EP1828697A1 - Procede et installation de production de gaz naturel traite , d ' une coupe riche en hydrocarbures en c3 + et courant riche en ethane - Google Patents
Procede et installation de production de gaz naturel traite , d ' une coupe riche en hydrocarbures en c3 + et courant riche en ethaneInfo
- Publication number
- EP1828697A1 EP1828697A1 EP05850537A EP05850537A EP1828697A1 EP 1828697 A1 EP1828697 A1 EP 1828697A1 EP 05850537 A EP05850537 A EP 05850537A EP 05850537 A EP05850537 A EP 05850537A EP 1828697 A1 EP1828697 A1 EP 1828697A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- stream
- column
- reflux
- ethane
- rich
- 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
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 140
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 53
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 51
- 239000003345 natural gas Substances 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 30
- 238000009434 installation Methods 0.000 title claims abstract description 20
- 239000004215 Carbon black (E152) Substances 0.000 title claims description 21
- 238000010992 reflux Methods 0.000 claims abstract description 75
- 239000007789 gas Substances 0.000 claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 23
- 238000000605 extraction Methods 0.000 claims abstract description 19
- 238000001816 cooling Methods 0.000 claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 claims abstract description 16
- 238000009833 condensation Methods 0.000 claims abstract description 4
- 230000005494 condensation Effects 0.000 claims abstract description 4
- 238000011084 recovery Methods 0.000 claims description 50
- 238000005194 fractionation Methods 0.000 claims description 37
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 22
- 239000001294 propane Substances 0.000 claims description 11
- 239000000203 mixture Substances 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 2
- SNOOUWRIMMFWNE-UHFFFAOYSA-M sodium;6-[(3,4,5-trimethoxybenzoyl)amino]hexanoate Chemical compound [Na+].COC1=CC(C(=O)NCCCCCC([O-])=O)=CC(OC)=C1OC SNOOUWRIMMFWNE-UHFFFAOYSA-M 0.000 abstract description 16
- 238000000926 separation method Methods 0.000 abstract description 3
- 238000007865 diluting Methods 0.000 abstract 2
- 238000010079 rubber tapping Methods 0.000 abstract 2
- 238000010790 dilution Methods 0.000 abstract 1
- 239000012895 dilution Substances 0.000 abstract 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 12
- 229910002092 carbon dioxide Inorganic materials 0.000 description 6
- 239000001569 carbon dioxide Substances 0.000 description 6
- 239000003507 refrigerant Substances 0.000 description 4
- 239000000470 constituent Substances 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 238000003303 reheating Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- -1 C 3 hydrocarbons Chemical class 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000003949 liquefied natural gas Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/62—Ethane or ethylene
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
- F25J2260/02—Integration in an installation for exchanging heat, e.g. for waste heat recovery
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
- F25J2260/20—Integration in an installation for liquefying or solidifying a fluid stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2280/00—Control of the process or apparatus
- F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/12—Particular process parameters like pressure, temperature, ratios
Definitions
- the present invention relates to a process for the simultaneous production of treated natural gas, a C 3 + hydrocarbon-rich fraction and, in at least some production conditions, an ethane-rich stream, from a natural gas.
- starting material comprising methane, ethane and C 3 + hydrocarbons, the process comprising the following steps:
- the cooled natural gas is separated into a liquid stream and a gaseous stream; the liquid stream is expanded and introduced into a C 1 hydrocarbon recovery column at a first intermediate level;
- the gas stream is separated into a supply stream of said column and a reflux stream;
- the supply stream is expanded in a turbine and then introduced into the column at a second intermediate level;
- the reflux stream is cooled and at least partially condensed and, after expansion, introduced into the column at a third intermediate level
- said foot stream is introduced at a feed level of a fractionation column provided with an overhead condenser, the fractionation column producing the ethane-rich stream at its head and the hydrocarbon cutting at the bottom; in C 3 + ;
- a primary reflux stream produced in the reflux condenser is introduced into the fractionation column.
