchanger channels of said plate-fin heat exchanger group; Wherein two gas phase end in three gas-liquid separators is connected with three sections compressions with two sections compressions of syllogic mixed working fluid compressor respectively, and another gas phase end is connected with the heat exchanger channels of said one group of plate-fin heat exchanger group;
Or when the azeotrope compressibility adopts two-period form mixed working fluid compressor compresses; This compressibility comprises two-period form mixed working fluid compressor, two coolers that are connected with each section of said two-period form mixed working fluid compressor respectively and two gas-liquid separators that are connected with said two coolers respectively; Two gas-liquid separators that four throttling arrangements that the ice chest system comprises one group of plate-fin heat exchanger group being connected with the liquid phase end of said two gas-liquid separators, be connected with the heat exchanger channels of said plate-fin heat exchanger group are connected with the heat exchanger channels with said plate-fin heat exchanger group; Wherein one gas phase end in two gas-liquid separators is connected with two sections compressions of two-period form mixed working fluid compressor, and another gas phase end is connected with the heat exchanger channels of said one group of plate-fin heat exchanger group.
The utility model adopts single mixed working fluid to freeze to come the device of liquefied natural gas, and it is divided into natural gas circulation and mixed working fluid kind of refrigeration cycle.In the mixed working fluid loop, mixed working fluid is followed gas-liquid separation step by step in the compression process through multi-stage compression at it step by step simultaneously, and isolated liquid phase stream thighs at different levels are not all participated in follow-up compression process, have effectively reduced postorder gas compression power consumption; Mixed working fluid separates gas phase and the liquid phase stream thigh that obtains before getting into heat exchanger package participation heat exchange, get into the different passage throttling heat exchange of heat exchanger package respectively, and the heat exchange curve of hot-fluid thigh and cold flow thigh more matees in the whole process; The liquid phase that gas-liquid separator separates at different levels go out all relies on pressure differential to get into heat exchanger package, and does not need pump that power is provided, thereby has reduced the energy consumption of system.
In one embodiment; The single mixed working fluid of the said employing of the utility model freezes and comes the device of liquefied natural gas; Comprise mixed working fluid compressor, cooler, gas-liquid separator, throttling arrangement, one group of plate-fin heat exchanger group and a LNG storage tank; This syllogic mixed working fluid compressor can be by a motor-driven; Its mix refrigerant compressibility comprises syllogic mixed working fluid compressor, three coolers and three gas-liquid separators, and the ice chest system comprises one group of plate-fin heat exchanger group (Pyatyi heat exchange), five throttling arrangements and two gas-liquid separators (comprising a heavy hydrocarbon separator); In the azeotrope compressibility; The compressor one section outlet connects the one-level cooler, and the one-level cooler is connected with the one-level gas-liquid separator again, and one-level gas-liquid separator gas phase end connects two sections compressions; Two sections compressions connect secondary coolers; Secondary coolers is connected with the secondary gas-liquid separator again, and secondary gas-liquid separator gas phase end connects three sections compressions, and three sections compressions connect three grades of coolers; Three grades of coolers connect three grades of gas-liquid separators again, and three grades of gas-liquid separator top gas phase ends are connected with heat exchanger package first heat exchanger channels (gas phase heat exchanger channels); One-level gas-liquid separator, secondary gas-liquid separator and three grades of gas-liquid separator bottom liquid phases ends respectively with heat exchanger package second, third, the 4th heat exchanger channels (liquid phase heat exchanger channels) is connected;
In the ice chest system, the one-level gas-liquid separator liquid phase end by the azeotrope compressibility is through an end of the connection of second heat exchanger channels in heat exchanger package first throttle device, and the other end of first throttle device is connected with the 5th heat exchanger channels of heat exchanger package; The secondary gas-liquid separator liquid phase end that is come by the cryogen compressor assembly is connected with an end of second throttling arrangement through heat exchanger package the 3rd heat exchanger channels, and the other end of second throttling arrangement is connected with the 5th heat exchanger channels of heat exchanger package; Connect the 3rd throttling arrangement again after the liquid phase end that three grades of gas-liquid separators bottom obtains connects heat exchanger package the 4th heat exchanger channels, the 3rd throttling arrangement other end is connected with heat exchanger package the 5th heat exchanger channels; The gas phase that three grades of gas-liquid separator tops obtain connects gas-liquid separator after through heat exchanger package first heat exchanger channels (gas phase channel) precooling; Gas phase cryogen after the separation connects the 7th passage of heat exchanger package; After cooling off in the subsequent stages heat exchanger of entering heat exchanger package; Be connected with the 4th throttling arrangement one end, the 4th throttling arrangement other end connects heat exchanger package the 5th heat exchanger channels; The liquid phase cryogen that the separator bottom obtains connects the 8th passage of heat exchanger package; After cooling off in the back first-class heat exchanger of entering heat exchanger package; Be connected with the 5th throttling arrangement one end, connect one section compression behind the five-way road of the 5th throttling arrangement other end connection heat exchanger package; Natural gas line connects the heavy hydrocarbon separator through heat exchanger package the 6th heat exchanger channels, and separator top gas phase end is successively through all the other heat exchangers at different levels of heat exchanger package.
In another embodiment; The single mixed working fluid of the said employing of the utility model freezes and comes the device of liquefied natural gas; Comprise two-period form mixed working fluid compressor, cooler, gas-liquid separator, throttling arrangement, one group of plate-fin heat exchanger group and a LNG storage tank, this two-period form mixed working fluid compressor can be by a motor-driven.The compressibility of its mix refrigerant comprises two-period form mixed working fluid compressor, two coolers, two gas-liquid separators, and the ice chest system comprises one group of plate-fin heat exchanger group (level Four heat exchange), two gas-liquid separators (comprising a heavy hydrocarbon separator) and four throttling arrangements; Mixed working fluid and natural gas are accomplished whole heat transfer process in the ice chest system.In the azeotrope compressibility; The compressor one section outlet connects the one-level cooler; The one-level cooler is connected with the one-level gas-liquid separator again, and one-level gas-liquid separator gas phase end connects two sections compressions, and two sections compressions connect secondary coolers; Secondary coolers is connected with the secondary gas-liquid separator again, and secondary gas-liquid separator top gas phase end is connected with heat exchanger package first heat exchanger channels (gas phase channel); One-level gas-liquid separator, secondary gas-liquid separator bottom liquid phases end are connected with the 3rd heat exchanger channels with heat exchanger package second heat exchanger channels respectively;
In the ice chest system, the one-level gas-liquid separator liquid phase end by the azeotrope compressibility is through an end of the connection of second heat exchanger channels in heat exchanger package first throttle device, and the other end of first throttle device is connected with the 4th heat exchanger channels of heat exchanger package; The secondary gas-liquid separator liquid phase end that is come by the cryogen compressor assembly is connected with an end of second throttling arrangement through heat exchanger package the 3rd heat exchanger channels, and the other end of second throttling arrangement is connected with the 4th heat exchanger channels of heat exchanger package; The gas phase that secondary gas-liquid separator top obtains connects gas-liquid separator after through heat exchanger package first heat exchanger channels (gas phase channel) precooling; Gas phase cryogen after the separation connects the 6th passage of heat exchanger package; After getting into the subsequent stages heat exchanger cooling of heat exchanger package; Be connected with the 3rd throttling arrangement one end, the 3rd throttling arrangement other end connects heat exchanger package the 4th heat exchanger channels; The liquid phase cryogen that the separator bottom obtains connects the 7th passage of heat exchanger package, after the back first-class heat exchanger cooling of entering heat exchanger package, is connected with the 4th throttling arrangement, and the 4th throttling arrangement other end connects one section compression after connecting heat exchanger package the 4th heat exchanger channels; Natural gas line connects separator through heat exchanger package the 5th heat exchanger channels, and separator top gas phase end is successively through all the other heat exchangers at different levels of heat exchanger package.
