EP1118827B1 - Procédé de liquéfaction partielle d'un fluide contenant des hydrocarbures tel que du gaz naturel - Google Patents
Procédé de liquéfaction partielle d'un fluide contenant des hydrocarbures tel que du gaz naturel Download PDFInfo
- Publication number
- EP1118827B1 EP1118827B1 EP01400050A EP01400050A EP1118827B1 EP 1118827 B1 EP1118827 B1 EP 1118827B1 EP 01400050 A EP01400050 A EP 01400050A EP 01400050 A EP01400050 A EP 01400050A EP 1118827 B1 EP1118827 B1 EP 1118827B1
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- EP
- European Patent Office
- Prior art keywords
- fluid
- line
- liquid
- liquefaction
- natural gas
- 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.)
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 106
- 238000000034 method Methods 0.000 title claims description 54
- 239000003345 natural gas Substances 0.000 title claims description 34
- 229930195733 hydrocarbon Natural products 0.000 title claims description 18
- 150000002430 hydrocarbons Chemical class 0.000 title claims description 18
- 239000004215 Carbon black (E152) Substances 0.000 title claims description 6
- 239000012530 fluid Substances 0.000 claims description 86
- 239000007788 liquid Substances 0.000 claims description 56
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 34
- 238000005194 fractionation Methods 0.000 claims description 20
- 239000001294 propane Substances 0.000 claims description 17
- 238000001816 cooling Methods 0.000 claims description 16
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 15
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical class CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 13
- 235000013844 butane Nutrition 0.000 claims description 10
- 239000002826 coolant Substances 0.000 claims description 8
- 230000003247 decreasing effect Effects 0.000 claims description 8
- 230000005611 electricity Effects 0.000 claims description 6
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 5
- 239000001273 butane Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 description 53
- 238000005057 refrigeration Methods 0.000 description 46
- 239000007789 gas Substances 0.000 description 43
- 239000003507 refrigerant Substances 0.000 description 40
- 238000010586 diagram Methods 0.000 description 15
- 239000003949 liquefied natural gas Substances 0.000 description 15
- 150000001875 compounds Chemical class 0.000 description 9
- 238000009834 vaporization Methods 0.000 description 9
- 238000001035 drying Methods 0.000 description 8
- 230000008016 vaporization Effects 0.000 description 8
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 7
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- 238000010992 reflux Methods 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 4
- 239000005977 Ethylene Substances 0.000 description 4
- 238000007792 addition Methods 0.000 description 4
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 239000012808 vapor phase Substances 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- -1 des pentanes Chemical class 0.000 description 2
- 239000008246 gaseous mixture Substances 0.000 description 2
- 239000001282 iso-butane Substances 0.000 description 2
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
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- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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Definitions
- the present invention relates to a method for at least partially liquefy a fluid or a gaseous mixture formed at less in part of a mixture of hydrocarbons, for example a natural gas.
- Natural gas is commonly produced at remote sites of use and it is common to liquefy it in order to transport it on long distances for example by LNG carrier or to store it under liquid form.
- natural gas we mean within the meaning of this description, a mixture formed mainly of methane, but which can also contain other hydrocarbons and nitrogen, whatever the state in which it is found (gas, liquid or two-phase).
- Natural gas in departure occurs mainly in the gaseous state, and at such a pressure, that during the liquefaction stage, it can be in different states, for example liquid and gaseous coexisting at a given time.
- a mixture of fluids used as a fluid refrigerant in the external refrigeration cycle, is vaporized, compressed, cooled by exchanging heat with an ambient medium such as water or air, condensed, relaxed and recycled.
- the refrigerant mixture used in the second stage in which is ensured the second refrigeration step is cooled by heat exchange with the ambient cooling, water or air, then the first stage in which ensures the first stage of refrigeration.
- the refrigerant mixture is in the form of a two-phase fluid comprising a vapor phase and a liquid phase.
- Said phases are separated, for example in a separator flask, and sent, for example, in a wound exchanger, in which the fraction steam is condensed, while natural gas is liquefied under pressure, the refrigeration being ensured by vaporization of the liquid fraction of the mixture refrigerant.
- the liquid fraction obtained by condensation of the vapor fraction is sub-cooled, expanded and vaporized to ensure final liquefaction natural gas, which is sub-cooled before being expanded through a valve or a turbine to produce the Liquefied Natural Gas (LNG) sought.
- LNG Liquefied Natural Gas
- This document shows a process in which natural gas is cooled by heat exchange with an external refrigerant and then by heat exchange with gaseous fractions from the expansion liquefied natural gas.
