Lng expander cycle process employing integrated cryogenic purification
阅读：585发布：2023-05-23
专利汇可以提供Lng expander cycle process employing integrated cryogenic purification专利检索，专利查询，专利分析的服务。并且A process and apparatus for the liquefaction of natural gas wherein raw feedstock is cryogenically fractionated to remove essentially all of the carbon dioxide and C5 hydrocarbons therefrom, and wherein the cryogenically purified feedstock is cooled and liquefied under pressure in a cryogenic heat exchanger. The pressurized cold liquid from the heat exchanger is isenthalpically expanded to reduce the pressure and further cool the liquid while at the same time flashing a minor gas fraction. Refrigeration for the liquefaction of the natural gas is supplied by a circulating refrigerant stream which is compressed and workexpanded to obtain the necessary cooling. The minor flash gas portion of the liquefaction step is commingled with the circulating refrigerant stream so that the analysis of the refrigerant stream is always rich in the lighter portions of the liquefaction stream, thus aiding in maintaining refrigeration temperature differentials to drive the liquefaction step. The work-expanded refrigerant portion undergoes a compression cycle and is work-expanded in a series of expansion turbines. The expansion turbines furnish at least part of the power necessary to drive the compressor system in the refrigerant gas cycle.，下面是Lng expander cycle process employing integrated cryogenic purification专利的具体信息内容。
2. Removing the liquid water phase from the process;
2. Removing the liquid water phase from the process;
2. The process of claim 1 wherein the nitrogen-methane and C2 to C5 hydrocarbon mixture in Step (8) is at a pressure in the range of from about 350 to about 750 psia.
3. The process of claim 1 wherein the nitrogen-methane and C2 to C5 hydrocarbon mixture in Step (8) is maintained at a pressure relative to its analysis such that the plot of the temperature vs. enthalpy of the mixture approaches as straight a line as is reasonably possible.
3. Substantially isentropically expanding the light hydrocarbon vapor phase in a work recovery engine to obtain mechanical energy and to cool the light hydrocarbon vapor phase;
3. Substantially isentropically expanding the light hydrocarbon vapor phase in a work recovery engine to obtain mechanical energy and to cool the light hydrocarbon vapor phase;
4. Fractionating the heavy hydrocarbon liquid phase from Step (1) and the cooled light hydrocarbon vapor phase from Step (3) to form (a) a methane-nitrogen fraction substantially free of carbon dioxide and hydrocarbons heavier than methane and (b) a carbon dioxide-hydrocarbon fraction substantially free of nitrogen and containing C2 and heavier hydrocarbons;
4. Fractionating the heavy hydrocarbon liquid phase from Step (1) and the cooled light hydrocarbon vapor phase from Step (3) to form (a) a meThane-nitrogen fraction substantially free of carbon dioxide and hydrocarbons heavier than methane and (b) a carbon dioxide-hydrocarbon fraction substantially free of nitrogen and containing C2 and heavier hydrocarbons;
4. The process of claim 1 wherein the flow rate of the combined methane-nitrogen gas mixture in Step (8) is from about 1.5 to about 4 times the flow rate of the nitrogen-methane and C2 to C5 hydrocarbon mixture in Step (8), expressed as Mols per hour.
5. The process of claim 3 wherein the flow rate of the combined methane-nitrogen gas in Step (8) is maintained at such a rate that the temperature vs. enthalpy curve for the combined gas as closely as possible parallels the temperature vs. enthalpy curve of the nitrogen-methane and C2 to C5 hydrocarbon mixture; whereby more effective heat exchange between the combined gas and the nitrogen-methane and C2 to C5 hydrocarbon mixture is effected.
5. Separating the methane-nitrogen fraction into a first portion and a second portion;
5. Fractionating the carbon dioxide-hydrocarbon fraction from Step (4) into (a) a substantially carbon dioxide fraction, (b) a C5 and heavier hydrocarbon fraction and, (c) C2 to C5 hydrocarbon fraction and removing the carbon dioxide and C5 and heavier hydrocarbon fractions from the process;
6. Compressing and cooling the C2 to C5 hydrocarbon fraction from Step (5) to form a low temperature liquid stream;
6. Heat exchanging the first portion with a first isentropically expanded methane-nitrogen refrigerant gas obtained subsequently so as to remove heat from the first portion and to heat the first isentropically expanded methane-nitrogen refrigerant gas;
6. The process of claim 1 wherein the compressed, methane nitrogen refrigerant gas mixture from Step (13) is at a pressure from about 400 to about 600 psia.