The technical scheme of the utility model is summarized as follows:
Adopt the device of single mixed working fluid refrigeration liquefying natural gas, it comprises azeotrope compressibility and ice chest system, and wherein the azeotrope compressibility adopts syllogic or two-period form mixed working fluid compressor compresses,
When the azeotrope compressibility adopts syllogic mixed working fluid compressor compresses; This compressibility comprises syllogic mixed working fluid compressor, be connected with first compression section, second compression section and the 3rd compression section of syllogic mixed working fluid compressor respectively first, second and the 3rd cooler and first, second that is connected with said three coolers respectively and the 3rd gas-liquid separator, and
The ice chest system comprises:
One group of plate-fin heat exchanger group, it comprises at least nine heat exchanger channels, promptly comprises the first, second, third, fourth, the 5th, the 6th, the 7th, the 8th and the 9th heat exchanger channels at least,
The first throttle device that two ends connect with said second heat exchanger channels and the 5th heat exchanger channels (promptly compile heat exchanger channels, turn back to first compression section from it) respectively;
Second throttling arrangement that two ends are connected with the 5th heat exchanger channels with said the 3rd heat exchanger channels respectively;
The 3rd throttling arrangement that two ends are connected with the 5th heat exchanger channels with said the 4th heat exchanger channels respectively;
The 4th throttling arrangement that two ends are connected with the 5th heat exchanger channels with said the 7th heat exchanger channels respectively;
The 5th throttling arrangement that two ends are connected with the 5th heat exchanger channels with said the 8th heat exchanger channels respectively;
The 4th gas-liquid separator that is connected with first heat exchanger channels of said plate-fin heat exchanger group;
The 5th gas-liquid separator that is connected with the 6th heat exchanger channels of said plate-fin heat exchanger group (being natural gas heavy hydrocarbon separator);
Wherein, The gas phase end of first gas-liquid separator is connected to second compression section; The gas phase end of second gas-liquid separator is connected to the 3rd compression section; The gas phase end of the 3rd gas-liquid separator is connected to the 4th gas-liquid separator via first heat exchanger channels, and the liquid phase end of first gas-liquid separator is connected to second heat exchanger channels, and the liquid phase end of second gas-liquid separator is connected to the 3rd heat exchanger channels; The liquid phase end of the 3rd gas-liquid separator is connected to the 4th heat exchanger channels; Be used to carry the pipeline that purifies the back natural gas to be connected to the 5th gas-liquid separator (being natural gas heavy hydrocarbon separator) via the 6th heat exchanger channels, the gas phase end of the 5th gas-liquid separator is connected to natural gas storage tank via the 9th heat exchanger channels, and the liquid phase end of the 4th gas-liquid separator is connected to the 5th heat exchanger channels via the 8th heat exchanger channels and the 5th throttling arrangement; And the gas phase end of the 4th gas-liquid separator is connected to the 5th heat exchanger channels via the 7th heat exchanger channels and the 4th throttling arrangement, and the 5th heat exchanger channels is connected to first compression section;
Or
When the azeotrope compressibility adopts two-period form mixed working fluid compressor compresses; This compressibility comprises two-period form mixed working fluid compressor, be connected with second compression section with first compression section of two-period form mixed working fluid compressor respectively first and second cooler and first and second gas-liquid separator being connected with said two coolers respectively, and
The ice chest system comprises:
One group of plate-fin heat exchanger group, it comprises at least eight heat exchanger channels, promptly comprises the first, second, third, fourth, the 5th, the 6th, the 7th and the 8th heat exchanger channels at least,
The first throttle device that two ends connect with said second heat exchanger channels and the 4th heat exchanger channels (promptly compile heat exchanger channels, turn back to first compression section from it) respectively;
Second throttling arrangement that two ends are connected with the 4th heat exchanger channels with said the 3rd heat exchanger channels respectively;
The 3rd throttling arrangement that two ends are connected with the 4th heat exchanger channels with said the 6th heat exchanger channels respectively;
The 4th throttling arrangement that two ends are connected with the 4th heat exchanger channels with said the 7th heat exchanger channels respectively;
The 3rd gas-liquid separator that is connected with first heat exchanger channels of said plate-fin heat exchanger group;
The 4th gas-liquid separator that is connected with the 5th heat exchanger channels of said plate-fin heat exchanger group (being natural gas heavy hydrocarbon separator);
Wherein, The gas phase end of first gas-liquid separator is connected to second compression section; The gas phase end of second gas-liquid separator is connected to the 3rd gas-liquid separator via first heat exchanger channels; The liquid phase end of first gas-liquid separator is connected to second heat exchanger channels; The liquid phase end of second gas-liquid separator is connected to the 3rd heat exchanger channels, is used to carry the pipeline that purifies the back natural gas to be connected to the 4th gas-liquid separator (being natural gas heavy hydrocarbon separator) via the 5th heat exchanger channels, and the gas phase end of the 4th gas-liquid separator is connected to natural gas storage tank via the 8th heat exchanger channels; The liquid phase end of the 3rd gas-liquid separator is connected to the 4th heat exchanger channels via the 7th heat exchanger channels and the 4th throttling arrangement, and the 4th heat exchanger channels is connected to first compression section of azeotrope compressibility.
