CN101228405A - Natural gas liquefaction process for producing LNG - Google Patents
Natural gas liquefaction process for producing LNG Download PDFInfo
- Publication number
- CN101228405A CN101228405A CNA2006800268485A CN200680026848A CN101228405A CN 101228405 A CN101228405 A CN 101228405A CN A2006800268485 A CNA2006800268485 A CN A2006800268485A CN 200680026848 A CN200680026848 A CN 200680026848A CN 101228405 A CN101228405 A CN 101228405A
- Authority
- CN
- China
- Prior art keywords
- cooling
- flow
- expansion
- cooling agent
- heat transfer
- 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.)
- Granted
Links
Images
Abstract
Embodiments of this invention relate to a process for liquefaction of natural gas and other methane-rich gas streams, and more particularly to a process for producing liquefied natural gas (LNG). In a first step of the process, a first fraction of the feed gas is withdrawn, compressed to a pressure greater than or equal to 1500 psia, cooled and expanded to a lower pressure to cool the withdrawn first fraction. The remaining fraction of the feed stream is cooled by indirect heat exchange with the expanded first fraction in a first heat exchange process. In a second step a separate stream comprising flash vapor is compressed, cooled and expanded to a lower pressure providing another cold stream. This cold stream is used to cool the remaining feed gas stream in a second indirect heat exchange process. The expanded stream exiting from the second heat exchange process is used for supplemental cooling in the first indirect heat exchange step. The remaining feed gas is subsequently expanded to a lower pressure, thereby partially liquefying this feed gas stream. The liquefied fraction of this stream is withdrawn from the process as LNG having a temperature corresponding to the bubble point pressure.
Description
The cross reference of related application
[0001] the application has required the rights and interests of No. the 60/795th, 101, the U.S. Provisional Application of No. the 60/706th, 798, U.S. Provisional Application proposing on August 9th, 2005 and proposition on April 26th, 2006.
Technical field
[0002] embodiments of the present invention relate to the liquifying method of natural gas and other methane rich gas streams, more specifically, relate to liquefied natural gas (liquefied natural gas, method LNG) of producing.
Background technology
[0003] natural gas is widely used in recent years because of the combustion quality and the convenience of its cleaning.Many gas sources are positioned at So Far Away, and are far apart from any commercial market of this gas.Sometimes, the pipeline natural gas transport that can be used for being produced is to the commercial market.When pipeline transportation was infeasible, the natural gas of being produced was processed to liquefied natural gas (it is called as " LNG ") usually and is used to be transported to market.
[0004] in the design of LNG factory, a most important Consideration is the method that natural gas feedstream is converted into LNG.At present, modal liquifying method uses the refrigeration system of certain form.Come liquefied natural gas although used many kind of refrigeration cycle, yet now LNG factory three types of the most normal use be: (1) " stepwise circulation ", it utilizes a plurality of one pack system cooling agents in heat exchanger, described cooling agent is reduced to condensing temperature by gradual layout with the temperature with gas; (2) " multiple group sub-refrigerating circulation ", it utilizes the multicomponent cooling agent in custom-designed heat exchanger; (3) " decompressor circulation (expander cycle) ", it makes gas be expanded to low pressure from raw gas pressure, the corresponding reduction of temperature.The change type or the combination of recycling these the three kinds of fundamental types of most of natural gas liquefactions.
[0005] in the multiple group sub-refrigerating circulation, used cooling agent can be the mixture of component such as methane, ethane, propane, butane and nitrogen.In " stepwise circulation ", cooling agent also can be a pure material, as propane, ethene or nitrogen.These cooling agents that need a large amount of compositions to be controlled by precision.In addition, these cooling agents may must be introduced into and store, and force with the logistics requirement.Some components that typically can prepare alternatively, cooling agent by the distillating method that combines with liquifying method.
[0006] utilize gas expander, for unstripped gas provides cooling, thus the logistical problem that elimination or reduction cooling agent are handled, this has caused process engineer's interest.The principle of expander system operation is: unstripped gas can expand by expansion turbine, thereby operates and reduce the temperature of gas.Cryogenic gas then with the unstripped gas heat exchange, so that required refrigeration to be provided.Usually need add refrigeration, with abundant liquefaction unstripped gas, and this can provide by coolant system.Because the power of expansion gained is generally used for supplying the main compression horsepower of employed part in the kind of refrigeration cycle.The typical decompressor of preparation LNG circulates in raw gas pressure under and to operate, typically about 6, under the 895kPa (1,000 pound/square inch).
[0007] yet, the circulation of the decompressor that proposes previously is all than the thermodynamic efficiency based on the natural gas liquefaction circulation of coolant system is low at present.Therefore up to now, the decompressor circulation does not provide the advantage on any installation cost, and comprises that the liquefaction cycle of cooling agent is still the preferred selection of natural gas liquefaction.
[0008] because the decompressor circulation produces the high circulating current flow velocity and the height inefficiency in precooling (warm) stage, gas expander typically is used to further cool off unstripped gas, and this unstripped gas has for example utilized external coolant to be chilled in advance far away from the temperature below-20 ℃ in closed circulation.Therefore, a common factor is to need second external refrigeration cycle in the decompressors circulation that proposes most of, so as before gas to enter decompressor this gas of precooling.The external refrigeration cycle of this combination and decompressor circulation are called as " mixing circulation " sometimes.Although this precooling based on cooling agent has been eliminated inefficient main source on decompressor is used, yet it has significantly reduced the advantage of decompressor circulation, this advantage has been removed external coolant exactly.Extra cooling also may be essential after the decompressor cooling, and can provide by another external coolant system, as nitrogen or cold freezing mixture.
[0009] therefore, circulating still to following decompressor, existence needs: compare with the technology of present application at least, this decompressor circulation has been eliminated the demand of external coolant and has been had the efficient of raising.
Summary of the invention
[0010] embodiments of the present invention provide the method for liquefied natural gas and other methane rich gas streams, to produce the methane-rich gas of liquefied natural gas (LNG) and/or other liquefaction.As comprising that at this specification term natural gas used in the appended claims is meant the gas raw material that is suitable for making LNG.Described natural gas can comprise gas (association natural gas) that derives from crude oil well or the gas (nonassociated gas) that derives from gas well.The composition of natural gas can marked change.As used herein, natural gas is to contain methane (C
1) as the high methane gas of key component.