7. The process of claim 1 wherein the compression of Step (13) is effected in a plurality of stages and the gas is cooled interstage.
7. Combining the low temperature liquid stream of Step (6) with at least a portion of the methane-nitrogen fraction from Step (4) so as to form a nitrogen-methane and C2 to C5 hydrocarbon mixture;
7. Returning the heat exchanged first portion to the fractionation of Step (4) as reflux;
8. Fractionating the carbon dioxide-hydrocarbon fraction from Step (4) to separate carbon dioxide from the C2 and heavier hydrocarbons and removing the carbon dioxide from the process;
8. The process of claim 1 wherein the minor portion of the combined gas mixture removed in Step (17) is charged to a separate work recovery engine whereby mechanical energy is obtained, and wherein the mechanical energy as obtained is employed at least to compress partly the major portion of the combined gas mixture.
8. Cooling the nitrogen-methane and C2 to C5 hydrocarbon mixture under elevated pressure by heat exchange with a combined gas mixture consisting essentially of methane and nitrogen produced subsequently whereby the combined gas mixture is heated and a predominant portion of the nitrogen-methane and C2 to C5 hydrocarbon mixture is liquified so as to form a predominantly liquid, liquid-vapor mixture;
9. A process for liquifying a natural gas mixture comprising nitrogen, carbon dioxide, water and lower boiling hydrocarbons so as to produce a substantially carbon dioxide- and water-free liquid natural gas, which process comprises:
9. Fractionating the C2 and heavier hydrocarbons from Step (8) to form a C2-C4 hydrocarbon fraction and a C4 and heavier hydrocarbon fraction and removing the C4 and heavier hydrocarbon fraction from the process;
9. Substantially isenthalpically reducing the pressure of the cooled predominantly liquid, liquid-vapor nitrogenmethane and C2 to C5 hydrocarbon mixture so as further to cool it and to form a minor gas fraction consisting essentially of a mixture of methane and nitrogen while liquifying completely the balance of the cooled stream to form a major liquid fraction containing methane and substantially all the hydrocarbons heavier than methane through C5;
10. Separating the minor, methane-nitrogen gas fraction from the major liquid fraction and recovering the major liquid fraction as liquified natural gas product;
10. Compressing and cooling the C2-C4 hydrocarbon fraction from Step (9) to form a low temperature liquid stream;
10. The process of claim 9 wherein the nitrogen-methane and C2-C4 hydrocarbon mixture in Step (13) is at a pressure in the range from about 350 to about 750 psia.
11. The process of claim 9 wherein the nitrogen-methane and C2-C4 hydrocarbon mixture in Step (13) is maintained at a pressure relative to its analysis such that the plot of the temperature vs. enthalpy of the mixture approaches as straight a line as is reasonably possible.
11. Combining the low temperature liquid stream of Step (10) with the second portion of the methane-nitrogen fraction from Step (4) so as to form a nitrogen-methane and C2-C4 hydrocarbon mixture;
11. Combining the minor, methane-nitrogen gas fraction with an isentropically expanded, refrigerant gas mixture produced subsequently and consisting essentially of methane and nitrogen to form the combined gas mixture;
12. Employing the combined gas mixture formed in Step (11) at least partially to cool the nitrogen-methane and C2 to C5 hydrocarbon mixture in Step (8);
12. Cooling the nitrogen-methane and C2-C4 hydrocarbon mixture under elevated pressure by heat exchange with a first isentropically expanded methane-nitrogen refrigerant gas obtained subsequently, thereby heating the first isentropically expanded refrigerant gas;
12. The process of claim 9 wherein the flow rate of the combined methane-nitrogen gas mixture in Step (13) is from about 1.5 to about four times the flow rate of the nitrogen-methane and C2-C4 hydrocarbon mixture in Step (13), expressed as moles per hour.
13. The process of claim 12 wherein the flow rate of the combined methane-nitrogen gas is maintained at such a rate that the temperature vs. enthalpy curve for the combined gas as closely as possible parallels the temperature vs. enthalpy curve of the nitrogen-methane and C2-C4 hydrocarbon gas mixture, whereby more effective heat exchange between the combined gas and the nitrogen-methane and C2-C4 hydrocarbon gas mixture is effected.