- the process of the present invention is applicable to plants intended to produce, from a natural gas extracted from the subsoil, a treated natural gas, possibly intended to be liquefied, a C 3 + hydrocarbon fraction, and a stream rich in ethane of variable flow.
- the process of the aforementioned type is optimized to simultaneously extract substantially all the C 3 + hydrocarbons in the starting natural gas, and a high proportion of ethane from the starting gas.
- the propane extraction rate is close to 99%.
- extraction rate refers to the ratio of the difference between the molar flow rate of a constituent in the starting natural gas and the molar flow rate of the constituent in the treated natural gas produced at the molar flow rate. constituent in the starting natural gas.
- the aforementioned article proposes to install in the existing plant, a secondary unit optimized for the production of C 3 + hydrocarbons when the extraction of ethane is low or nothing.
- the plant operator then selectively sends, depending on the amount of ethane required, the starting natural gas in the unit optimized for high ethane extraction rates or in the optimized unit for rates. low or zero ethane extraction.
- the method is therefore complex to implement and expensive, in particular because of the maintenance costs of the installation in which it is implemented.
- An object of the invention is to provide a method of the aforementioned type, which allows by simple and inexpensive means to substantially extract the all of the C 3 + hydrocarbons of a starting natural gas stream, regardless of the amount of ethane produced by the process.
- the subject of the invention is a process of the aforementioned type, characterized in that the ethane-rich stream is withdrawn from an intermediate level of the fractionation column situated above said feed level of the feedstock. this column; and in that, for ethane extraction rates below a predetermined threshold, at least one secondary reflux stream is produced from said overhead condenser and said secondary reflux stream at the top of the head is refluxed. the recovery column.
- the process according to the invention may comprise one or more of the following characteristics, taken separately or according to all the possible combinations:
- the flow rate of the ethane rich stream is controlled by adjusting the flow rate of the secondary reflux stream and adjusting the pressure of the recovery column;
- the fractionation column comprises between 1 and 7 theoretical plates above said intermediate level
- the secondary reflux stream is cooled by heat exchange with at least a first portion of the overhead stream of the recovery column;
- the reflux stream of the recovery column is cooled by heat exchange with at least a second portion of the overhead stream of the recovery column;
- the secondary reflux stream is produced from a mixture of a stream of gas and a stream of liquid from the overhead condenser;
- the invention further relates to a plant for simultaneous production of treated natural gas and a hydrocarbon rich cut in CV " and, in at least some conditions of production of a stream rich in ethane, from a starting natural gas comprising methane, ethane and C 3 + hydrocarbons, the plant comprising:
- a fractionation column provided with a head condenser; means for introducing said foot stream to a feed level of the fractionation column;
- the means for recovering an ethane-rich stream are stitched at an intermediate level of the fractionation column located above said feed level of said column; and in that the plant comprises means for producing, for ethane extraction rates of the starting natural gas lower than a predetermined threshold, a secondary reflux stream from the overhead condenser, and means for producing introducing this refluxing secondary reflux stream into the recovery column.
- the installation according to the invention may comprise one or more of the following characteristics, taken separately or in any technically possible combination:
- means for controlling the flow rate of the ethane-rich stream comprising means for adjusting the flow rate of the secondary reflux flow and means for adjusting the pressure in the recovery column;
- the fractionation column comprises between 1 and 7 theoretical plates above said intermediate level
- the means for producing the secondary reflux flow comprise means for mixing a stream of gas and a stream of liquid coming from the overhead condenser; and it comprises means for controlling the maximum content of methane and propane in the ethane-rich stream comprising a bottom reboiler mounted on the recovery column.
- the installation 11 shown in the Figure is intended for the simultaneous production, from a source 13 of natural gas, desulfurized, dry, and at least partially decarbonated, a natural gas treated as the main product, d a C- 3 + hydrocarbon fraction 17, and a stream 19 rich in ethane, adjustable flow.
- At least partially decarbonated means that the carbon dioxide content in the starting gas 13 is advantageously less than or equal to 50 ppm when the treated natural gas is to be liquefied. This content is advantageously less than 3% when the treated natural gas is sent directly to a gas distribution network.