[0011] produce in one or more embodiments of LNG method at this paper, implement first step, wherein first's unstripped gas is extracted, compresses, cools off and be expanded to the first that lower pressure is extracted with cooling.The remainder of feed stream is cooled by carrying out indirect heat exchange with the first of expanding in first heat transfer process.In second step, it comprises cooling circuit (sub-cooling loop) again, and the independent stream that comprises flash-off steam (flash vapor) is compressed, cools off and be expanded to lower pressure, so that another cool stream to be provided.This cool stream is used in the remaining flow of feed gas of second indirect heat exchange process cooling, and this second indirect heat exchange process constitutes cooling heat transferring process again.The expansion flow that comes out from second heat transfer process is used for replenishing cooling in the first indirect heat exchange step.Remaining unstripped gas is expanded to more low-pressure subsequently, thus this flow of feed gas of partial liquefaction.The liquefaction part of this stream is retracted from technology as LNG, and the temperature of this LNG is corresponding to bubble point pressure.The vapor portion of this stream is returned, so that the cooling that is provided in the indirect heat exchange step to be provided.Refrigerating gas from the heating in various sources is compressed and recycles.
[0012] in one or more other embodiments according to the present invention, the liquifying method of methane rich gas streams is provided, described method comprises: provide methane rich gas streams under the pressure below 1,000 pound/square inch; Under the pressure below 1,000 pound/square inch, provide cooling agent; Compress described cooling agent to more than or equal to 1500 pounds/square inch pressure, so that compresses refrigerant to be provided; Cool off described compresses refrigerant by carrying out indirect heat exchange with cooling fluid; Described compresses refrigerant is expanded with the described compresses refrigerant of further cooling, thereby produce cooling agent that expand, cooling; Make cooling agent described expansion, cooling pass through heat transfer zone; And make described air-flow through described heat transfer zone, so that be cooled to the described air-flow of small part, thereby form cooled gas flow by cooling cooling agent indirect heat exchange with described expansion.In one or more other specific embodiment, a part that provides cooling agent to comprise extracting gases under the pressure below 1,000 pound/square inch is as cooling agent.In other embodiments, this part air-flow that is used as cooling agent is extracted from air-flow through before heat transfer zone at this air-flow.Still in other embodiments, the method according to this invention further comprises, utilizes the loop of the flash-off steam filling that is produced in the process with the liquefaction methane rich gas streams, for heat transfer zone provides to the small part refrigerating function.According to other embodiment of the present invention will be conspicuous for those of ordinary skills.
The accompanying drawing summary
[0013] Fig. 1 is according to the described schematic flow diagram that is used to produce the embodiment of LNG of the inventive method.
[0014] Fig. 2 is the schematic flow diagram that is used to produce second embodiment of LNG, and it is similar to
Technology shown in Figure 1, just the gaseous coolant in compression, cooling and expansion circuit separates with unstripped gas, and therefore can have the composition different with unstripped gas.
[0015] Fig. 3 is that it has utilized a plurality of work expansion step, is used to raise the efficiency according to the described schematic flow diagram that is used to produce the 3rd embodiment of LNG of the inventive method.
[0016] Fig. 4 is according to the described schematic flow diagram that is used to produce the 4th embodiment of LNG of the inventive method, it has utilized the work expansion step of a plurality of Fig. 3 of being similar to, but the extra expansion step and the compression of unstripped gas have also been incorporated into, to improve the performance of expansion step.
[0017] Fig. 5 is that it is similar to embodiment shown in Figure 4, but has utilized the expansion of extra effluent and process gas according to the described schematic flow diagram that is used to produce the 5th embodiment of LNG of the inventive method, so that cooling again to be provided.
[0018] Fig. 6 is another embodiment that is similar to the embodiment shown in Fig. 1 and Fig. 2, and wherein the cooling agent of cooling circuit had been cooled in the cooling heat exchanger before expanding again again.
[0019] Fig. 7 is another embodiment, and wherein said cooling circuit again is connected with unstripped gas.
[0020] Fig. 8 is another embodiment, has shown the optional layout of cooling circuit again.
[0021] Fig. 9 is the embodiment that is similar to Fig. 8, but has been to use the separation expansion flow through aftercooler, and wherein expansion valve, Joules-Thompson valve or similar bloating plant are used for improving the efficient of aftercooler.
[0022] Figure 10 is another embodiment, and wherein nitrogen removal stage is merged in the situation that wherein may need denitrogenation.
[0023] Figure 11 is another embodiment, and wherein therefore the coolant source of cooling circuit and is rich in nitrogen from the beginning from the flash-off steam of denitrogenation unit again.
Detailed Description Of The Invention
[0024] embodiment of the present invention provides natural gas liquefaction, and it mainly utilizes gas expander and has eliminated demand to external coolant.That is, in embodiments more disclosed herein, unstripped gas itself (for example, natural gas) is used as the cooling agent in all kind of refrigeration cycle.This class kind of refrigeration cycle does not need to utilize external coolant (promptly, except that the cooling agent of unstripped gas itself or in LNG processing factory or near cooling agent the gas of manufacturing) additional cooling, as needed in the common gas expander circulation that is proposed, yet these kind of refrigeration cycle have higher efficient.In one or more embodiments, cooling water or cooling air are unique cooling fluid external sources, and after being used to compressor interstage or cooling.
[0025] Fig. 1 illustrates an embodiment of the invention, has wherein used decompressor loop 5 (be decompressor circulation) and cooling circuit 6 again.For the purpose of clear, decompressor loop 5 and again cooling circuit 6 show with the line of widening among Fig. 1.In this specification and appended claim, term " loop " and " circulation " are exchanged use.In Fig. 1, flow of feed gas 10 is about below 1200 pounds/square inch or about below 1100 pounds/square inch or about below 1000 pounds/square inch or about below 900 pounds/square inch or about below 800 pounds/square inch or enter liquefaction process below 700 pounds/square inch or under about pressure below 600 pounds/square inch approximately.Typically, the pressure of flow of feed gas 10 will be about 800 pounds/square inch.Flow of feed gas 10 generally comprises utilizes method and apparatus well known in the art to handle to remove the natural gas of pollutant.Before its process heat exchanger, part flow of feed gas 10 is extracted and forms effluent 11, therefore the cooling agent that is in corresponding under the pressure of flow of feed gas 10 pressure is provided, be that above-mentioned any pressure comprises about pressure below 1000 pounds/square inch, according to following discussion, this will be conspicuous.Therefore, in embodiment shown in Figure 1, the part of flow of feed gas is used as the cooling agent in decompressor loop 5.Although the embodiment that is shown among Fig. 1 has utilized at the effluent of flow of feed gas 10 through extracting from this flow of feed gas 10 before the heat exchanger, yet the unstripped gas effluent that is used as the cooling agent in the decompressor loop 5 can extract from unstripped gas through after the heat transfer zone at this unstripped gas.Therefore, in one or more embodiments, this method is any in other embodiment as herein described, and the flow of feed gas part that wherein is used as cooling agent is extracted, expands and return heat transfer zone from heat transfer zone, so that provide to the small part refrigerating function for heat transfer zone.