In addition; When the azeotrope compressibility adopts syllogic mixed working fluid compressor compresses, the top gas phase end of heavy hydrocarbon separator successively through behind the 9th heat exchanger channels of heat exchanger package further other the tenth heat exchanger channels through heat exchanger package be connected to LNG tank; Or; When the azeotrope compressibility adopts two-period form mixed working fluid compressor compresses, the top gas phase end of heavy hydrocarbon separator successively through behind the 8th heat exchanger channels of heat exchanger package further other the 9th heat exchanger channels through heat exchanger package be connected to LNG tank.
" first section compression " described here or " one section compression " and " first compression section " interchangeable use, by that analogy.
Operating process is described below.
The device of the said employing syllogic of the utility model mixed working fluid compressibility; In its azeotrope compressibility; Compressor one section outlet gas gets into one-level cooler cooling back through the one-level gas-liquid separator separates; Gas phase after the separation continues to get into two sections compressions, and the hot gas after the compression gets into the secondary gas-liquid separator separates after the secondary coolers cooling, and the gas phase after the separation continues to get into three sections compressions; Hot gas after the compression gets into three grades of gas-liquid separator separates after three grades of cooler coolings, the gas phase after the separation gets into first heat exchanger channels (gas phase channel) of downstream heat exchanger; The liquid that one-level gas-liquid separator, secondary gas-liquid separator and three grades of gas-liquid separator bottoms obtain gets into second, third and the four or three liquid phase heat exchanger channels of downstream heat exchanger respectively.In the ice chest system, the liquid cryogen that bottom cryogen compressibility one-level gas-liquid separator, comes passes through the first throttle device after getting into the heat exchanger package precooling, and this stream thigh after the throttling is back to cold is provided in the heat exchanger package; The liquid cryogen that is come by secondary gas-liquid separator bottom passes through second throttling arrangement after the heat exchanger package precooling, the stream thigh after the throttling returns heat exchanger package provides cold; The liquid cryogen that is come by three grades of gas-liquid separator bottoms passes through the 3rd throttling arrangement after the heat exchanger package precooling, the stream thigh after the throttling returns cold is provided in the heat exchanger package; The gas phase cryogen that is come by the cryogen compressibility gets into separator after the heat exchanger package precooling; After cooling off in the subsequent stages heat exchanger of the gas phase cryogen entering heat exchanger package after the separation; Through the 4th throttling arrangement throttling, burst reverse heat exchanger package that gets into of this stream after the throttling provides cold; After separating the back first-class heat exchanger cooling of the liquid phase cryogen entering heat exchanger package that obtains, through the 5th throttling arrangement throttling, burst reverse entering heat exchanger package of this stream after the throttling provides cold.Natural gas gets into separator separates after at first being cooled to uniform temperature through heat exchanger package, and the bottom obtains the heavy hydrocarbon component, and the gas phase that the top obtains partly continues to get into all the other heat exchanger heat exchange at different levels of heat exchanger package, is cooled to supercooled state and obtains LNG.
The device of the said employing two-period form of the utility model mixed working fluid compressibility; In its azeotrope compressibility; Compressor one section outlet gas gets into one-level cooler cooling back through the one-level gas-liquid separator separates; Gas phase after the separation continues to get into two sections compressions, and the hot gas after the compression gets into the secondary gas-liquid separator separates after the secondary coolers cooling, and the gas phase after the separation gets into first heat exchanger channels (gas phase channel) of downstream heat exchanger; The liquid that one-level gas-liquid separator, secondary gas-liquid separator bottom obtain gets into second and the 3 two liquid phase heat exchanger channels of downstream heat exchanger respectively.In the ice chest system, the liquid cryogen that bottom cryogen compressibility one-level gas-liquid separator, comes passes through the first throttle device after getting into the heat exchanger package precooling, and this stream thigh after the throttling is back to cold is provided in the heat exchanger package; The liquid cryogen that is come by secondary gas-liquid separator bottom passes through second throttling arrangement after the heat exchanger package precooling, the stream thigh after the throttling returns heat exchanger package provides cold; The gas phase cryogen that is come by secondary gas-liquid separator top gets into separator after the heat exchanger package precooling; After cooling off in the subsequent stages heat exchanger of the gas phase cryogen entering heat exchanger package after the separation; Through the 3rd throttling arrangement throttling, burst reverse heat exchanger package that gets into of this stream after the throttling provides cold; After the liquid phase cryogen that the separator bottom obtains got into the back first-class heat exchanger cooling of heat exchanger package, through the 4th throttling arrangement throttling, burst reverse heat exchanger package that gets into of this stream after the throttling provided cold.Natural gas gets into separator separates after at first being cooled to uniform temperature through heat exchanger package, and the bottom obtains the heavy hydrocarbon component, and the gas phase that the top obtains partly continues to get into all the other heat exchanger heat exchange at different levels of heat exchanger package, is cooled to supercooled state and obtains LNG.
The technological process of the device that adopts single mixed working fluid to freeze to come liquefied natural gas is following:
The natural gas circulation:
Raw natural gas after the purification at first gets into the plate-fin heat exchanger group and carries out precooling; Get into heavy hydrocarbon separator (gas-liquid separator) after being cooled to-30 ℃～-60 ℃ and carry out gas-liquid separation; Continue to get into all the other heat exchangers at different levels of heat exchanger package by the isolated vapor phase stream thigh in heavy hydrocarbon separator top; And be cooled to-130 ℃～-166 ℃ therein, obtain the LNG product and send in the LNG storage tank storing.
The azeotrope circulation:
Adopt the device of syllogic mixed working fluid compressibility, its mixed working fluid circulation technology flow process is:
By C1～C5 and N
2The mixed working fluid of forming is selected from C1, C2, C3, C4 and C5 alkane and N usually
2In four kinds, five kinds or six kinds; They are according to the arbitrary volume ratio or according to the volume ratio that approximately is equal to; Get into the inlet of compressor, warp is compressed to 0.6～1.8MPaA for one section, gets into the one-level cooler and is cooled to 30 ℃～40 ℃; Get into the one-level gas-liquid separator again and carry out gas-liquid separation; The isolated gas in one-level gas-liquid separator top continues to get into two sections inlets of compressor, gets into secondary coolers through two sections again after being compressed to 1.2～5.4MPaA and is cooled to 30 ℃～40 ℃, and cooled mixed working fluid gets into the secondary gas-liquid separator subsequently and carries out gas-liquid separation; Secondary gas-liquid separator top gas continues to get into three sections inlets of compressor; Finally be compressed into to draw compressor and get into aftercooler behind 2.4～8.0MPaA and be cooled to 30 ℃～40 ℃, cooled working medium continues to get into the final stage gas-liquid separator and carries out gas-liquid separation, and the isolated gas in final stage gas-liquid separator top gets into the gas phase channel of main heat exchanger group subsequently and participates in heat exchange.The different liquids passage that one-level gas-liquid separator, secondary gas-liquid separator and three grades of isolated liquid in gas-liquid separator bottom get into the main heat exchanger group is respectively participated in heat exchange.