- This installation 11 comprises a unit 21 for recovering C 2 + hydrocarbons, and a unit 23 for fractionating these C 2 + hydrocarbons.
- a unit 21 for recovering C 2 + hydrocarbons and a unit 23 for fractionating these C 2 + hydrocarbons.
- the pressures considered are absolute pressures
- the percentages considered are molar percentages.
- the unit 21 for recovering C 2 + hydrocarbons successively comprises, downstream of the source 13, a first heat exchanger 25, a first separator tank 27, a turbine 29 coupled to a first compressor 31, a first exchanger 33, and a recovery column 35 having an upper side reboiler 37, a lower side reboiler 39 and a bottom reboiler 41.
- the unit 21 further comprises a second compressor 43 driven by an external energy source and a first refrigerant 45.
- the unit 21 also comprises a pump 47 of the bottom of the column.
- the fractionation unit 23 comprises a fractionation column 61.
- the column 61 comprises at the head a top condenser 63, and at the bottom a reboiler 65.
- the overhead condenser 63 comprises a second refrigerant 67 and a second separator tank 69 associated with a reflux pump 71 and a second head exchanger 73 of the column 35.
- the starting gas 13 is separated into a main stream 101 and a secondary stream 103.
- the ratio of the flow rate of the secondary stream 103 to the flow rate of the starting gas 13 is for example between 20% and 40%.
- the main stream 101 is cooled in the first heat exchanger 25 to form a cooled gas stream 105.
- the secondary stream 103 is successively cooled in heat exchangers respective lower and upper side reboilers 37, 109, 109, to form a cooled secondary stream 111 which is mixed with the cooled main stream 105.
- the mixture 113 obtained is introduced into the separator tank 27 in which a separation between a gaseous phase 115 and a liquid phase 117 takes place.
- the liquid phase 117 forms, after passing through an expansion valve 119, a relaxed liquid phase 120 which is introduced at a first intermediate level N1 of the recovery column 35 situated in the upper region of the column, above the lateral reboilers 37 and 39.
- intermediate level is meant a location comprising distillation means, above and below this level.
- the gaseous fraction 115 is separated into a feed stream 121 and a reflux stream 123.
- the feed stream 121 is expanded in the turbine 29 to provide a relaxed feed stream 125, which is fed into the recovery column At a second intermediate level N2, located above the first intermediate level N1.
- the reflux stream 123 is partially condensed in the first head exchanger 33, and then expanded in an expansion valve 127, to form a relaxed reflux stream 128.
- This stream 128 is introduced into the recovery column 35 at a third intermediate level. N3, located above the intermediate level N2.
- the pressure of the recovery column 35 is for example between 15 and 40 bar.
- the recovery column 35 produces a top stream 131 which is separated into a major fraction 133 and a minor fraction 135.
- the major fraction 133 is reheated in the first head exchanger 33 by heat exchange with the reflux stream 123 to form a major fraction heated up 137.
- the ratio of the flow of the minority fraction 135 to the majority fraction 133 is for example less than 20%.
- the minor fraction 135 is reheated in the second head exchanger 73 to form a heated fraction 136.
- This fraction 136 is mixed with the heated majority fraction 137 to form a heated treated gas stream 139.
- This stream 139 is reheated in the first heat exchanger 25 by heat exchange with the main stream 101 of the pretreated natural gas.
- the warmed treated natural gas 139 is then compressed in the first compressor 31, then in the second compressor 43, and cooled in the first refrigerant 45 to form the treated natural gas 15.
- the treated gas contains 0.0755 mol% of hydrogen, 0.0049% of carbon dioxide, 1.2735 mol% of nitrogen, 90.8511 mol% of methane, 7.7717 mol% of hydrocarbons in Cs , 0.0232 mol% of C 3 hydrocarbons and a C 4 hydrocarbon content of less than 1 ppm.
- This treated gas comprises a content of hydrocarbons in Ce * of less than 1 ppm, a water content of less than 1 ppm, advantageously less than 0.1 ppm, a sulfur dioxide content of less than 4 ppm, and a carbon dioxide content of carbon less than 50 ppm.