[0026] effluent 11 is passed to compression unit 20, and at this, it is compressed into more than or equal to about 1500 pounds/square inch pressure, thereby the cooling agent stream 12 of compression is provided.Alternatively, effluent 11 is compressed into more than or equal to about 1600 pounds/square inch or more than or equal to about 1700 pounds/square inch or more than or equal to about 1800 pounds/square inch or more than or equal to about 1900 pounds/square inch or more than or equal to about 2000 pounds/square inch or more than or equal to about 2500 pounds/square inch or more than or equal to about 3000 pounds/square inch pressure, thereby the cooling agent stream 12 of compression is provided.Used as comprising in this manual in the claims, term " compression unit " is meant the compression device that is known in the art any type that is used for pressurized contents or mixture of substances or the combination of similar or dissimilar compression devices, and can comprise auxiliary equipment." compression unit " can adopt one or more compression stages.Exemplary compressor can include, but are not limited to the positive displacement type, as reciprocating type and rotary compressor, and power type, as centrifugal and Axial Flow Compressor.
[0027] leave after the compression unit 20, the cooling agent of compression stream 12 is passed to cooler 30, is cooled by carrying out indirect heat exchange with suitable cooling fluid this its, and the cooling refrigerant (cooling agent) of compression is provided.In one or more embodiments, cooler 30 belongs to provides water or the air type as cooling fluid, although can use the cooler of any kind.When compressed coolant stream 12 when cooler 30 comes out, its temperature depends on environmental condition and employed cooling medium, and typically is about 35 to about 105 .Then, the compressed coolant stream 12 of cooling is passed to decompressor 40, expands this its and therefore is cooled and forms the cooling agent stream 13 of expansion.In one or more embodiments, decompressor 40 is merit bloating plant (work-expansion device), for example produces the decompressor of the merit that can be removed and be used to compress.
[0028] expansion cooling agent stream 13 is passed to heat transfer zone 50, for heat transfer zone 50 provides to the small part refrigerating function.Used as comprising in the appended claim at this specification, term " heat transfer zone " is meant the equipment of the arbitrary type that becomes known for promoting heat exchange in this area or the combination of similar or dissimilar equipment.Therefore, " heat transfer zone " can be contained in the single-chip device, and perhaps it can comprise the zone that is included in a plurality of equipment sheets.On the contrary, a plurality of heat transfer zone can be included in the single-chip device.
[0029] leave after the heat transfer zone 50, the cooling agent of expansion stream 13 is sent to compression unit 60 and pressurizes to form stream 14, and it converges with effluent 11 then.It is evident that in case decompressor loop 5 has been full of the unstripped gas from effluent 11, then only need to replenish unstripped gas to replace the loss that causes because of leakage, the most of gas that enters compressor unit 20 is provided by stream 14 usually.The part of the flow of feed gas 10 that extracts as effluent 11 is not passed to heat transfer zone 50, and at this, it is cooled off to small part by carrying out indirect heat exchange with expansion cooling agent stream 13.Leave after the heat transfer zone 50, flow of feed gas 10 is passed to heat transfer zone 55.The basic function of heat transfer zone 55 is to cool off flow of feed gas again.Therefore, in heat transfer zone 55, flow of feed gas 10 is by cooling circuit 6 quilts cooling (as described below) more again, to produce cool stream 10a again.Cool stream 10a is expanded to lower pressure then in decompressor 70 again, thereby partial liquefaction cool stream 10a again forms liquid part and remaining vapor portion.Decompressor 70 can be any pressure regulating equipment, includes but not limited to valve, control valve, Joule Thompson valve, Venturi tube equipment, liquid expander, hydraulic turbine etc.The 10a of cool stream again of partial liquefaction is passed to surge tank 80, and at this, liquefaction part 15 is retracted from this technology as LNG, and the temperature that this LNG has is corresponding to bubble point pressure.Remaining vapor portion (flash-off steam) stream 16 is used as fuel to be provided power for compressor unit and/or is used as cooling agent in the cooling circuit 6 again, as described below.Before being used as fuel, all or part flash-off steam stream 16 can randomly be passed to heat transfer zone 50 and 55 from surge tank 80, so that the cooling that is provided in these heat transfer zone to be provided.
[0030] with reference to figure 1, part flash-off steam 16 is extracted through pipeline 17, to fill cooling circuit 6 again.Therefore, the partial raw gas from flow of feed gas 10 is extracted (with the form from the flashed vapour of flash vapor stream 16) as the cooling agent in the cooling circuit 6 again.It is evident that equally,, only need to replenish the gas other flash-off steam of pipeline 17 (promptly from), to replace the loss that causes because of leakage in case cooling circuit 6 is full of flashed vapour fully again.In cooling circuit 6 again, expansion flow 18 is discharged from decompressor 41, and is inhaled into by heat transfer zone 55 and 50.Flash-off steam stream 18 (Leng Que the cryogen flow again) that expand are back to compression unit 90 then, and at this, it is compressed to higher pressure and heats up.Leave after the compression unit 90, the cooling agent of cooling again of recompression stream is cooled in cooler 31, and this cooler can have the type identical with cooler 30, although can use the cooler of any kind.After the cooling, the cooling agent of the cooling again stream of recompression is passed to heat transfer zone 50, and at this, it is by with expansion cooling agent stream 13, cool off cooling agent stream 18 and randomly carry out indirect heat exchange with flash-off steam stream 16 and be further cooled again.Leave after the heat transfer zone 50, flow through overexpansion machine 41 of the cooling agent of cooling again of recompression and cooling expands, and so that cool stream to be provided, it cools off flow of feed gas then again through heat transfer zone 55 part produces LNG so that finally expand.The expansion of leaving heat transfer zone 55 is cooled off cooling agent stream again and is passed through heat transfer zone 50 once more, adds cooling so that provided before recompressing.By this way, the circulation in the cooling circuit 6 is constantly repeated again.Therefore, in one or more embodiments, this method is any in this disclosed other embodiment, described other embodiment further comprises and utilizes the loop be filled with the flash-off steam (for example, flash-off steam 16) that is produced by LNG production (for example cooling circuit 6) again that cooling is provided.
[0031] it is evident that, in the graphic embodiment of Fig. 1 (and in other embodiment as herein described), when flow of feed gas 10 when a heat transfer zone is passed to another heat transfer zone, the temperature of flow of feed gas 10 will be lowered, up to final generation cool stream again.In addition, when effluent extracts from flow of feed gas 10, the mass flow of flow of feed gas 10 will be lowered.Also can carry out other modification, for example compression to flow of feed gas 10.Although can be considered to produce new and homogeneous turbulence not to every kind of this type of modification of flow of feed gas 10, but for clear and be easy to set forth for the purpose of, unless otherwise indicated, flow of feed gas will be called as flow of feed gas 10, and its understanding is through heat transfer zone, takes away the change that effluent and other change will make flow of feed gas 10 produce temperature, pressure and/or flow velocitys.