The liquid of drawing from mixed working fluid compressibility one-level gas-liquid separator bottom at first gets into a liquid channel of heat exchanger package; Therein by precooling to about 10 ℃～-10 ℃, strand converging and oppositely get into the previous stage heat exchanger through the mixed working fluid stream that returns with first-class heat exchanger after heat exchanger package behind choke valve throttling to 0.25～0.8MPaA provides cold for it.The liquid of being drawn by secondary gas-liquid separator bottom is through another liquid channel precooling to 0 of heat exchanger package ℃～-30 ℃; Again behind choke valve throttling to 0.25～0.8MPaA, the mixed working fluid stream thigh that returns with first-class heat exchanger after heat exchanger package converges and returns heat exchanger package previous stage heat exchanger.The liquid of bottom final stage (three grades) gas-liquid separator, drawing is through another liquid channel of heat exchanger package; And precooling therein is to-30 ℃～-80 ℃; After choke valve throttling to 0.25～0.8MPaA, the mixed working fluid stream thigh that returns with first-class heat exchanger after heat exchanger package converges and returns the previous stage heat exchanger.Get into gas-liquid separator by after the vapor phase stream thigh of the isolated mixed working fluid in the final stage gas-liquid separator top gas phase channel precooling to 10 through heat exchanger package ℃～-30 ℃; Be cooled to-135 ℃～-171 ℃ in the follow-up heat exchanger of gas phase cryogen after the separation through another gas phase channel entering heat exchanger package of heat exchanger package, reverse entering heat exchanger package is that heat exchanger provides cold behind choke valve throttling to 0.25～0.8MPaA again.The liquid phase cryogen that the gas-liquid separator bottom obtains is cooled to-30 ℃～-100 ℃ through the back first-class heat exchanger of another liquid channel entering heat exchanger package of heat exchanger package; Again through choke valve throttling to 0.25～0.8MPaA, the mixed working fluid stream thigh that returns with first-class heat exchanger after heat exchanger package converges and returns the previous stage heat exchanger.
Adopt the device of two-period form mixed working fluid compressibility, its mixed working fluid circulation technology flow process is:
By C1～C5 and N
2The mixed working fluid of forming is selected from C1, C2, C3, C4 and C5 alkane and N usually
2In four kinds, five kinds or six kinds; They get into the inlet of compressor according to the arbitrary volume ratio or according to the volume ratio that approximately is equal to, and are compressed to 0.6～1.8MPaA through one section; Get into the one-level cooler and be cooled to 30 ℃～40 ℃; Get into the one-level gas-liquid separator again and carry out gas-liquid separation, the isolated gas in one-level gas-liquid separator top continues to get into two sections inlets of compressor, gets into secondary coolers through two sections again after being compressed to 1.2～5.4MPaA and is cooled to 30 ℃～40 ℃; Cooled mixed working fluid gets into the secondary gas-liquid separator subsequently and carries out gas-liquid separation, and secondary gas-liquid separator top gas gets into the gas phase channel of main heat exchanger group subsequently and participates in heat exchange.The isolated liquid of one-level gas-liquid separator and secondary gas-liquid separator bottom gets into the different liquid channels of main heat exchanger group respectively and participates in heat exchange.
The liquid of drawing from mixed working fluid compressibility one-level gas-liquid separator bottom at first gets into a liquid channel of heat exchanger package; By extremely about 10 ℃～-30 ℃ of precoolings, converging and oppositely get into the previous stage heat exchanger through the mixed working fluid stream thigh that returns with first-class heat exchanger after heat exchanger package behind choke valve throttling to 0.25～0.8MPaA is that heat exchanger package provides cold therein.The liquid of being drawn by secondary gas-liquid separator bottom passes through another liquid channel precooling of heat exchanger package to-30 ℃～-80 ℃; Again behind choke valve throttling to 0.25～0.8MPaA, the mixed working fluid stream thigh that returns with first-class heat exchanger after heat exchanger package converges and returns heat exchanger package previous stage heat exchanger.Get into separator by after the vapor phase stream thigh of the isolated mixed working fluid in the secondary gas-liquid separator top gas phase channel precooling to 10 through heat exchanger package ℃～-30 ℃; Separate in the follow-up heat exchanger of gas phase cryogen that obtains being cooled to-135 ℃～-171 ℃, the more reverse heat exchanger package that gets into behind choke valve throttling to 0.25～0.8MPaA through another gas phase channel continuation entering heat exchanger package of heat exchanger package.Be cooled to-30 ℃～-100 ℃ in the back first-class heat exchanger of the liquid phase cryogen that the separator bottom obtains through another liquid channel entering heat exchanger package of heat exchanger package; After choke valve throttling to 0.25～0.8MPaA, after converging, the mixed working fluid stream thigh that returns with first-class heat exchanger after heat exchanger package returns the previous stage heat exchanger.
Here, pressure unit MPaA is a MPa, absolute pressure.
The advantage of the utility model:
1. three grades of (or secondary) azeotrope compressors have been adopted in the utility model device; Azeotrope is compressed and separation step by step step by step; Isolated liquid at different levels directly get into heat exchanger and carry out heat exchange, reduced the power consumption of gas compression, and the heat exchange curve of the cold fluid of whole heat transfer process and hot fluid mate more; Effectively reduce the flow of azeotrope, finally made the energy consumption of whole device decrease.
2. each gas-liquid separator bottom liquid stream thigh is directly sent into heat exchanger and without the subsequent handling of compressor, has been reduced the influence degree of the fluctuation of azeotrope proportioning to the compressor bank operating condition to a certain extent, makes whole device be easier to operation.
3. the vapor phase stream thigh that obtains of cryogen compressibility final stage separator has increased gas-liquid separator after the precooling in the main heat exchanger group; Varying duty running to device has excellent adaptability on the one hand, can effectively avoid ice chest bottom hydrops and heavy component crystallization, thereby guarantee when running on the lower load; Product energy consumption and nominal situation energy consumption are approaching; The cold fluid of heat transfer process and the heat exchange curve of hot fluid are more mated, thereby reduce the azeotrope flow, reduce plant energy consumption.