- the treated gas can thus be sent directly to a liquefaction train to produce liquefied natural gas.
- Reboiler streams 163, 161 are withdrawn from the column 35 and are reintroduced into the column 35 after reheating in the respective exchangers 109, 107 of the upper and lower reboilers 37 and 39, by heat exchange with the minority current 111 of the natural gas. 'Entrance.
- a bottom reboiler stream 165 is withdrawn in the vicinity of the bottom of the column 35. This stream 165 passes into a bottom heat exchanger 167 in which it is reheated by heat exchange with an adjustable temperature reheating stream 169. The heated reboiler stream is then reintroduced into the column 35.
- a bottom stream 171 rich in C 2 + hydrocarbons is extracted from the bottom of the fractionation column 35 to form a C 2 + hydrocarbon fraction.
- the bottom stream 171 is pumped by the bottom pump 47 and introduced at an intermediate level P1 of the fractionation column 61.
- the fractionation column 61 operates a pressure of between 20 and 42 bar.
- the pressure of the fractionation column 61 is at least 1 bar higher than the pressure of the recovery column 35.
- a bottom stream 181 is removed from the fractionation column 61 to form the C 3 + hydrocarbon section 17.
- the extraction rate of C 3 + hydrocarbons in the process is greater than 99%. In all cases, the propane extraction rate is greater than 99% and the C / hydrocarbons extraction rate is greater than 99.8%.
- the molar ratio of ethane to propane in section 17 is less than 2% and in particular substantially equal to 0.5%.
- the ethane-rich stream 19 is withdrawn directly at an intermediate level P2 located in the upper region of the fractionation column 61.
- This stream comprises 0.57% methane, 97.4% ethane, 2% propane and 108 ppm carbon dioxide.
- the number of theoretical plates between the head of the column 61 and the upper level P2 is for example between 1 and 7.
- the level P2 is greater than the supply level P1.
- the content of methane and propane in the bottom stream 171, and thus in the stream 19, is regulated in particular by the temperature of the reheating current 169 of the bottom reboiler.
- These grades are. preferably less than 1% and 2% respectively.
- a head stream 183 is withdrawn from the top of the column 61 and then cooled in the second cooler 67 to form a top stream 185 at least partially cooled and condensed.
- This stream 185 is introduced into the second separator tank 69 to produce a liquid fraction 187.
- the liquid fraction 187 is then separated into a primary reflux stream 189 and a secondary reflux stream 191.
- the primary reflux stream 189 is pumped to be introduced as reflux in the fractionation column 35, at a head level P3 located at above the P2 level.
- the secondary reflux stream 191 is introduced into the second head exchanger 73, where it is cooled by heat exchange with the stream 135 and then expanded in a valve 193 and introduced into reflux at the N4 head level of the recovery column 35.
- stream 191 contains 1.64% methane, 97.75% ethane, 0.59% propane and 216 ppm carbon dioxide.
- the ethane extraction rate, and consequently the ethane flow rate produced in the installation 11, is controlled by regulating the flow rate of the secondary reflux stream 191 flowing through the expansion valve 193, on the one hand, and by adjusting the pressure in the recovery column 35, using the compressors 43 and 31 which are of the variable speed type, on the other hand.
- the flow rate of the ethane rich stream is adjustable, virtually without affecting the C 3 + hydrocarbon removal rate.
- the method according to the invention thus makes it possible, by simple and inexpensive means, to obtain a variable and easily adjustable flow rate of a stream rich in ethane 19 extracted from the starting natural gas 13, while maintaining the extraction rate of propane greater than 99%. This result is obtained without significant modification of the installation in which the process is carried out.
- composition of the secondary reflux stream 191, richer in methane than the ethane stream 19 withdrawn from the fractionation column 61, makes it possible to obtain this result.
- the recoveries of frigories within the heat exchangers 107, 109 of the lateral reboilers 37, 39 of the recovery column 35 adapt autonomously, without the need to drive the flow rates of fluid passing through these exchangers, regardless of the flow rate of the ethane-rich stream 19 produced.