13. Cooling further the nitrogen-methane and C2-C4 hydrocarbon mixture under elevated pressure by heat exchange with a combined gas mixture consisting essentially of methane and nitrogen produced subsequently whereby the combined gas mixture is heated and a predominant portion of the nitrogenmethane and C2-C4 hydrocarbon mixture is liquified so as to form a predominantly liquid, liquid-vapor mixture;
13. Compressing a major portion of the heated, combined gas mixture from Step (8) to provide a compressed refrigerant gas mixture;
14. Heat exchanging at least the major portion of the combined gas mixture prior to the compression of Step (13) with the compressed refrigerant gas mixture whereby the at least major portion of the heated, combiNed gas mixture is further heated to a temperature from about -50* to about 300*F. and the compressed refrigerant gas mixture is cooled;
14. Substantially isenthalpically reducing the pressure of the cooled predominantly liquid, liquid-vapor nitrogen-methane and C2-C4 hydrocarbon mixture so as further to cool it and to form a minor gas fraction consisting essentially of a mixture of methane and nitrogen while liquifying completely the balance of the cooled stream to form a major liquid fraction containing methane and the C2-C4 hydrocarbons;
14. The process of claim 9 wherein the compressed, methane-nitrogen refrigerant gas mixture from Step (18) is at a pressure from about 400 to about 600 psia.
15. The process of claim 9 wherein the compression of Step (18) is effected in a plurality of stages and the gas is cooled interstage.
15. Separating the minor, methane-nitrogen gas fraction from the major liquid fraction and recovering the major liquid fraction as liquified natural gas product;
15. Additionally cooling the compressed refrigerant gas to a temperature such that in expansion in a work recovery engine the temperature and enthalpy are sufficiently low to provide the refrigeration required for Step (8);
16. Substantially isentropically expanding the additionally cooled, compressed refrigerant gas mixture in a work recovery engine to obtain mechanical energy and to further cool the refrigerant gas, whereby the isentropically expanded, refrigerant gas mixture is formed;
16. Combining the minor, methane-nitrogen gas fraction with a second isentropically expanded, refrigerant gas mixture produced subsequently and consisting essentially of methane and nitrogen to form the combined gas mixture;
16. A continuous process for the liquefaction of natural gas which comprises the steps of: Condensing the natural gas mixture under elevated pressure to form (a) a liquid water phase, (b) a heavy hydrocarbon liquid phase containing nitrogen and carbon dioxide and (c) a light hydrocarbon vapor phase containing nitrogen and carbon dioxide; removing the liquid water phase from the process; adjusting the pressure of the heavy hydrocarbon liquid phase and the light hydrocarbon vapor phase to a range of from about 350 to about 750 psia; fractionating the pressure adjusted heavy and light hydrocarbon phases to form (a) a methane-nitrogen fraction substantially free of carbon dioxide and hydrocarbons heavier than methane and (b) a carbon dioxide-hydrocarbon fraction substantially free of nitrogen and containing C2 and heavier hydrocarbons; fractionating further the carbon dioxide-hydrocarbon fraction to form a C2-C4 hydrocarbon fraction and a C4 and heavier hydrocarbon fraction and removing the C4 and heavier hydrocarbon fraction from the process; combining the C2-C4 hydrocarbon fraction with the carbon dioxide free methane-nitrogen fraction to form a substantially purified natural gas mixture; cooling and substantially completely liquifying the purified natural gas mixture in a countercurrent heat exchanger-liquifier; flash evaporating a minor gas fraction from the cooled effluent from the heat exchanger-liquifier by substantially isenthalpically reducing the pressure thereof, said flash evaporation causing the temperature of both the minor gas fraction and the remaining major liquid fraction to decrease; collecting the major liquid fraction as product and returning the flashed fraction to a point where it is combined with an isentropically expanded refrigeration gas fraction produced subsequently in the process; passing said combined gases countercurrently to the purified natural gas mixture in said heat exchanger-liquifier at a flow rate of two to four times that of the purified natural gas stream; separating the warmed effluent from said heat exchanger-liquifier into a major refrigeration gas fraction and a minor fuel gas fraction; passing the refrigeration gas fraction through a counter-current heat exchanger precooler to a compressor system to be compressed to a pressure in the range of about 400 to 600 psia; passing the pressurized gas from said compressor system through said heat exchanger precooler to cool the refrigeration gas; isentropically expanding the cooled effluent from said heat exchanger precooler with an expansion engine at a temperature and pressure sufficient to maintain the gas in the gaseous state in said expansion turbine to form the isentropically expanded refrigeration gas, whereby mechanical energy is obtained and the pressure of the refrigeration gas fraction is reduced, thereby further cooling such fraction; combining the further cooled, reduced pressure, isentropically expanded refrigeration gas effluent from said expansion engine with said flash gas to a point prior to entry into said heat exchanger-liquifier; and utilizing (a) the fuel gas fraction to furnish fuel for a gas driven turbine which provides a portion of the mechanical energy necessary to drive said compressor system and (b) the mechanical energy obtained from the isentropic expansion to provide an additional portion of the mechanical energy necessary to drive the said compressor system.