4. in the azeotrope compressibility, the liquid phase that gas-liquid separator separates at different levels go out all relies on pressure differential directly to get into heat exchanger package, and does not need pump that power is provided, thereby has reduced the energy consumption of system.
Description of drawings
Fig. 1 is a kind of structure chart of prior art;
Fig. 2 is the another kind of structure chart of prior art;
Fig. 3 is the device allocation plan of the said employing syllogic of the utility model mixed working fluid compressibility;
Fig. 4 is the device allocation plan of the said employing two-period form of the utility model mixed working fluid compressibility.
The specific embodiment
Further specify below in conjunction with accompanying drawing.
Device shown in Figure 3 comprises a motor-driven syllogic mixed working fluid compressor 1, cooler 21,22,23, gas-liquid separator 31,32,33,5,6; Throttling arrangement 41,42,43,44,45; One group of plate-fin heat exchanger group 7 and a LNG storage tank 8, its mix refrigerant compressibility comprise 21,22,23 and three gas-liquid separators 31,32,33 of 1, three cooler of syllogic mixed working fluid compressor; The ice chest system comprises one group of plate-fin heat exchanger group 7 (Pyatyi heat exchange); 41,42,43,44,45, one gas-liquid separators of five throttling arrangements 5, a heavy hydrocarbon separator 6 (also be gas-liquid separator, be known as the 5th gas-liquid separator here); In the azeotrope compressibility; The compressor one section outlet connects one-level cooler 21, and one-level cooler 21 is connected with one-level gas-liquid separator 31 again, and one-level gas-liquid separator 31 gas phase ends connect two sections compressions; Two sections compressions connect secondary coolers 22; Secondary coolers 22 is connected with secondary gas-liquid separator 32 again, and secondary gas-liquid separator 32 gas phase ends connect three sections compressions, and three sections compressions connect three grades of coolers 23; Three grades of coolers 23 connect 33, three grades of gas-liquid separators of three grades of gas-liquid separators, 33 top gas phase ends again and are connected with heat exchanger package first heat exchanger channels (gas phase heat exchanger channels); One-level gas-liquid separator 31, secondary gas-liquid separator 32 and three grades of gas-liquid separators 33 separately the bottom the liquid phase end respectively with heat exchanger package 7 second, third, the 4th heat exchanger channels (liquid phase heat exchanger channels) is connected;
In the ice chest system; One-level gas-liquid separator 31 liquid phase ends by the azeotrope compressibility are through an end of the connection of second heat exchanger channels in the heat exchanger package 7 first throttle device 41, and the other end of first throttle device 41 is connected with the 5th heat exchanger channels (be called here and compile heat exchanger channels) of heat exchanger package; The secondary gas-liquid separator 32 liquid phase ends that come by the cryogen compressor assembly are connected with an end of second throttling arrangement 42 through heat exchanger package 7 the 3rd heat exchanger channels, and the other end of second throttling arrangement 42 is connected with the 5th heat exchanger channels of heat exchanger package 7; The liquid phase end that three grades of gas-liquid separator 33 bottoms obtain connects and connects the 3rd throttling arrangement 43, the three throttling arrangements 43 other ends again behind the 4th heat exchanger channels of heat exchanger package 7 and be connected with heat exchanger package the 5th heat exchanger channels; The gas phase that three grades of gas-liquid separator 33 tops obtain is connected to gas-liquid separator 5 through first heat exchanger channels (gas phase channel) of heat exchanger package 7 after the precooling; The output channel of the gas phase cryogen after the separation is connected to the 7th passage of heat exchanger package 7; After getting into the middle cooling of subsequent stages heat exchanger (for example the 7th heat exchanger channels) of heat exchanger package 7; Be connected with the 4th throttling arrangement 44 1 ends, the 4th throttling arrangement 44 other ends are connected to the 5th heat exchanger channels of heat exchanger package 7; The output channel of the liquid phase cryogen that the 4th separator 5 bottoms obtain is connected to the 8th passage of heat exchanger package 7; After getting into the middle cooling of back first-class heat exchanger (for example the 8th heat exchanger channels) of heat exchanger package 7; Be connected with the 5th throttling arrangement 45 1 ends, five-way road and this five-way road that the other end of the 5th throttling arrangement 45 connects heat exchanger package 7 are connected to one section compression; Be used to carry the pipeline of purified natural gas to be connected to heavy hydrocarbon separator 6 through heat exchanger package the 6th heat exchanger channels; Heavy hydrocarbon separator 6 top gas phase ends are (the 9th heat exchanger channels for example of all the other heat exchangers at different levels through heat exchanger package 7 successively; Randomly can also be further through the tenth heat exchanger channels), be connected to storage tank 8.
Device shown in Figure 4 comprises two-period form mixed working fluid compressor 1, cooler 21,22, gas-liquid separator 31,32,41,42,43,44, one groups of plate-fin heat exchanger groups 7 of throttling arrangement and a LNG storage tank 8.The compressibility of its mix refrigerant comprises two-period form mixed working fluid compressor 1; Two coolers 21,22; Two gas-liquid separators 31,32, the ice chest system comprises one group of plate-fin heat exchanger group 7 (level Four heat exchange), gas-liquid separator 5, heavy hydrocarbon separator 6 (gas-liquid separator), 41,42,43,44 and LNG storage tanks 8 of four throttling arrangements; Mixed working fluid and natural gas are accomplished whole heat transfer process in the ice chest system.In the azeotrope compressibility; Compressor 1 one section outlet connects one-level cooler 21; One-level cooler 21 is connected with one-level gas-liquid separator 31 again, and one-level gas-liquid separator 31 gas phase ends connect two sections compressions, and two sections compressions connect secondary coolers 22; Secondary coolers 22 is connected with secondary gas-liquid separator 32 again, and secondary gas-liquid separator 32 top gas phase ends are connected with heat exchanger package first heat exchanger channels (gas phase channel); One-level gas-liquid separator 31, secondary gas-liquid separator 32 bottom liquid phases ends are connected with the 3rd heat exchanger channels with heat exchanger package second heat exchanger channels respectively;
In the ice chest system; One-level gas-liquid separator 31 liquid phase ends by the azeotrope compressibility are through an end of the connection of second heat exchanger channels in the heat exchanger package 7 first throttle device 41, and the other end of first throttle device 41 is connected with the 4th heat exchanger channels (be also referred to as and compile heat exchanger channels) of heat exchanger package; The secondary gas-liquid separator 32 liquid phase ends that come by the cryogen compressor assembly are connected with an end of second throttling arrangement 42 through heat exchanger package 7 the 3rd heat exchanger channels, and the other end of second throttling arrangement 42 is connected with the 4th heat exchanger channels of heat exchanger package 7; The gas phase that secondary gas-liquid separator 32 tops obtain is through connecting gas-liquid separator 5 after heat exchanger package 7 first heat exchanger channels (gas phase channel) precoolings; Gas phase cryogen after the separation connects the 6th passage of heat exchanger package; After getting into subsequent stages heat exchanger (for example the 6th heat exchanger channels) cooling of heat exchanger package; Be connected with the 3rd throttling arrangement 43 1 ends, the 3rd throttling arrangement 43 other ends connect heat exchanger package the 4th heat exchanger channels; The liquid phase cryogen that separator 5 bottoms obtain connects the 7th passage of heat exchanger package 7; After getting into the back first-class heat exchanger cooling of heat exchanger package 7; Be connected with the 4th throttling arrangement 44, the 4th throttling arrangement 44 other ends connect one section compression after connecting heat exchanger package 7 the 4th heat exchanger channels; Natural gas line connects heavy hydrocarbon separator 6 through heat exchanger package the 5th heat exchanger channels; Heavy hydrocarbon separator 6 top gas phase ends are successively through all the other heat exchangers at different levels of heat exchanger package (the 8th heat exchanger channels for example; Randomly can also be further through the 9th heat exchanger channels), connect storage tank 8 again.