- Another arrangement according to the prior art consists in operating by means of three refrigeration cycles in series, each of which operates with a pure body as a refrigerant.
- a first cycle running on propane allows to condense ethylene under pressure at a temperature about - 35 ° C.
- the vaporization of ethylene at a pressure close to the atmospheric pressure in a second cycle allows to condense methane under pressure at a temperature of approximately - 100 ° C.
- Vaporization methane allows to sub-cool the liquefied natural gas (LNG) produced and to be able to relax it so that it can be stored and transported to a pressure close to atmospheric pressure.
- LNG liquefied natural gas
- the present invention relates to a process for partial liquefaction of a fluid G or a gaseous mixture formed at least in part of hydrocarbons, such than a natural gas GN, and its implementation device.
- the process of present invention at least partially overcomes the aforementioned drawbacks of prior art.
- At least part of the gaseous fraction representing at least 20 percent by weight relative to the weight of the fluid G initially introduced into said process can be used to produce electricity.
- At least part of the gaseous fraction representing at least 20 percent by weight relative to the weight of the fluid G initially introduced into said process can be reinjected into the zone to from which it is recovered and in particular in the case where the fluid G is a natural gas in the well from which it is recovered.
- Step a) of refrigeration comprises for example several exchange zones heat and refrigeration can be provided in said exchange zones successive heat using the external refrigerant M which is expanded and vaporized at decreasing pressure levels.
- the fluid G leaves monophasic condensed from step at).
- the fluid G leaves in dense phase of step a).
- the external refrigerant M comprises at least one hydrocarbon and preferably at least two hydrocarbons. This or these hydrocarbons are preferably chosen from the group formed by methane, ethane, propane and butanes. According to a particular embodiment of the method of the invention the external refrigerant M comprises methane, ethane, propane and at least one butane
- Step b) comprises for example a single exchange zone, in which the liquefied fluid G is sub-cooled.
- the liquefied gas is separated into two parts: one part being sent to the storage after expansion, the other part being relaxed and returned to the same exchange zone to produce by vaporization the cold necessary for under cooling and possibly when the fluid G entering said step b) is not completely liquid to the total liquefaction of said fluid G.
- the part of the fluid G used for produce the cold necessary for this step b) is vaporized at different levels decreasing pressure.
- step b) A preferred option for step b) is as follows: at the end of step b) the liquefied gas is expanded to an intermediate pressure, between 0.3 and 1.2 MPa, using either a liquid turbine or a Joule-Thomson valve.
- the fluid G is completely liquid at the end of this first expansion.
- the fluid G is then separated into two substantially equal parts: a part usually being sent after expansion to cryogenic storage, possibly after a denitrogenation step comprising a partial re-vaporization, the rest being returned, partly to pressure intermediate and for the other party at a lower pressure towards step b) to produce by vaporization the cold necessary for sub-cooling, and optionally when the fluid G entering said step b) is not totally liquid to the total liquefaction of said fluid G.
- the operating conditions of the process according to the invention will preferably be chosen so that the quantity of liquefied gas obtained is approximately 20 to about 80% by weight, more preferably about 30% to approximately 70% by weight of the quantity of gas at the inlet of the process.
- the liquefied part of the fluid G circulating in the line (21) (designated above by the terms “The other part") is relaxed and partially vaporized in one stage until storage pressure.
- the liquefied part of the fluid G circulating in the line (18) (hereinafter referred to as "the other party") is relaxed and partially vaporized in two stages until storage pressure.
- the process liquefies about 50 percent (%) by weight of the gas entering, while 50% by weight leaves as of gas at a lower pressure than that at which it is at the inlet.
- the specific power per unit of gas liquefied is around 600 kilojoule per kilo (kJ / kg), which is much lower at the usual specific powers (approximately 1000 kJ / kg).
- This configuration could be applied when together with the liquefaction, we have a central electric operating for example using a natural gas turbine, the compressors used for liquefaction would then be driven by a small part of the electricity produced by the power plant.
- a unit of 300 megawatt (MW) could be associated with a liquefaction of 0.4 million tonnes per year, consuming about 8 MW.
- the method could also be associated with a scheme comprising a gas reinjection as specified above.
- the simplified diagram of Figure 3 illustrates how (not limited) the gas pre-cooling (R) can be performed.
- the gas G must be almost completely liquefied at the end of this stage, which requires descending more low than with a propane cycle.
- a refrigerant mixture M is therefore used, mainly comprising ethane and propane, and lower quantity of methane and butanes.