[0032] Fig. 2 illustrates another embodiment of the invention, and it is similar to the embodiment shown in Fig. 1, and just decompressor loop 5 has been replaced by decompressor loop 7.Other term among Fig. 2 is described in the above.For the purpose of clear, decompressor loop 7 shows to widen line in Fig. 2.7 utilizations of decompressor loop and decompressor loop 5 essentially identical equipment (for example, compressor 20, cooler 30 and decompressor 40, all these are described in the above).Yet the gaseous coolant in the decompressor loop 7 separates with unstripped gas, and therefore can have the composition different with unstripped gas.That is, decompressor loop 7 is loop substantially, and is not connected with flow of feed gas 10.Therefore the cooling agent in decompressor loop 7 needs not to be unstripped gas, although it can be.Decompressor loop 7 can be charged into any suitable coolant gas, this coolant gas in utilizing the LNG processing factory in decompressor loop 7 or near production.For example, the coolant gas that is used to charge into decompressor loop 7 can be a unstripped gas, as natural gas, its only by section processes to remove pollutant.
[0033] as decompressor loop 5, decompressor loop 7 is gases at high pressure loops.Stream 12a is with more than or equal to about 1500 pounds/square inch or more than or equal to about 1600 pounds/square inch or more than or equal to about 1700 pounds/square inch or more than or equal to about 1800 pounds/square inch or more than or equal to about 1900 pounds/square inch or more than or equal to about 2000 pounds/square inch or more than or equal to about 2500 pounds/square inch or more than or equal to leaving compression unit 20 under about 3000 pounds/square inch pressure.When compressed coolant stream 12a when cooler 30 occurs, its temperature depends on environmental condition and used cooling medium, and typically is about 35 to about 105 .The compressed coolant stream 12a of cooling is passed to decompressor 40 then, and at this, it expands and further cooling, forms expansion cooling agent stream 13a.Expansion cooling agent stream 13a is passed to heat transfer zone 50, so that for heat transfer zone 50 provides to the small part refrigerating function, in this heat transfer zone, flow of feed gas 10 is by carrying out indirect heat exchange with expansion cooling agent stream 13a and being cooled off to small part.After leaving heat transfer zone 50, expansion cooling agent stream 13a is back to compression unit 20, recompresses.In any embodiment as herein described, decompressor loop 5 and 7 can exchange use.For example, in the embodiment that utilizes decompressor loop 5, decompressor loop 7 can replace decompressor loop 5.
[0034] Fig. 3 has shown another embodiment of producing LNG according to the inventive method.Among Fig. 3 graphic technology utilization a plurality of merit expansion cycles (work expansion cycle), add cooling for unstripped gas and other streams provide.The application of these merit expansion cycles causes the gross efficiency of liquefaction process to be improved.With reference to figure 3, flow of feed gas 10 enters liquefaction process once more under above-mentioned pressure.In the specific embodiment shown in Figure 3, effluent 11 is sent to decompressor loop 5 in foregoing mode, but it is evident that, sealing decompressor loop 7 can be used for replacing decompressor loop 5, and in such cases, effluent 11 is with optional.Decompressor loop 5 with as above the described identical mode of the embodiment shown in Fig. 1 is operated, the cooling agent that just expands stream 13, will be described in detail for heat transfer zone 56 provides to the small part refrigerating function below through heat transfer zone 56.
[0035] the part material air-flow 10 that is not extracted as effluent 11 is passed to heat transfer zone 56, and at this, it connects heat exchange in the ranks and be cooled by flowing to expansion cooling agent stream 13 and described below other at least in part.After leaving heat transfer zone 56, flow of feed gas 10 is further cooled by connecing heat exchange in the ranks with other flowing to described below this its through heat transfer zone 57 and 58.In the present embodiment, the following first and second merit expansion cycles of utilizing are to raise the efficiency: before flow of feed gas 10 enters heat transfer zone 57, effluent 11b is derived from flow of feed gas 10.After flow of feed gas 10 is left heat transfer zone 57 and before it enters heat transfer zone 58, effluent 11c is derived from flow of feed gas 10.Therefore, effluent 11b and 11c draw from flow of feed gas 10 in the different phase of flow of feed gas cooling.That is, the difference place of each effluent on the unstripped gas cooling curve withdraws from from flow of feed gas, makes that the initial temperature of the effluent that each is withdrawn from succession is lower than the effluent of before having withdrawn from.
[0036] effluent 11b is the part of the first merit expansion cycles, and it is passed to decompressor 42, expands this its and also therefore cools off and formation expansion flow 13b.Expansion flow 13b is through heat transfer zone 56 and 57, for heat transfer zone 56 and 57 provides to the small part refrigerating function.Similarly, effluent 11c is the part of the second merit expansion cycles, and it is passed to decompressor 43, expands this its and also therefore cools off and formation expansion flow 13c.Expansion flow 13c passes through heat transfer zone 56,57 and 58 then, for heat transfer zone 56,57 and 58 provides to the small part refrigerating function.Therefore, flow of feed gas 10 also is cooled by carrying out indirect heat exchange with expansion flow 13b and 13c in heat transfer zone 56 and 57.In heat transfer zone 58, flow of feed gas 10 also is cooled by carrying out other indirect heat exchange with expansion flow 13c.
[0037] leave after the heat transfer zone 56, expansion flow 13b and 13c are passed to compression unit 61 and 62 respectively, and they are recompressed and flow 14a in conjunction with forming at this.Stream 14a with flow of feed gas 10 recombinations before by cooler 32 cooling.Cooler 32 can be cooler or the cooler type with cooler 30 and 31 same types.Decompressor 42 and 43 is merit bloating plant types well known to those skilled in the art.Exemplary, the non-limiting example of suitable merit bloating plant comprise liquid expander and hydraulic turbine.Therefore, in embodiment shown in Figure 3, flow of feed gas is further cooled by a plurality of merit bloating plants.It will be apparent for a person skilled in the art that extra merit expansion cycles to be added in the graphic embodiment of Fig. 3 institute, perhaps can adopt single merit expansion cycles.Therefore, generally speaking, can adopt one or more merit bloating plants in the above described manner.Each merit bloating plant dilation flow of feed gas, thereby and cool off this part, each part of the described flow of feed gas part that wherein expands in the merit bloating plant is withdrawn from from flow of feed gas in the different phase (that is, under different flow of feed gas temperature) of flow of feed gas cooling.
[0038] in one or more other embodiments according to the present invention, utilizes the merit bloating plant as follows: from flow of feed gas, extract one or more effluents out; Make described one or more effluent be passed to one or more merit bloating plants; The described one or more effluent that expands expanding and cooling this one or more effluents, thereby forms effluent one or more expansions, that cool off; With described one or more expansions, cold side stream is passed at least one heat transfer zone; Make described air-flow through described at least one heat transfer zone; And by with described one or more expansions, cold side flows to and connects heat exchange in the ranks, cools off described air-flow to small part.