The technological process of the device of use Fig. 3 and Fig. 4 is following:
The natural gas circulation:
Shown in accompanying drawing 3 and accompanying drawing 4; Raw natural gas after the purification at first gets into plate-fin heat exchanger group 7 (Pyatyi heat exchange or level Four heat exchange) and carries out precooling; Get into heavy hydrocarbon separator (gas-liquid separator) 6 after being cooled to-30 ℃～-60 ℃ and carry out gas-liquid separation; Continue to get into all the other heat exchangers at different levels of heat exchanger package by the isolated vapor phase stream thigh in heavy hydrocarbon separator 6 tops; And be cooled to-130 ℃～-166 ℃ therein, and obtaining the LNG product and send in the LNG storage tank 8 storing, the bottom of heavy hydrocarbon separator 6 obtains liquefied petroleum gas (LPG).
The azeotrope circulation:
Adopt the device of syllogic mixed working fluid compressibility, shown in accompanying drawing 3, its mixed working fluid circulation technology flow process is:
By C1～C5 and N
2The mixed working fluid of forming is selected from C1, C2, C3, C4 and C5 alkane and N usually
2In four kinds, five kinds or six kinds; They are according to the arbitrary volume ratio or according to the volume ratio that approximately is equal to; Get into the inlet of compressor 1; Warp is compressed to 0.6～1.8MPaA for one section, gets into one-level cooler 21 and is cooled to 30 ℃～40 ℃, gets into one-level gas-liquid separator 31 again and carries out gas-liquid separation; The isolated gas in one-level gas-liquid separator 31 tops continues to get into two sections inlets of compressor 1; Get into secondary coolers 22 through two sections again after being compressed to 1.2～5.4MPaA and be cooled to 30 ℃～40 ℃, cooled mixed working fluid gets into secondary gas-liquid separator 32 subsequently and carries out gas-liquid separation, and secondary gas-liquid separator 32 top gas continue to get into three sections inlets of compressor 1; Finally be compressed into to draw compressor and get into aftercooler 23 behind 2.4～8.0MPaA and be cooled to 30 ℃～40 ℃; Cooled working medium continues to get into final stage gas-liquid separator 33 and carries out gas-liquid separation, and the isolated gas in final stage gas-liquid separator 33 tops gets into the gas phase channel of main heat exchanger group subsequently and participates in heat exchange, and the different liquids passage that one-level gas-liquid separator 31, secondary gas-liquid separator 32 and three grades of isolated liquid in gas-liquid separator 33 bottoms get into the main heat exchanger group is respectively participated in heat exchange.
The liquid of drawing from mixed working fluid compressibility one-level gas-liquid separator 31 bottoms at first gets into a liquid channel of heat exchanger package 7; By extremely about 10 ℃～-10 ℃ of precoolings, the mixed working fluid stream thigh that behind choke valve 41 throttlings to 0.25～0.8MPaA, returns with first-class heat exchanger after heat exchanger package 7 converges and oppositely gets into the previous stage heat exchanger provides cold for it therein; The liquid of being drawn by secondary gas-liquid separator 32 bottoms is through another liquid channel precooling to 0 of heat exchanger package ℃～-30 ℃; Again behind choke valve 42 throttlings to 0.25～0.8MPaA, converge with the mixed working fluid stream thigh that returns from heat exchanger package 7 back first-class heat exchanger and to return heat exchanger package previous stage heat exchanger; The liquid of being drawn by final stage (three grades) gas-liquid separator 33 bottoms is through another liquid channel of heat exchanger package 7; And precooling therein is to-30 ℃～-80 ℃; After choke valve 43 throttlings to 0.25～0.8MPaA, converge with the mixed working fluid stream thigh that returns from heat exchanger package 7 back first-class heat exchanger and to return the previous stage heat exchanger; Get into gas-liquid separator 5 by after the vapor phase stream thigh of the isolated mixed working fluid in the final stage gas-liquid separator 33 tops gas phase channel precooling to 10 through heat exchanger package ℃～-30 ℃; Be cooled to-135 ℃～-171 ℃ in the follow-up heat exchanger of gas phase cryogen after the separation through another gas phase channel entering heat exchanger package 7 of heat exchanger package 7, the reverse heat exchanger package 7 that gets into provides cold for heat exchanger behind choke valve 44 throttlings to 0.25～0.8MPaA again; The liquid phase cryogen that gas-liquid separator 5 bottoms obtain is cooled to-30 ℃～-100 ℃ through the back first-class heat exchanger of another liquid channel entering heat exchanger package of heat exchanger package 7; Again through choke valve 45 throttlings to 0.25～0.8MPaA, converge with the mixed working fluid stream thigh that returns from heat exchanger package 7 back first-class heat exchanger and to return the previous stage heat exchanger.