- the gas G enters via line (10) into the pre-refrigeration section (R) of the gas, where it is cooled and liquefied successively in the exchange zones E10, E11, and E12, from which it leaves by lines (11), (12) and (13) respectively. In line (13), the fluid G is almost completely liquefied.
- the refrigerant mixture M is compressed by the compressor K10, from where it leaves via the conduit (100). It is condensed by the condenser C10, from where it exits at the bubble point via the conduit (101) for be partly sent to the exchange zone E10 where it is under cooled. he leaves the exchange zone E10 via the conduit (102) to be partly sent to exchange area E11. Another part of the refrigerant mixture M circulating in the line (102) is taken and sent by the conduit (131) in the valve V10 in which it is relaxed then reintroduced by the conduit (132) in the exchange zone E10 where this cooling mixture M is vaporized to produce the cold necessary for this area.
- the refrigerant mixture M leaving the exchange zone E11 is partly sent to the exchange area E12 via the conduit (103).
- Another part of the refrigerant mixture M circulating in the line (103) is taken and sent through the conduit (121), into the valve V11 in which it is relaxed and then returned to the exchange zone E11 by the conduit (122) where it is sprayed to provide the necessary cold for this area.
- the mixture refrigerant leaves the exchange zone E12 via the conduit (111), it crosses the valve V12 in which it is relaxed, then sent by the line (112) in the exchange zone E12 where it is vaporized, to supply the cold for this zone.
- Valves V10, V11, V12 expand the refrigerant mixture M to decreasing pressures corresponding to vaporization temperatures decreasing in the three exchange zones E10, E11 and E12.
- three exchange zones E10, E11, and E12 the vaporized refrigerant mixture is sent to three different stages of the K10 compressor respectively by the conduits (133), (123) and (113).
- the simplified diagram of FIG. 5 presents a variant making it possible to recover almost all of the C2 + compounds (i.e. compounds having at least two carbon atoms, such as ethane, propane, butanes, etc.) present in liquefied natural gas.
- the gas leaving the compressor K1 through the conduit (25) and intended to be burned in turbines is first refrigerated using the pre-refrigeration section (R), then sent by line 62 at the bottom of the fractionation column T2.
- a small part of the refrigerated and liquefied natural gas leaving of the pre-cooling section (R) by the line (61) is expanded in the valve V61 before being introduced at the head of column T2.
- the methane content of the combustible gas at the top of T2 will be around 90% molar, and the methane content of liquefied natural gas of 64 mol%.
- the rest of the diagram is identical to what has been described above in connection with the illustration in figure 2.
- At least part of the gaseous fraction representing at least 10% by weight relative to the weight of the fluid G initially introduced in said process is used to produce electricity.
- At least part of the fraction gaseous representing at least 10% by weight relative to the weight of the fluid G initially introduced in said process is reinjected into the zone from from which it is recovered and in the case where the fluid G is a natural gas in the well from which it is recovered.
- the other liquefied part of the fluid G is expanded and partially vaporized in one or two stages until the pressure of the storage.
- the part of the fluid G used to produce the necessary cold at the second stage is sprayed at different pressure levels decreasing.
- the operating conditions are chosen to so that the quantity of liquefied gas obtained is approximately 20% at approximately 80% by weight of the quantity of gas at the inlet of the process.
- the first refrigeration step comprises several heat exchange zones and refrigeration is provided in said heat exchange zones using the external refrigerant M which is expanded and vaporized at pressure levels decreasing.
- the external refrigerant M comprises at least one hydrocarbon and preferably at least two hydrocarbons.
- the external refrigerant M comprises at least one hydrocarbon chosen from the group formed by methane, ethane, propane and butanes. Even more preferably, the refrigerant external M includes methane, ethane, propane and at least one butane.
- the fluid G exits single-phase condensed from the first stage of refrigeration. More preferably, the fluid G leaves in dense phase of the first stage of refrigeration.
- the fluid G is at a temperature at least below about - 40 ° C.
- the vaporized part of the fluid G in the second step of the process is compressed to a pressure sufficient, to allow its reinjection into the area from which it is recovers and in case fluid G is a natural gas in the well from from which we recover it.
- the vaporized part of fluid G in the second step of the process is compressed to a sufficient pressure, to allow its use to produce electricity especially in a gas turbine.
- the part of the fluid G compressed to a pressure sufficient for its use in a gas turbine is cooled using the first stage of pre-refrigeration then sent to the bottom of a fractionation column in which also introduces at the head of said column a part of the same fluid G cooled in the first pre-refrigeration step and relaxed.