[0039] refer again to Fig. 3, flow of feed gas 10 is passed to heat transfer zone 59 after being cooled then in heat transfer zone 56,57 and 58, be further cooled this its, produces cool stream 10a again.The major function of heat transfer zone 59 is to cool off flow of feed gas 10 again.Cool stream 10a is expanded to lower pressure then in decompressor 85 again, thereby partial liquefaction cool stream 10a again forms liquefaction part and remaining vapor portion.Decompressor 85 can be any pressure regulating equipment, includes but not limited to valve, control valve, Joule Thompson valve, Venturi tube equipment, liquid expander, hydraulic turbine etc.The 10a of cool stream again of partial liquefaction is passed to surge tank 80, and at this, liquefaction part 15 is retracted from this technology as LNG, and the temperature that this LNG has is corresponding to bubble point pressure.Remaining vapor portion (flash-off steam) stream 16 is used as fuel, for compressor unit provides power, and/or with the front cooling is again gone the same way 6 described essentially identical modes as the cooling agent in the cooling circuit 8 again.As from table 3 as seen, cooling circuit 8 is similar to cooling circuit 6 again again, just again cooling circuit 8 to four heat transfer zone ( heat transfer zone 56,57,58 and 59) supply cooling.
[0040] Fig. 4 illustrates another embodiment of the present invention.Embodiment shown in embodiment shown in Fig. 4 and Fig. 3 is basic identical, has just added compression unit 25 and decompressor 35.Decompressor 35 can be the liquid expander or the hydraulic turbine of any kind.Decompressor 35 is placed between heat transfer zone 58 and 59, makes flow of feed gas 10 flow into the decompressor 35 from heat transfer zone 58, thereby expands and cooling this its, produces the flow of feed gas 10b that expands.Stream 10b is passed to heat transfer zone 59 then, is cooled off this its again and produces cool stream 10c again.By expanding in decompressor 35 and therefore cooling off flow of feed gas 10, to produce stream 10b, the total cooling load on the cooling circuit 8 is advantageously reduced again.Therefore, in one or more embodiments, this method is any of other embodiments described herein, and described other embodiments further comprise and are expanded to the described cooling flow of feed gas of small part, to produce flow of feed gas cooling, that expand (for example, stream 10b); With by carrying out indirect heat exchange the flow of feed gas further described cooling of cooling, that expand with loop (for example, cooling circuit 6 or 8) again, described loop is filled the flash-off steam (for example, flash-off steam 16) that obtains with from LNG production.
[0041] continue with reference to figure 4, compression unit 25 is used to increase the pressure of flow of feed gas 10 before entering liquefaction process.Therefore, flow of feed gas 10 is passed to compression unit 25, is compressed into the pressure that is higher than more than the unstripped gas supply pressure this its, perhaps, in one or more other embodiments, is compressed into about pressure more than 1200 pounds/square inch.Alternatively, flow of feed gas 10 is compressed into more than or equal to about 1300 pounds/square inch or more than or equal to about 1400 pounds/square inch or more than or equal to about 1500 pounds/square inch or more than or equal to about 1600 pounds/square inch or more than or equal to about 1700 pounds/square inch or more than or equal to about 1800 pounds/square inch or more than or equal to about 1900 pounds/square inch or more than or equal to about 2000 pounds/square inch or more than or equal to about 2500 pounds/square inch or more than or equal to about 3000 pounds/square inch pressure.After the compression, flow of feed gas 10 is passed to cooler 33, is cooled before being passed to heat transfer zone 56 this its.Should be appreciated that at compression unit 25 to be used for flow of feed gas 10 (and so effluent 11) is compressed under the situation of the pressure lower than the pressure of compressed coolant stream 12 expectations that compression unit 20 can be used for increasing this pressure.
[0042] compression of aforesaid flow of feed gas 10 provides three kinds of benefits.At first, by increasing the pressure of flow of feed gas, the pressure of effluent 11b and 11c also is increased, and the result is, merit bloating plant 42 and 43 cooling performance are enhanced.The second, the heat transfer coefficient in the heat transfer zone improves.Therefore, in one or more embodiments, LNG production method as herein described is implemented according to other embodiments arbitrarily as herein described, and wherein unstripped gas was compressed into above-mentioned pressure before entering heat transfer zone.Still in other embodiments, this method comprises from a plurality of merit bloating plants adds cooling for flow of feed gas provides, therefore each merit bloating plant dilation flow of feed gas also cools off this part, form the effluent of one or more expansion coolings, wherein the described part material air-flow of each that expands in the merit bloating plant is drawn out of from flow of feed gas in the different phase (that is, under different flow of feed gas temperature) of flow of feed gas cooling; And carry out indirect heat exchange by effluent and cool off described flow of feed gas with described one or more expansion coolings.
[0043] still in other embodiments, each above-mentioned partial raw gas has about more than 1200 pounds/square inch before expansion, or more than or equal to about 1300 pounds/square inch, or more than or equal to about 1400 pounds/square inch, or more than or equal to about 1500 pounds/square inch, or more than or equal to about 1600 pounds/square inch, or more than or equal to about 1700 pounds/square inch, or more than or equal to about 1800 pounds/square inch, or more than or equal to about 1900 pounds/square inch, or more than or equal to about 2000 pounds/square inch, or more than or equal to about 2500 pounds/square inch, or more than or equal to about 3000 pounds/square inch pressure.Still in other embodiments, this method is arbitrarily other embodiments described herein, and described other embodiments further comprise flow of feed gas is compressed to above-mentioned any pressure, to produce the flow of feed gas of pressurization; Described pressurization flow of feed gas is delivered to the merit bloating plant, perhaps deliver to a plurality of merit bloating plants; By described merit bloating plant or by a plurality of merit bloating plants the flow of feed gas of described compression is expanded, add cooling for flow of feed gas provides.
[0044] by compressing the 3rd benefit that flow of feed gas obtains as mentioned above be, the cooling capacity of decompressor 35 is improved, and the result is that decompressor 35 can even further reduce the cooling load on the cooling circuit 8 again.Should recognize, compression unit 25 and/or decompressor 35 also can advantageously be added into other embodiments described herein, so that on the cooling circuit again that these embodiments utilized, provide similar cooling load to reduce, other of perhaps cooling aspect improve, and compression unit 25 and decompressor 35 can be independently of one another with in any embodiments herein.In addition, not it is to be further appreciated that even and need compress feed stream that the cooling capacity of decompressor 35 (or merit bloating plant 42 and 43) will be improved to the degree that feed stream is supplied under the pressure that is higher than the LNG bubble point pressure.For example, if unstripped gas is supplied under any above-mentioned pressure that is produced by the unstripped gas compression, the benefit of this kind pressure will obviously can get, and need not extra compression.Therefore, when the school bag of explaining is drawn together claims, utilize the about stream more than 1200 pounds/square inch of the merit bloating plant and/or decompressor 35 bulbs of pressure should not be interpreted as needing to use compression unit 25 or any other compressor or compression step, perhaps need compression unit 25 or any other compressor or compression step to exist.