Adopt the device of two-period form mixed working fluid compressibility, shown in accompanying drawing 4, its mixed working fluid circulation technology flow process is:
By C1～C5 and N
2The mixed working fluid of forming is selected from C1, C2, C3, C4 and C5 alkane and N usually
2In four kinds, five kinds or six kinds; They are according to the arbitrary volume ratio or according to the volume ratio that approximately is equal to; Get into the inlet of compressor 1; Be compressed to 0.6～1.8MPaA through one section; Get into one-level cooler 21 and be cooled to 30 ℃～40 ℃, get into one-level gas-liquid separator 31 again and carry out gas-liquid separation, the isolated gas in one-level gas-liquid separator 31 tops continues to get into two sections inlets of compressor 1; Get into secondary coolers 22 through two sections again after being compressed to 1.2～5.4MPaA and be cooled to 30 ℃～40 ℃; Cooled mixed working fluid gets into secondary gas-liquid separator 32 subsequently and carries out gas-liquid separation, and secondary gas-liquid separator top gas gets into the gas phase channel of main heat exchanger group 7 subsequently and participates in heat exchange, and the isolated liquid of one-level gas-liquid separator 31 and secondary gas-liquid separator 32 bottoms gets into the different liquid channels of main heat exchanger group 7 respectively and participates in heat exchange.
The liquid of drawing from mixed working fluid compressibility one-level gas-liquid separator 31 bottoms at first gets into a liquid channel of heat exchanger package 7; By extremely about 10 ℃～-30 ℃ of precoolings, behind choke valve 41 throttlings to 0.25～0.8MPaA, converging and oppositely get into the previous stage heat exchanger with the mixed working fluid stream thigh that returns from heat exchanger package 7 back first-class heat exchanger is that heat exchanger package 7 provides cold therein; The liquid of being drawn by secondary gas-liquid separator 32 bottoms passes through heat exchanger package 7 another liquid channel precoolings to-30 ℃～-80 ℃; Again behind choke valve 42 throttlings to 0.25～0.8MPaA, converge with the mixed working fluid stream thigh that returns from heat exchanger package 7 back first-class heat exchanger and to return heat exchanger package 7 previous stage heat exchangers; Get into separator 5 by after the vapor phase stream thigh of the isolated mixed working fluid in the secondary gas-liquid separator 32 tops gas phase channel precooling to 10 through heat exchanger package 7 ℃～-30 ℃; Separate in the follow-up heat exchanger of gas phase cryogen that obtains being cooled to-135 ℃～-171 ℃, the more reverse heat exchanger package 7 that gets into behind choke valve 43 throttlings to 0.25～0.8MPaA through another gas phase channel continuation entering heat exchanger package 7 of heat exchanger package 7; Be cooled to-30 ℃～-100 ℃ in the back first-class heat exchanger of the liquid phase cryogen that separator 5 bottoms obtain through another liquid channel entering heat exchanger package 7 of heat exchanger package 7; After choke valve 44 throttlings to 0.25～0.8MPaA, return the previous stage heat exchanger after converging with the mixed working fluid stream thigh that returns from heat exchanger package 7 back first-class heat exchanger.
Claims (2)
1. adopt the device of single mixed working fluid refrigeration liquefying natural gas, it is characterized in that: it comprises azeotrope compressibility and ice chest system, and wherein the azeotrope compressibility adopts syllogic or two-period form mixed working fluid compressor compresses,
When the azeotrope compressibility adopts syllogic mixed working fluid compressor compresses; This compressibility comprises syllogic mixed working fluid compressor, be connected with first compression section, second compression section and the 3rd compression section of syllogic mixed working fluid compressor respectively first, second and the 3rd cooler and first, second that is connected with said three coolers respectively and the 3rd gas-liquid separator, and
The ice chest system comprises:
One group of plate-fin heat exchanger group, it comprises at least nine heat exchanger channels: the 5th, the 6th, the 7th, the 8th and the 9th heat exchanger channels first, second, third, fourth,,
The first throttle device that two ends are connected with the 5th heat exchanger channels with said second heat exchanger channels respectively;
Second throttling arrangement that two ends are connected with the 5th heat exchanger channels with said the 3rd heat exchanger channels respectively;
The 3rd throttling arrangement that two ends are connected with the 5th heat exchanger channels with said the 4th heat exchanger channels respectively;
The 4th throttling arrangement that two ends are connected with the 5th heat exchanger channels with said the 7th heat exchanger channels respectively;
The 5th throttling arrangement that two ends are connected with the 5th heat exchanger channels with said the 8th heat exchanger channels respectively;
The 4th gas-liquid separator that is connected with first heat exchanger channels of said plate-fin heat exchanger group;
The 5th gas-liquid separator that is connected with the 6th heat exchanger channels of said plate-fin heat exchanger group, i.e. natural gas heavy hydrocarbon separator;
Wherein, The gas phase end of first gas-liquid separator is connected to second compression section; The gas phase end of second gas-liquid separator is connected to the 3rd compression section; The gas phase end of the 3rd gas-liquid separator is connected to the 4th gas-liquid separator via first heat exchanger channels, and the liquid phase end of first gas-liquid separator is connected to second heat exchanger channels, and the liquid phase end of second gas-liquid separator is connected to the 3rd heat exchanger channels; The liquid phase end of the 3rd gas-liquid separator is connected to the 4th heat exchanger channels; Being used to carry the pipeline that purifies the back natural gas to be connected to the 5th gas-liquid separator via the 6th heat exchanger channels is natural gas heavy hydrocarbon separator, and the gas phase end of the 5th gas-liquid separator is connected to natural gas storage tank via the 9th heat exchanger channels, and the liquid phase end of the 4th gas-liquid separator is connected to the 5th heat exchanger channels via the 8th heat exchanger channels and the 5th throttling arrangement; And the gas phase end of the 4th gas-liquid separator is connected to the 5th heat exchanger channels via the 7th heat exchanger channels and the 4th throttling arrangement, and the 5th heat exchanger channels is connected to first compression section;
Or
When the azeotrope compressibility adopts two-period form mixed working fluid compressor compresses; This compressibility comprises two-period form mixed working fluid compressor, be connected with second compression section with first compression section of two-period form mixed working fluid compressor respectively first and second cooler and first and second gas-liquid separator being connected with said two coolers respectively, and
The ice chest system comprises:
One group of plate-fin heat exchanger group, it comprises at least eight heat exchanger channels: the 5th, the 6th, the 7th and the 8th heat exchanger channels first, second, third, fourth,,
The first throttle device that two ends are connected with the 4th heat exchanger channels with said second heat exchanger channels respectively;
Second throttling arrangement that two ends are connected with the 4th heat exchanger channels with said the 3rd heat exchanger channels respectively;
The 3rd throttling arrangement that two ends are connected with the 4th heat exchanger channels with said the 6th heat exchanger channels respectively;
The 4th throttling arrangement that two ends are connected with the 4th heat exchanger channels with said the 7th heat exchanger channels respectively;
The 3rd gas-liquid separator that is connected with first heat exchanger channels of said plate-fin heat exchanger group;
The 4th gas-liquid separator, i.e. natural gas heavy hydrocarbon separator being connected with the 5th heat exchanger channels of said plate-fin heat exchanger group;
Wherein, The gas phase end of first gas-liquid separator is connected to second compression section; The gas phase end of second gas-liquid separator is connected to the 3rd gas-liquid separator via first heat exchanger channels; The liquid phase end of first gas-liquid separator is connected to second heat exchanger channels; The liquid phase end of second gas-liquid separator is connected to the 3rd heat exchanger channels, and being used to carry the pipeline that purifies the back natural gas to be connected to the 4th gas-liquid separator via the 5th heat exchanger channels is natural gas heavy hydrocarbon separator, and the gas phase end of the 4th gas-liquid separator is connected to natural gas storage tank via the 8th heat exchanger channels; The liquid phase end of the 3rd gas-liquid separator is connected to the 4th heat exchanger channels via the 7th heat exchanger channels and the 4th throttling arrangement, and the 4th heat exchanger channels is connected to first compression section of azeotrope compressibility.