- the liquefaction method according to the invention may optionally further comprise a drying step and a step of fractionating natural gas comprising at least two fractionation columns, said fractionation being carried out immediately after drying, by feeding the first fractionation column with the drying temperature, and using the second exchange zone of the first refrigeration step for the condenser of said column. More preferably, the product leaving the bottom of the first fractionation column is refrigerated in the pre-refrigeration section using the external refrigerant M used in the first pre-refrigeration stage, before being expanded and sent in head of the second fractionation column.
- This gas arrives in the liquefaction unit at a pressure of 5.6 MPa and at a temperature of 40 ° C. We also considered a temperature of 40 ° C for the process side output of the water exchangers.
- Natural gas G is supplied by line (10) to the exchanger E13 in which it is cooled by an intermediate fluid (FI), to a temperature of 19 ° C then is sent via line (51) to the dryer (S) before entering via the conduit (52) in the fractionation zone (F).
- This fractionation zone usually comprises at least two fractionation columns.
- the intermediate fluid FI is moved by the circulation system Cl, and cooled in the exchange zone E10 of the pre-refrigeration section (R).
- the fractionation F has a first column T11.
- the dry gas is sent to the bottom of column T11 by the line (52). This dry gas enters column T11 at its outlet temperature of the drying section.
- the fraction leaving the top of column T11 is sent through the conduit (58) at a temperature of 12 ° C to the area exchange E11 of the pre-refrigeration section (R) from which it leaves partially condensed at a temperature of - 0.5 ° C before being sent by line (59) to the reflux ball B11.
- the P51 pump is used to return by line 201 the liquid fraction separated in the flask B11 and leaving by the line 200 to column T11 and thus ensure reflux into the column.
- the gas leaving balloon B11 through line (53) is purified from too heavy cuts and in particular benzene.
- the gas is sent through the conduit (53) (see figure 7) to the exchange zone E11 where it will be cooled to - 25 ° C before being sent to the exchange zone E12 via the conduit (12).
- the liquid leaving through the line (81) ( Figure 6) at the bottom of column T11 includes enough compounds C2 and C3 (compounds comprising 2 and 3 atoms respectively carbon) for the coolant mixture additions.
- This liquid mixture circulating in the line (81) is sent to the pre-refrigeration section (R2) from where it leaves cooled by the conduit (82), then it is relaxed through the valve V51 and sent via line (83) at the head of column T12 (Demethanizer).
- This column is reboiled using the reboiler E51 to remove most of the methane from the mixture.
- Gas coming out on top from column T12 by line (54), rich in methane, will be remixed with the rest of the combustible gas leaving the compressor K1 via the line (25) (see figure 8).
- the product leaving the bottom of column T12 via line (84) (see Figure 6) is sent, after expansion in the valve V52, by the conduit (85) in column T13.
- This column is reboiled using the exchanger E52. The gas leaving the head of column T13 (FIG.
- the mixture thus refrigerated leaves this pre-refrigeration section (R2) by the line (57) then it is mixed with the refrigerated and liquefied gas circulating in the line (12) before being sent to the exchange area E12.
- the part of the refrigerant mixture M entering the pre-refrigeration section (R2) through the line (1001) is cooled, separated and expanded at two pressure levels to produce the cold necessary for cooling the incoming mixture in this section by line (56).
- the different vaporized parts leaving respectively by lines (1123) and (1133) are returned with the fluids in the same pressure, entering respectively by lines (123) and (133) in the compressor K10.
- the pre-refrigeration section (R) (simplified diagram of FIG. 7) implements a mixture of refrigerant M whose composition in molar percent (% mol.) Is as follows: Methane 1.9 Ethane 46.5 Propane 44.0 isobutane 4.9 N-Butane 2.7
- This mixture leaves the compressor K10 by the line (100) compressed to a pressure of 3.23 MPa.
- Intermediate cooling C11 is required to bring the fluid leaving by line 141 of the second stage of the fluid to 40 ° C. compressor K10 before reintroducing it via line (142) on the third compressor stage K10.
- the mixture circulating in line (100) is cooled to a temperature of 40 ° C by the exchanger C10 from which it leaves fully condensed by line (101).
- a small part of the mixture M is sent by line (1001) to the pre-cooling zone (R2), the rest is sent to heat exchange zone E10. It is sub-cooled successively in the heat exchange zones E10, E11, and E12.
- the refrigerant mixture M leaving the exchange zone E11 is partly sent to the exchange area E12 via the conduit (103).
- Another part of the refrigerant mixture M circulating in the line (103) is taken and sent through the conduit (121), into the valve V11 in which it is relaxed and then reintroduced into the exchange zone E11 by the conduit (122) where it vaporizes to provide the cold necessary for this area.