[0045] Fig. 5 is the schematic flow diagram that is used to produce the 5th embodiment of LNG according to the inventive method, and it is similar to the embodiment shown in Fig. 4, but has utilized another expansion step that cooling again is provided.With reference to figure 5, can see that cooling circuit 8 is not present in the embodiment shown in Figure 5 again.On the contrary, effluent 11d draws and is passed to bloating plant 105 from flowing 10b, expands this its and also therefore cools off and formation expansion flow 13d.Bloating plant 105 is (work-producing) decompressors that produce merit, and its a lot of types are easy to obtain.Exemplary, the non-limiting example of this kind equipment comprise liquid expander and hydraulic turbine.Expansion flow 13d is through heat transfer zone 59,58,57 and 56, for these heat transfer zone provide to the small part refrigerating function.As can be seen from Fig. 5, flow 10b and also can be cooled by carrying out indirect heat exchange with expansion flow 13d and flash-off steam stream 16.Therefore, in one or more embodiments, the inventive method (for example further is included in before the last heat exchange steps, before heat transfer zone 59), in decompressor 35, be expanded to small part cooling blast (flow of feed gas 10), to produce the cooling blast (for example, stream 10b) that expands; The part of the cooling blast of described expansion is passed to the decompressor that produces merit; The cooling blast of the further described expansion of expanding in the decompressor of described production merit; And the stream that will produce from the decompressor of described generation merit (for example, stream 13d) is passed to heat transfer zone, with by the further cooling blast of the described expansion of cooling of the indirect heat exchange that carries out in described heat transfer zone.
[0046] leave heat transfer zone 56 after, expansion flow 13d is passed to compression unit 95, is recompressed this its and combines with the stream that produces from compression unit 61 and 62, forms the part of stream 14a, it is cooled as previously mentioned and then is circulated to feed stream 10.
[0047] the further embodiment shown in Fig. 6 is similar to Fig. 1 and above-mentioned embodiment, just cooling circuit 6 has been modified again, make that after the cooling agent stream of recompression and cooling leaves heat transfer zone 50 it was further cooled in heat transfer zone 55 before expanding through decompressor 41.This embodiment is favourable, has wherein used cooling fluid, and there is not a lot of condensation processes in it after decompressor 41.
[0048] Fig. 7 has described another embodiment, and wherein cooling circuit 6a has utilized a part of unstripped gas 10 again.This part of unstripped gas 10 from 201 is pressurizeed in compressor 25 again and is cooled at cooler 33, according to Fig. 4 in identical mode.
[0049] Fig. 8 is another embodiment that is similar to Fig. 7, has shown the optional layout of cooling circuit 6 again.The composition that depends on unstripped gas 10 can use other compressor (not shown) to prevent in cooling circuit again condensation or guarantees suitable line pressure.
[0050] embodiment that Fig. 9 has described with certain unstripped gas 10 is formed and/or pressure is used in combination.Be used for the cooling curve of the unstripped gas 10 that LNG collects in order to make better to be cooled, with the cooling curve coupling of the partial raw gas 10 that is used for cooling off in cooling heat transferring district 55 again, may be essential be the separating part of the coolant gas that enters again cooling circuit 6 of further expanding.This is to use expansion valve 82 or other decompressors (for example, the Joules-Thompson valve) are realized, adds cooling so that provide in cooling circuit 6 again.
[0051] Figure 10 represents another embodiment, and it has shown for the situation that needs denitrogenation, based on the composition of unstripped gas 10, utilizes distillation column 81 or other equivalent apparatus to incorporate nitrogen removal stage into.This may be essential, to satisfy the nitrogen specification be used for carrying with the product LNG of final use.
[0052] Figure 11 represents another embodiment, has shown incorporating into of denitrogenation unit, wherein is used as the cooling agent of cooling circuit from the flash-off steam of denitrogenation unit again.Therefore the cooling agent of gained is rich in nitrogen.
Embodiment
[0053] quality of supposing and energy balance to illustrate the embodiment shown in Fig. 4, the results are shown in the following table.Data are to utilize the commercial HYSYS by name that can get
TMThe process simulator of (deriving from the Hyprotech Ltd. of Canadian Calgary) obtains; Yet the process simulator that can use other commerce to get comes development data, comprises for example HYSIM
TM, PROII
TMWith ASPEN PLUS
TM, those skilled in the art are familiar with these programs.This embodiment supposes that flow of feed gas 10 has following composition in mole percent: C
1: 90.25%; C
2: 5.70%:C
3: 0.01%; N
2: 4.0%; He:0.04%.Provided the data that are presented in the table, so that provide better understanding to the embodiment shown in Fig. 4, but the present invention is not interpreted as unnecessarily being limited to this.In view of the teachings contained herein, temperature, pressure and flow velocity can have a lot of changes.The actual temp, pressure and the flow velocity that calculate at state point 201 to 214 (position shown in Fig. 4) are set forth in the table.
[0054] in an embodiment of the inventive method, the temperature of the stream that comes out from last heat transfer zone by control, the volume of flash-off steam stream 16 is controlled, with the demanded fuel of coupling compression unit and other equipment.For example, with reference to figure 4, the temperature at state point 207 places can be controlled, so that based on fuel requires to produce flash-off steam (stream 16) more or less.The higher temperature at state point 207 places will cause more flash-off steam (and so how available fuel) to produce, and vice versa.Alternatively, can adjust temperature, make the flash-off steam flow velocity be higher than demanded fuel, in this case, the surplus stream that surpasses the requirement of fuel stream can be recycled after compression and cooling.
Table
| State point | Temperature () | Pressure (pound/inch 2) | Flow velocity (lb-mol/hr) |
| 201 | 262 | 985 | 3.35×10 5 |
| 202 | 100 | 1500 | 1.08×10 6 |
| 203 | -36 | 1480 | 4.85×10 5 |
| 204 | -130 | 1470 | 3.35×10 5 |
| 205 | -213 | 1460 | 3.35×10 5 |
| 206 | -229 | 48 | 3.35×10 5 |
| 207 | -236 | 42 | 3.35×10 5 |
| 208 | -254 | 18 | 3.35×10 5 |
| 209 | -217 | 71 | 3.12×10 5 |
| 210 | -140 | 420 | 2.29×10 4 |
| 211 | 100 | 126 | 2.57×10 4 |
| 212 | -240 | 44 | 2.57×10 4 |
| 213 | 100 | 3000 | 8.57×10 5 |
| 214 | -40 | 895 | 8.57×10 5 |
[0055] those skilled in the art particularly obtain technical staff that this paper instructs benefit and will recognize a lot of modifications and changes to the above-mentioned specific embodiment.For example, show that in one embodiment feature may be added in other embodiments and forms other embodiment.Therefore, concrete disclosed embodiment and embodiment should not be used to restriction or limit scope of the present invention, and this scope is determined by appended claims.