2. the device of the single mixed working fluid refrigeration liquefying of employing according to claim 1 natural gas is characterized in that:
When the azeotrope compressibility adopts syllogic mixed working fluid compressor compresses, the top gas phase end of natural gas heavy hydrocarbon separator successively through behind the 9th heat exchanger channels of heat exchanger package further other the tenth heat exchanger channels through heat exchanger package be connected to LNG tank; Or
When the azeotrope compressibility adopts two-period form mixed working fluid compressor compresses, the top gas phase end of natural gas heavy hydrocarbon separator successively through behind the 8th heat exchanger channels of heat exchanger package further other the 9th heat exchanger channels through heat exchanger package be connected to LNG tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201120459035 CN202432825U (en) | 2011-11-18 | 2011-11-18 | Device adopting single refrigeration of mixed working mediums to liquefy natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201120459035 CN202432825U (en) | 2011-11-18 | 2011-11-18 | Device adopting single refrigeration of mixed working mediums to liquefy natural gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202432825U true CN202432825U (en) | 2012-09-12 |
Family
ID=46782265
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201120459035 Expired - Lifetime CN202432825U (en) | 2011-11-18 | 2011-11-18 | Device adopting single refrigeration of mixed working mediums to liquefy natural gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202432825U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103697660A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing LNG and hydrogen-rich products out of high methane gas |
| CN103697661A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of coke oven gas |
| CN104089463A (en) * | 2014-07-16 | 2014-10-08 | 北京安珂罗工程技术有限公司 | Mixed refrigerant gas-liquid separating type throttling and refrigerating method and system |
| CN110173961A (en) * | 2019-06-25 | 2019-08-27 | 杭州杭氧股份有限公司 | A kind of hydrogen and lighter hydrocarbons cryogenic separation device based on efficient plate-fin heat exchanger |
-
2011
- 2011-11-18 CN CN 201120459035 patent/CN202432825U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103697660A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing LNG and hydrogen-rich products out of high methane gas |
| CN103697661A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of coke oven gas |
| CN104089463A (en) * | 2014-07-16 | 2014-10-08 | 北京安珂罗工程技术有限公司 | Mixed refrigerant gas-liquid separating type throttling and refrigerating method and system |
| CN104089463B (en) * | 2014-07-16 | 2017-11-17 | 北京安珂罗工程技术有限公司 | A kind of method and system of azeotrope gas-liquid separating throttling refrigeration |
| CN110173961A (en) * | 2019-06-25 | 2019-08-27 | 杭州杭氧股份有限公司 | A kind of hydrogen and lighter hydrocarbons cryogenic separation device based on efficient plate-fin heat exchanger |
| CN110173961B (en) * | 2019-06-25 | 2024-01-26 | 杭氧集团股份有限公司 | Hydrogen and light hydrocarbon cryogenic separation device based on high-efficiency plate-fin heat exchanger |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102636000B (en) | Method for refrigerating liquefied natural gas by aid of single mixed working medium and device | |
| CN202328997U (en) | Device for refrigerating liquefied natural gas by adopting single mixed working medium | |
| CN202361751U (en) | Device for refrigerating liquefied natural gas by adopting single mixed refrigerant | |
| CN101967413A (en) | Method and device for liquefying natural gas via refrigeration of single mixed refrigerant | |
| CN109140903B (en) | Air separation system and air separation method utilizing cold energy of liquefied natural gas | |
| RU2538192C1 (en) | Method of natural gas liquefaction and device for its implementation | |
| CN104513680B (en) | Technology and device for removing hydrogen and nitrogen from methane-rich gas through rectification and producing liquefied natural gas | |
| CN102748919A (en) | Single-cycle mixed-refrigerant four-stage throttling refrigeration system and method | |
| CN201463463U (en) | Three-phase mixed refrigeration natural-gas liquefying device | |
| WO2023272971A1 (en) | Hydrogen liquefaction system | |
| CN201762300U (en) | Device using single-mixed refrigerant refrigeration to liquefy natural gas | |
| CN202432825U (en) | Device adopting single refrigeration of mixed working mediums to liquefy natural gas | |
| CN114111215A (en) | Device for preparing liquid hydrogen by using low-temperature hydrogen-containing mixed gas and using method | |
| CN202494271U (en) | Device for liquefying natural gas through refrigeration of single mixed working medium | |
| CN103542692B (en) | Based on the Unconventional forage liquefaction system of wrap-round tubular heat exchanger | |
| CN102147162B (en) | Rectifying type variation-concentration self-overlaying gas liquefaction system | |
| CN103398545B (en) | System for producing liquefied natural gas from raw gas by means of multi-stage pressure throttling | |
| CN102564056A (en) | Multi-flow spiral winding tube type main heat exchange equipment with mixed refrigerant for low-temperature liquefaction of LNG (liquefied natural gas) | |
| CN101126041A (en) | Cascade connection method for preparing liquefied natural gas | |
| CN107560321A (en) | BOG is reclaimed and nitrogen gas liquefaction system and process | |
| CN204757541U (en) | Single cryogenic natural gas liquefaction device of cryogen that mixes | |
| CN101135506A (en) | Middle and small mixed working substance natural gas liquefaction cooling cycle system with injector | |
| CN202630582U (en) | Unicyclic mixed refrigerant four-stage throttling refrigeration system | |
| CN102645084B (en) | Method and device for preparing liquefied natural gas by using mixed refrigerant three-level refrigeration | |
| CN104880024B (en) | Natural gas liquefying system for double-expansion cooling process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20120912 |