- the refrigerant mixture leaves the exchange zone E12 via the conduit (111), it crosses the valve V12 in which it is relaxed, then sent by the line (112) in the exchange zone E12 where it is vaporized, to supply the cold of this zone.
- the part of the mixture entering through the line (122) in the exchanger E11 in which it vaporizes is sent by the line (123) to the compressor K10 at a pressure of 0.655 MPa.
- the part of the mixture entering through the line (112) in the exchanger E12 in which it vaporizes is sent by the line (113) to the 1st stage of the compressor K10 at the pressure of 0.15 MPa.
- Total energy consumption for compressors in this section is 15526 kW.
- the liquefied natural gas circulating in the conduit (13) enters the exchanger cryogenic E1 (see the simplified diagram in Figure 8) where it is sub-cooled and exits through line (14) at a temperature of -142.5 ° C. He is then expanded in the EX1 expansion turbine at a pressure of 0.65 MPa below which is still completely liquid at a temperature of -143.2 ° C and leaves this expansion turbine via line (15). Part of the fluid circulating in line (15) is sent by line (16) at this pressure to the cryogenic exchanger E1 in which it vaporizes.
- the rest of this fluid (referred to above as "the other party") is sent by line (18) in the V100 valve in which it is relaxed and then sent to the balloon B1 at a temperature of -144.9 ° C and a pressure of 0.26 MPa.
- a part of the liquid from balloon B1 is returned by line (19) in mixture with the vapor from the ball B1 and circulating in the line (18V) in the exchanger cryogenic E1 to be vaporized there.
- the other part of this liquid is sent by the line (21) in the exchanger E2 in which it is cooled before being expanded in valve V200 and sent to balloon B2 via line (22) at a pressure of 0.105 MPa and at a temperature of -157.6 ° C.
- Steam from of tank B2 via line (24) is sent back to exchanger E2: the flow of steam at the exit of the E2 exchanger (line 26 figure 8) is 544 kmoles at a temperature of -146.7 ° C.
- the liquefied natural gas leaves through line (23) at the bottom of the cylinder B2 with a flow rate of 4,985 kmole / h, i.e. approximately 50 mole percent of the input flow rate natural gas in the liquefaction unit with a molecular weight of 23.34, or by weight 116.35 tonnes / h.
- the gas vaporized at low pressure leaves the cryogenic exchanger E1 by the conduit (20) at a temperature of -66. ° C. It is sent through this conduit to balloon B3 where the non-vaporized fraction is separated and sent by line (20L) to balloon B4 by pump P3. Gas vaporized at higher pressure leaving the cryogenic exchanger E1 is sent to the balloon B4 by the conduit (17).
- the liquid (17L) separated in the tank B4 is pumped by the pump P4 and sent as a mixture with the fluid (13) to the inlet of the exchanger cryogenic E1.
- the vapor phases of balloons B3 and B4 (circulating respectively in lines 17V and 20V) are sent to the different compressor stages K1 to be compressed at a pressure of 1.5 MPa. There are 4315 Kmole / h at the outlet of compressor K1 in line (25), at a temperature of 22 ° C.
- Energy consumption for this sub-cooling section low temperature is 3820 kW for the K1 compressor, plus 108 kW for P3 and P4 pumps.
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Description
- Les figures 1 et 2 montrent les deux options du schéma de principe de l'unité suivant l'invention, la figure 2 figurant une option préférée.
- La figure 3 montre une possibilité pour réaliser la première étape de réfrigération
- La figure 4 montre une réalisation du procédé intégrant le fractionnement du gaz
- La figure 5 montre une variante du procédé permettant d'augmenter la récupération en composés C2+ dans la partie liquéfiée du fluide G.
- Les figures 6 à 8 seront décrites ci-après.
- par le conduit (54) du gaz combustible
- par le conduit (55), des condensats stabilisés contenant des pentanes, la totalité de l'hexane, du benzène et éventuellement des composés plus lourds,
- par le conduit (71) une coupe contenant principalement de l'éthane et par le conduit (74) une coupe contenant principalement du propane. Ces deux coupes sont utilisées comme appoint pour compenser les fuites du mélange réfrigérant M.
- par le conduit (53) on récupère le gaz à liquéfier purifié des composés lourds qui est renvoyé à la section de pré-réfrigération (R)
- par le conduit (56) un mélange, contenant principalement de l'éthane, du propane et des butanes, est envoyé à la section de pré-réfrigération (R2) pour être ultérieurement re-mélangé au gaz à liquéfier sortant de la section de pré-réfrigération (R).