Claims (22)
1. the liquifying method of methane rich gas streams, described method comprises:
Described air-flow is provided under the pressure below 1,000 pound/square inch;
Under the pressure below 1,000 pound/square inch, provide cooling agent;
Compress described cooling agent to more than or equal to 1500 pounds/square inch pressure, so that compresses refrigerant to be provided;
By with the cooling fluid indirect heat exchange, cool off the cooling agent of described compression;
The cooling agent of described compression is expanded,, thereby produce the cooling agent of the cooling of expanding with the cooling agent of the described compression of further cooling; With
The cooling agent of described expansion cooling is passed to heat transfer zone; With
Make described air-flow through described heat transfer zone, be cooled to the described air-flow of small part, thereby form cooling blast by cooling agent indirect heat exchange with described expansion cooling.
2. the described method of claim 1 wherein provides described cooling agent to comprise that extraction unit divides described air-flow as described cooling agent under the pressure below 1,000 pound/square inch.
3. the described method of claim 2, the described part of wherein said air-flow was drawn out of before described air-flow is passed to described heat transfer zone.
4. the described method of claim 2, the described part of wherein said air-flow is drawn out of from described heat transfer zone.
5. the described method of claim 1 also comprises and utilizes loop to provide to the small part refrigerating function for described heat transfer zone, and described loop is filled with the flash-off steam that produces in described methane rich gas streams liquifying method.
6. the described method of claim 5 also comprises:
Make to the described cooling blast expansion of small part, to produce the expansion cooled gas flow; With
By carrying out indirect heat exchange, further cool off described expansion cooled gas flow with the described loop that is filled with flash-off steam.
7. the described method of claim 1 also comprises:
Make to the described cooling blast expansion of small part, to produce the expansion cooled gas flow; With
By in one or more other heat transfer zone indirect heat exchange, further cool off described expansion cooled gas flow.
8. the described method of claim 1 also comprises:
Utilize a plurality of merit bloating plants to cool off described air-flow, the part of each the described flow of feed gas that expands in the described merit bloating plant, thereby and cool off described part, form the effluent of one or more expansion coolings, wherein the described part material air-flow of each that expands in described merit bloating plant is extracted out from described flow of feed gas in the different phase of flow of feed gas cooling; With
By with the effluent indirect heat exchange of described one or more expansions cooling, cool off described flow of feed gas.
9. the described method of claim 1 also comprises:
Extract a part or the described air-flow of many parts out:
Make a described part or each part in many parts of described air-flow be passed to one or more merit bloating plants, and the described part of the described air-flow that expands or each part in many parts, so that a described part or many parts expand and cooling, thereby form the effluent of one or more expansion coolings;
Make the flow measurement of described one or more expansion coolings be passed at least one heat transfer zone;
Make described air-flow through described at least one heat transfer zone; With
By with the effluent indirect heat exchange of described one or more expansions cooling, cool off described air-flow to small part.
10. claim 6,7,8 or 9 described methods, wherein said air-flow at first is compressed to the pressure that is higher than gas supply pressure.
11. the described method of claim 1 comprises that also described cooling blast is before the last heat exchange step and expand with the expansion stage before producing LNG.
12. the described method of claim 1 also comprises:
Before last heat exchange step, be expanded to the described cooling blast of small part, to produce the expansion cooled gas flow;
Make the part of described expansion cooled gas flow be passed to the decompressor that produces merit, and the described part of the described expansion cooled gas flow that in the decompressor of described generation merit, further expands; With
Make the stream that from the decompressor of described generation merit, occurs be passed to heat transfer zone, by further cooling off remaining described expansion cooled gas flow in the heat exchange of described heat transfer zone indirect.
13. the described method of claim 1, wherein said cooling agent are compressed into the pressure more than or equal to 3,000 pounds/square inch, so that compresses refrigerant to be provided.
14. the described method of claim 1, wherein said heat transfer zone comprises a plurality of heat-exchanging chambers.
15. the described method of claim 1 also comprises:
Cooling heat transferring district again, it receives described air-flow, and cools off by the expansion of second cooling agent, so that cooling blast again to be provided;
The last afterwards described cooling blast again of expansion also reclaims LNG.
16. the described method of claim 15, wherein said second cooling agent are the parts of described methane rich gas streams.
17. the described method of claim 15, wherein before described second cooling agent expanded, described second cooling agent was cooled off in described cooling heat transferring again district again.
18. the described method of claim 16, wherein said methane rich gas streams is being pressurizeed through before the described heat transfer zone again, described cooling blast is inflated, and the part of the cooling blast of described expansion is further expanded in described cooling heat transferring again district and is used as described second cooling agent.
19. the described method of claim 15, the part of wherein said cooling blast again are inflated and its part is described second cooling agent.
20. the described method of claim 19, the described part of wherein said cooling blast again are divided into two part streams, one of described part stream is further expanded, and described two part streams all comprise described second cooling agent.
21. the described method of claim 1 also comprises denitrogenation gas when reclaiming LNG.