17. In an integrated apparatus for purifying and liquifying natural gas, the combination comprising: gas-liquid separating means for separating condensed water and a heavy hydrocarbon condensate from a pressurized natural gas mixture comprising nitrogen, carbon dioxide, water and lower boiling hydrocarbons; means for adjusting the pressure of the heavy hydrocarbon condensate and the water and heavy hydrocarbon condensate-free remainder of the natural gas mixture to about 350 to about 750 psia; means for fractionating the combined, pressure adjusted hydrocarbon condensate and water-free natural gas mixture to form a methane-nitrogen fraction substantially free of carbon dioxide and a carbon dioxide-hydrocarbon fraction substantially free of nitrogen and containing predominantly C2 hydrocarbons; means for fractionating the carbon dioxide-hydrocarbon fraction to form a carbon dioxide fraction and a C2 hydrocarbon fraction, said carbon dioxide fraction including all of the methane present in the carbon dioxide-hydrocarbon and a portion of the C2 hydrocarbons contained therein; means for combining the C2 hydrocarbon fraction with the methane-nitrogen fraction, thus forming a substantially water-free and carbon dioxide-free natural gas mixture; a heat exchanger-liquifier for cooling and liquifying the water-free and carbon dioxide-free natural gas by countercurrent heat exchange with a combined flash gas and work expanded refrigerant gas from an expansion engine; means for isenthalpically expanding anD partially flashing the natural gas effluent from said heat exchanger-liquifier; gas-liquid separating means for separating said expanded effluent into a major liquid fraction and a minor flash gas fraction; means for recovering the major liquid fraction as product; means for passing the flash gas to the heat exchanger-liquifier; compression means for compressing the combined flash gas and work expanded refrigerant gas from the heat exchanger-liquifier; a heat exchanger precooler for precooling the gas coming from the compression means by countercurrent heat exchange with the combined flash gas and work expanded gas from said heat exchanger-liquifier; an expansion engine for work expanding said precooled gas, said engine further cooling the precooled gas and reducing the pressure thereof while generating mechanical energy; means for feeding the work expanded and cooled gas from said expansion engine to said heat exchanger-liquifier to join said flash gas; and means for bleeding from the apparatus a minor portion of the combined flash gas and work expanded gas prior to compression thereof, said expansion engine and said compression means being operatively cooperative whereby the mechanical energy obtained from said engine supplies at least a portion of the work required to operate said compression means.
17. Employing the combined gas mixture formed in Step (16) to cool the nitrogen-methane and C2-C4 hydrocarbon mixture in Step (13);
17. Removing from the process system subsequent to Step (8) a minor portion of the combined gas mixture substantially equal in magnitude to the minor methane-nitrogen gas fraction formed in Step (9); and
18. Employing the mechanical energy obtained from the work recovery engines of Steps (3) and (16) to compress, at least partly, the major portion of the combined refrigerant gas mixture in Step (13).
18. Compressing at least a major portion of the heated, combined gas mixture from Step (13) to provide a compressed refrigerant gas mixture;
19. Heat exchanging at least a major portion of the combined gas mixture prior to the compression of Step (18) with the compressed refrigerant gas mixture whereby the at least major portion of the heated, combined gas mixture is further heated to a temperature from about -50* to about 300*F. and the compressed refrigerant gas mixture is cooled;
20. Additionally cooling the compressed refrigerant gas to a temperature such that in expansion in a wOrk recovery engine the temperature and enthalpy are sufficiently low to provide the refrigeration required for Steps (12) and (13);
21. Substantially isentropically expanding the additionally cooled, compressed refrigerant gas mixture in a work recovery engine to obtain mechanical energy and to further cool the refrigerant gas, whereby the first isentropically expanded, methane-nitrogen refrigerant gas is formed;
22. Substantially isentropically expanding the heated first isentropically expanded refrigerant gas from Step (12) in a work recovery engine whereby (a) mechanical energy is obtained, (b) the heated refrigerant gas is cooled, and (c) the second isentropically expanded methane-nitrogen refrigerant gas is formed;
23. Removing from the process system subsequent to Step (13) a minor portion of the combined gas mixture substantially equal in magnitude to the minor methane-nitrogen gas fraction formed in Step (14); and
24. Employing the mechanical energy obtained from the work recovery engine of Steps (3), (21) and (22) at least to compress partly the major portion of the combined refrigerant gas mixture in Step (18).
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