- une fraction liquide après détente,
- une fraction gazeuse représentant au moins 10 % poids par rapport au poids du fluide G introduit initialement dans ledit procédé,
- et comportant au moins deux étapes de réfrigération au cours
desquelles :
- dans la première étape a) on refroidit le fluide G essentiellement gazeux à l'aide d'un réfrigérant externe M pour qu'à l'issue de cette première étape il soit au moins partiellement liquide à la pression opératoire et
- dans la deuxième étape b) on termine si nécessaire la liquéfaction dudit fluide G et on sous refroidit ledit fluide G, à l'aide d'une partie du même fluide G, ladite partie étant ainsi détendue et vaporisée de manière à produire le froid nécessaire pour récupérer l'autre partie dudit fluide G totalement liquide.
De préférence, le réfrigérant externe M comprend au moins un hydrocarbure et de préférence au moins deux hydrocarbures.
De manière plus préférée, le produit sortant en fond de la première colonne de fractionnement est réfrigéré dans la section de pré-réfrigération en se servant du réfrigérant externe M utilisé dans la première étape de pré-réfrigération, avant d'être détendu et envoyé en tête de la deuxième colonne de fractionnement.
Azote | 0,1 |
Méthane | 76,5 |
Éthane | 12,7 |
Propane | 7,8 |
IsoButane | 1,2 |
N-Butane | 1,0 |
IsoPentane | 0,25 |
N-Pentane | 0,15 |
C6+ | 0,3 |
Le gaz naturel G est alimenté par le conduit (10) à l'échangeur E13 dans lequel il est refroidi par un fluide intermédiaire (FI), jusqu'à une température de 19 °C puis est envoyé par le conduit (51) au sécheur (S) avant d'entrer par le conduit (52) dans la zone de fractionnement (F). Cette zone de fractionnement comporte habituellement au moins deux colonnes de fractionnement. Le fluide intermédiaire FI est mû par le système de circulation Cl, et refroidi dans la zone d'échange E10 de la section de pré-réfrigération (R).
Méthane | 1.9 |
Éthane | 46.5 |
Propane | 44.0 |
IsoButane | 4.9 |
N-Butane | 2.7 |
- 99 Kmoles/h de gaz combustible (sortant par le conduit 54 (figures 6 et 7)) en tête de la colonne T12 (figure 6) à une température de - 14°C, et à une pression de 3 MPa,
- 49 Kmoles/h (sortant par le conduit 55) de C5+ stabilisés en fond de la colonne T14 (figures 6 et 7)), et
- 9852 Kmoles/h sont envoyés vers l'échangeur E1 par le conduit (13) (le débit de liquide circulant dans le conduit 13 est égal à la somme des débits de fluides circulant dans les-conduits 12 et 57) sous forme totalement condensée à une température de -64.5 °C et à une pression de 5,58 MPa.
Claims (15)
- Procédé de liquéfaction partielle d'un fluide G formé au moins en partie d'hydrocarbures, dans lequel :a) on refroidit le fluide G par échange de chaleur avec un réfrigérant externe M pour liquéfier au moins partiellement le fluide G,b) on sous-refroidit le fluide G obtenu à l'étape a) par échange de chaleur avec une première fraction liquide de manière à obtenir un fluide G liquide sous-refroidi, la première fraction liquide étant vaporisée durant l'échange de chaleur pour former une fraction gazeuse,c) on détend ledit fluide G liquide sous-refroidi pour obtenir un fluide G liquide détendu,d) on sépare ledit fluide G liquide détendu pour obtenir ladite première fraction liquide et une deuxième fraction liquide, la fraction gazeuse représentant an moins 10% poids par rapport an poid du fluide G.
- Procédé de liquéfaction selon la revendication 1, dans lequel le fluide G est un gaz naturel et au moins une partie de ladite fraction gazeuse est réinjectée dans un puits à partir duquel on récupère ledit gaz naturel.
- Procédé de liquéfaction du fluide G selon l'une des revendications 1 ou 2, dans lequel la deuxième fraction liquide est détendue et partiellement vaporisée jusqu'à une pression du stockage.
- Procédé de liquéfaction selon l'une des revendications 1 à 3, dans lequel la première fraction liquide est vaporisée à différents niveaux de pression décroissants.
- Procédé de liquéfaction selon l'une des revendications 1 à 4, dans lequel la quantité de ladite deuxième fraction liquide obtenue est comprise entre 20 % et 80 % en poids de la quantité dudit fluide G à l'étape a).