22. the methane rich gas streams liquifying method, described method comprises:
Described air-flow is provided under the pressure below 1,000 pound/square inch;
Cooling agent is provided in loop;
Described cooling agent is compressed to pressure more than or equal to 1500 pounds/square inch, so that the cooling agent of compression to be provided;
By with the cooling fluid indirect heat exchange, cool off the cooling agent of described compression;
The cooling agent of described compression is expanded,, thereby produce the cooling agent of the cooling of expanding with the cooling agent of the described compression of further cooling;
The cooling agent of described expansion cooling is passed to heat transfer zone; With
Make described air-flow through described heat transfer zone, be cooled to the described air-flow of small part by cooling agent indirect heat exchange with described expansion cooling.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US70679805P | 2005-08-09 | 2005-08-09 | |
| US60/706,798 | 2005-08-09 | ||
| US79510106P | 2006-04-26 | 2006-04-26 | |
| US60/795,101 | 2006-04-26 | ||
| PCT/US2006/020121 WO2007021351A1 (en) | 2005-08-09 | 2006-05-24 | Natural gas liquefaction process for lng |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101228405A true CN101228405A (en) | 2008-07-23 |
| CN101228405B CN101228405B (en) | 2010-12-08 |
Family
ID=35658860
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2006800268485A Expired - Fee Related CN101228405B (en) | 2005-08-09 | 2006-05-24 | Natural gas liquefaction process for producing LNG |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101228405B (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102538390A (en) * | 2011-12-22 | 2012-07-04 | 西安交通大学 | Novel natural gas liquefaction system and natural gas liquefaction method |
| CN103175379A (en) * | 2013-03-18 | 2013-06-26 | 上海交通大学 | Device for preparing liquefied natural gas with pipeline pressure energy and application method thereof |
| CN103582792A (en) * | 2011-06-15 | 2014-02-12 | 盖斯康萨特有限公司 | Process for liquefaction of natural gas |
| CN104204698A (en) * | 2012-03-30 | 2014-12-10 | 埃克森美孚上游研究公司 | Lng formation |
| CN104315801A (en) * | 2014-10-15 | 2015-01-28 | 中国海洋石油总公司 | Mixed refrigerant-expansive refrigeration-circulated natural gas liquefying method |
| CN105074370A (en) * | 2012-12-28 | 2015-11-18 | 林德工艺装置股份有限公司 | Integrated process for NGL (natural gas liquids recovery) and LNG (liquefaction of natural gas) |
| CN105202366B (en) * | 2011-04-06 | 2017-07-21 | 巴布科克知识产权管理（第一）有限公司 | Cool down the method and the equipment for it of boil-off gas |
| CN107110599A (en) * | 2015-01-09 | 2017-08-29 | 三菱重工业株式会社 | Gas liquefaction equipment and gas liquefaction method |
| CN106091574B (en) * | 2016-06-02 | 2018-10-30 | 成都深冷液化设备股份有限公司 | Gas liquefaction device with compression heat recovery function and liquefaction method thereof |
| CN108759302A (en) * | 2018-06-04 | 2018-11-06 | 中海石油气电集团有限责任公司 | A kind of high-pressure natural gas liquefaction system and method |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4740223A (en) * | 1986-11-03 | 1988-04-26 | The Boc Group, Inc. | Gas liquefaction method and apparatus |
| US4846862A (en) * | 1988-09-06 | 1989-07-11 | Air Products And Chemicals, Inc. | Reliquefaction of boil-off from liquefied natural gas |
| MY122625A (en) * | 1999-12-17 | 2006-04-29 | Exxonmobil Upstream Res Co | Process for making pressurized liquefied natural gas from pressured natural gas using expansion cooling |
| FR2841330B1 (en) * | 2002-06-21 | 2005-01-28 | Inst Francais Du Petrole | LIQUEFACTION OF NATURAL GAS WITH RECYCLING OF NATURAL GAS |
| US6694774B1 (en) * | 2003-02-04 | 2004-02-24 | Praxair Technology, Inc. | Gas liquefaction method using natural gas and mixed gas refrigeration |
-
2006
- 2006-05-24 CN CN2006800268485A patent/CN101228405B/en not_active Expired - Fee Related
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105202366B (en) * | 2011-04-06 | 2017-07-21 | 巴布科克知识产权管理（第一）有限公司 | Cool down the method and the equipment for it of boil-off gas |
| CN103582792B (en) * | 2011-06-15 | 2016-06-22 | 盖斯康萨特有限公司 | Method for natural gas liquefaction |
| CN103582792A (en) * | 2011-06-15 | 2014-02-12 | 盖斯康萨特有限公司 | Process for liquefaction of natural gas |
| CN102538390B (en) * | 2011-12-22 | 2014-08-06 | 西安交通大学 | Novel natural gas liquefaction system and natural gas liquefaction method |
| CN102538390A (en) * | 2011-12-22 | 2012-07-04 | 西安交通大学 | Novel natural gas liquefaction system and natural gas liquefaction method |
| CN104204698A (en) * | 2012-03-30 | 2014-12-10 | 埃克森美孚上游研究公司 | Lng formation |
| CN104204698B (en) * | 2012-03-30 | 2017-09-08 | 埃克森美孚上游研究公司 | Liquefied natural gas is formed |
| CN105074370A (en) * | 2012-12-28 | 2015-11-18 | 林德工艺装置股份有限公司 | Integrated process for NGL (natural gas liquids recovery) and LNG (liquefaction of natural gas) |
| CN105074370B (en) * | 2012-12-28 | 2017-04-19 | 林德工程北美股份有限公司 | Integrated process for NGL (natural gas liquids recovery) and LNG (liquefaction of natural gas) |
| CN103175379B (en) * | 2013-03-18 | 2015-10-14 | 上海交通大学 | Utilize pipeline pressure can prepare device and the using method of liquefied natural gas |
| CN103175379A (en) * | 2013-03-18 | 2013-06-26 | 上海交通大学 | Device for preparing liquefied natural gas with pipeline pressure energy and application method thereof |
| CN104315801A (en) * | 2014-10-15 | 2015-01-28 | 中国海洋石油总公司 | Mixed refrigerant-expansive refrigeration-circulated natural gas liquefying method |
| CN107110599A (en) * | 2015-01-09 | 2017-08-29 | 三菱重工业株式会社 | Gas liquefaction equipment and gas liquefaction method |
| CN107110599B (en) * | 2015-01-09 | 2019-12-27 | 三菱重工工程株式会社 | Gas liquefaction device and gas liquefaction method |
| CN106091574B (en) * | 2016-06-02 | 2018-10-30 | 成都深冷液化设备股份有限公司 | Gas liquefaction device with compression heat recovery function and liquefaction method thereof |
| CN108759302A (en) * | 2018-06-04 | 2018-11-06 | 中海石油气电集团有限责任公司 | A kind of high-pressure natural gas liquefaction system and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101228405B (en) | 2010-12-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101228405B (en) | Natural gas liquefaction process for producing LNG | |
| EP1929227B1 (en) | Natural gas liquefaction process for lng | |
| CN102334001B (en) | Liquefaction method and system | |
| US8616021B2 (en) | Natural gas liquefaction process | |
| US9140490B2 (en) | Natural gas liquefaction processes with feed gas refrigerant cooling loops | |
| CN101097112B (en) | Method for air feeding in low temperature separation process | |
| US6751985B2 (en) | Process for producing a pressurized liquefied gas product by cooling and expansion of a gas stream in the supercritical state | |
| CN100445673C (en) | System and process for liquefying high pressure natural gas | |
| CN100410609C (en) | Hybrid gas liquefaction cycle with multiple expanders | |
| CN101156038B (en) | Method and apparatus for liquefying a natural gas stream | |
| CN1206505C (en) | Process for liquefying naturla gas by expansion cooling | |
| US4970867A (en) | Liquefaction of natural gas using process-loaded expanders | |
| CN101413750A (en) | System to cold compress an air stream using natural gas refrigeration | |
| CA3079890C (en) | Natural gas liquefaction by a high pressure expansion process using multiple turboexpander compressors | |
| CN103109144A (en) | Refrigerant composition control | |
| US6006545A (en) | Liquefier process | |
| CN102155841A (en) | Cryogenic separation method and apparatus | |
| CA2898745C (en) | Process for cooling a hydrocarbon-rich fraction | |
| CA3109918C (en) | Managing make-up gas composition variation for a high pressure expander process | |
| CN102149998B (en) | Air separation refrigeration supply method | |
| CN204785551U (en) | BOG recovery unit that liquefies again | |
| CN106016967A (en) | Regenerative mixed working-medium refrigerating gas liquefaction cycle system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20101208 Termination date: 20150524 |
|
| EXPY | Termination of patent right or utility model |