- Procédé de liquéfaction selon l'une des revendications 1 à 5, dans lequel l'étape a) de réfrigération comporte plusieurs zones d'échange de chaleur et dans lequel lesdites zones d'échange de chaleur sont refroidies à l'aide du réfrigérant externe M qui est détendu et vaporisé à des niveaux de pression décroissants.
- Procédé de liquéfaction selon l'une des revendications 1 à 6, dans lequel le réfrigérant externe M comprend au moins un hydrocarbure et de préférence au moins deux hydrocarbures.
- Procédé de liquéfaction selon la revendication 7, dans lequel le réfrigérant externe M comprend au moins un hydrocarbure choisi dans le groupe formé par le méthane, l'éthane, le propane et les butanes.
- Procédé de liquéfaction selon l'une des revendications 7 et 8 dans lequel le réfrigérant externe M comprend du méthane, de l'éthane, du propane et au moins un butane.
- Procédé de liquéfaction selon l'une des revendications 1 à 9, dans lequel le fluide G au moins partiellement liquéfié à l'étape a) est monophasique condensé.
- Procédé de liquéfaction selon l'une des revendications 1 à 9, dans lequel le fluide G au moins partiellement liquéfié à l'étape a) est en phase dense.
- Procédé de liquéfaction d'un gaz naturel selon l'une des revendications 1 à 11, dans le fluide G est un gaz naturel et le fluide G au moins partiellement liquéfié à l'étape a) est à une température au moins inférieure à environ - 40°C.
- Procédé de liquéfaction d'un gaz naturel selon l'une des revendications 1 à 12, dans lequel la fraction gazeuse est comprimée, puis utilisée pour produire de l'électricité dans une turbine à gaz.
- Procédé de liquéfaction selon l'une des revendications 1 à 13, dans lequel avant l'étape b), ledit fluide G au moins partiellement liquéfié à l'étape a) est séché et fractionné dans au moins deux colonnes de fractionnement.
- Procédé de liquéfaction selon la revendication 14 dans lequel le produit sortant en fond de la première colonne de fractionnement est réfrigéré par échange de chaleur avec le réfrigérant externe M, puis est détendu et envoyé en tête de la deuxième colonne de fractionnement.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0000737A FR2803851B1 (fr) | 2000-01-19 | 2000-01-19 | Procede de liquefaction partielle d'un fluide contenant des hydrocarbures tel que du gaz naturel |
FR0000737 | 2000-01-19 |
Publications (2)
Publication Number | Publication Date |
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EP1118827A1 EP1118827A1 (fr) | 2001-07-25 |
EP1118827B1 true EP1118827B1 (fr) | 2004-10-20 |
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ID=8846136
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Application Number | Title | Priority Date | Filing Date |
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EP01400050A Expired - Lifetime EP1118827B1 (fr) | 2000-01-19 | 2001-01-10 | Procédé de liquéfaction partielle d'un fluide contenant des hydrocarbures tel que du gaz naturel |
Country Status (6)
Country | Link |
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US (1) | US6449982B1 (fr) |
EP (1) | EP1118827B1 (fr) |
JP (1) | JP4898006B2 (fr) |
DE (1) | DE60106499D1 (fr) |
ES (1) | ES2232571T3 (fr) |
FR (1) | FR2803851B1 (fr) |
Families Citing this family (23)
Publication number | Priority date | Publication date | Assignee | Title |
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US6581409B2 (en) * | 2001-05-04 | 2003-06-24 | Bechtel Bwxt Idaho, Llc | Apparatus for the liquefaction of natural gas and methods related to same |
GB0120272D0 (en) * | 2001-08-21 | 2001-10-10 | Gasconsult Ltd | Improved process for liquefaction of natural gases |
FR2841330B1 (fr) * | 2002-06-21 | 2005-01-28 | Inst Francais Du Petrole | Liquefaction de gaz naturel avec recyclage de gaz naturel |
US7866184B2 (en) | 2004-06-16 | 2011-01-11 | Conocophillips Company | Semi-closed loop LNG process |
CA2681417C (fr) * | 2007-05-03 | 2016-07-26 | Exxonmobil Upstream Research Company | Processus de liquefaction de gaz naturel |
FR2923000B1 (fr) * | 2007-10-26 | 2015-12-11 | Inst Francais Du Petrole | Procede de liquefaction d'un gaz naturel avec recuperation amelioree de propane. |
US8020406B2 (en) * | 2007-11-05 | 2011-09-20 | David Vandor | Method and system for the small-scale production of liquified natural gas (LNG) from low-pressure gas |
US9243842B2 (en) | 2008-02-15 | 2016-01-26 | Black & Veatch Corporation | Combined synthesis gas separation and LNG production method and system |
US8464551B2 (en) | 2008-11-18 | 2013-06-18 | Air Products And Chemicals, Inc. | Liquefaction method and system |
DK2365852T3 (da) * | 2009-07-13 | 2022-07-18 | Dexpro Corp | Fremgangsmåde til fjernelse af kondenserbare bestanddele fra et fluid |
KR20120081602A (ko) * | 2009-09-30 | 2012-07-19 | 쉘 인터내셔날 리써취 마트샤피지 비.브이. | 탄화수소 스트림을 분별증류하는 방법 및 그 장치 |
US9441877B2 (en) | 2010-03-17 | 2016-09-13 | Chart Inc. | Integrated pre-cooled mixed refrigerant system and method |
US10113127B2 (en) | 2010-04-16 | 2018-10-30 | Black & Veatch Holding Company | Process for separating nitrogen from a natural gas stream with nitrogen stripping in the production of liquefied natural gas |
WO2012075266A2 (fr) | 2010-12-01 | 2012-06-07 | Black & Veatch Corporation | Récupération de ngl à partir de gaz naturel à l'aide d'un mélange de réfrigérants |
US10139157B2 (en) | 2012-02-22 | 2018-11-27 | Black & Veatch Holding Company | NGL recovery from natural gas using a mixed refrigerant |
US11428463B2 (en) | 2013-03-15 | 2022-08-30 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
CA2907444C (fr) | 2013-03-15 | 2022-01-18 | Douglas A. Ducote, Jr. | Procede et systeme refrigerant mixte |
US11408673B2 (en) | 2013-03-15 | 2022-08-09 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
US10563913B2 (en) | 2013-11-15 | 2020-02-18 | Black & Veatch Holding Company | Systems and methods for hydrocarbon refrigeration with a mixed refrigerant cycle |
US9574822B2 (en) | 2014-03-17 | 2017-02-21 | Black & Veatch Corporation | Liquefied natural gas facility employing an optimized mixed refrigerant system |
AR105277A1 (es) | 2015-07-08 | 2017-09-20 | Chart Energy & Chemicals Inc | Sistema y método de refrigeración mixta |
FR3039080B1 (fr) * | 2015-07-23 | 2019-05-17 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Methode de purification d'un gaz riche en hydrocarbures |
CN105758113A (zh) * | 2016-03-04 | 2016-07-13 | 浙江大学常州工业技术研究院 | 一种波动入口换热***及其方法 |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
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US3690114A (en) * | 1969-11-17 | 1972-09-12 | Judson S Swearingen | Refrigeration process for use in liquefication of gases |
US4195979A (en) * | 1978-05-12 | 1980-04-01 | Phillips Petroleum Company | Liquefaction of high pressure gas |
JPH06159928A (ja) * | 1992-11-20 | 1994-06-07 | Chiyoda Corp | 天然ガス液化方法 |
FR2743140B1 (fr) * | 1995-12-28 | 1998-01-23 | Inst Francais Du Petrole | Procede et dispositif de liquefaction en deux etapes d'un melange gazeux tel qu'un gaz naturel |
US6196021B1 (en) * | 1999-03-23 | 2001-03-06 | Robert Wissolik | Industrial gas pipeline letdown liquefaction system |
-
2000
- 2000-01-19 FR FR0000737A patent/FR2803851B1/fr not_active Expired - Lifetime
-
2001
- 2001-01-10 EP EP01400050A patent/EP1118827B1/fr not_active Expired - Lifetime
- 2001-01-10 ES ES01400050T patent/ES2232571T3/es not_active Expired - Lifetime
- 2001-01-10 DE DE60106499T patent/DE60106499D1/de not_active Expired - Lifetime
- 2001-01-19 US US09/764,438 patent/US6449982B1/en not_active Expired - Lifetime
- 2001-01-19 JP JP2001011715A patent/JP4898006B2/ja not_active Expired - Lifetime
Also Published As
Publication number | Publication date |
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EP1118827A1 (fr) | 2001-07-25 |
DE60106499D1 (de) | 2004-11-25 |
JP4898006B2 (ja) | 2012-03-14 |
FR2803851B1 (fr) | 2006-09-29 |
JP2001226685A (ja) | 2001-08-21 |
FR2803851A1 (fr) | 2001-07-20 |
ES2232571T3 (es) | 2005-06-01 |
US6449982B1 (en) | 2002-09-17 |
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