- the installation 11 according to the invention also does not require imperative use of multiflux exchangers. It is thus possible to use only tube and shell exchangers, which increase the reliability of the installation and reduce the risk of clogging.
- the treated natural gas comprises substantially zero levels of C 5 + hydrocarbons, for example less than 1 ppm. As a result, if the carbon dioxide content in the treated gas is less than 50 ppm, this gas can be liquefied without further treatment or fractionation.
- the top stream 183 of the fractionation column is not totally condensed in the refrigerant 67.
- the gas stream 201 coming from the separator drum 69 is then mixed with the secondary reflux stream. 191, before passing through the second head exchanger 73.
- the pressure in the recovery column 35 is greater than the pressure in the fractionation column 61.
- the bottom stream 171 of the recovery column 35 is fed to the fractionation column 61 through an expansion valve.
- the secondary reflux stream 191 is then pumped to the top of the recovery column 35.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Chemical & Material Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Catalysts (AREA)
- Gas Separation By Absorption (AREA)
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PL05850537T PL1828697T3 (pl) | 2004-12-22 | 2005-12-19 | Sposób i instalacja do wytwarzania oczyszczonego gazu ziemnego, frakcji bogatej w węglowodory C3+ i strumienia bogatego w tlen |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0413751A FR2879729B1 (fr) | 2004-12-22 | 2004-12-22 | Procede et installation de production de gaz traite, d'une coupe riche en hydrocarbures en c3+ et d'un courant riche en ethane |
PCT/FR2005/003186 WO2006070097A1 (fr) | 2004-12-22 | 2005-12-19 | Procede et installation de production de gaz naturel traite , d ' une coupe riche en hydrocarbures en c3 + et courant riche en ethane |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1828697A1 true EP1828697A1 (fr) | 2007-09-05 |
EP1828697B1 EP1828697B1 (fr) | 2008-12-03 |
Family
ID=34953803
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP05850537A Active EP1828697B1 (fr) | 2004-12-22 | 2005-12-19 | Procede et installation de production de gaz naturel traite , d ' une coupe riche en hydrocarbures en c3 + et courant riche en ethane |
Country Status (18)
Country | Link |
---|---|
US (1) | US7458232B2 (fr) |
EP (1) | EP1828697B1 (fr) |
CN (1) | CN100547326C (fr) |
AT (1) | ATE416352T1 (fr) |
AU (1) | AU2005321162B2 (fr) |
BR (1) | BRPI0519380B1 (fr) |
CA (1) | CA2592012C (fr) |
DE (1) | DE602005011482D1 (fr) |
DK (1) | DK1828697T3 (fr) |
EA (1) | EA010386B1 (fr) |
EG (1) | EG24056A (fr) |
ES (1) | ES2318587T3 (fr) |
FR (1) | FR2879729B1 (fr) |
MX (1) | MX2007007351A (fr) |
MY (1) | MY145312A (fr) |
PL (1) | PL1828697T3 (fr) |
PT (1) | PT1828697E (fr) |
WO (1) | WO2006070097A1 (fr) |
Families Citing this family (16)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2923001B1 (fr) * | 2007-10-26 | 2015-12-11 | Inst Francais Du Petrole | Procede de liquefaction d'un gaz naturel avec fractionnement a haute pression. |
FR2923000B1 (fr) * | 2007-10-26 | 2015-12-11 | Inst Francais Du Petrole | Procede de liquefaction d'un gaz naturel avec recuperation amelioree de propane. |
CN101614464B (zh) * | 2008-06-23 | 2011-07-06 | 杭州福斯达实业集团有限公司 | 高低温氮气双膨胀天然气液化方法 |
EP2350546A1 (fr) * | 2008-10-07 | 2011-08-03 | Exxonmobil Upstream Research Company | Récupération de l hélium dans le gaz naturel intégrée à la récupération du lgn |
FR2943683B1 (fr) * | 2009-03-25 | 2012-12-14 | Technip France | Procede de traitement d'un gaz naturel de charge pour obtenir un gaz naturel traite et une coupe d'hydrocarbures en c5+, et installation associee |
FR2970258B1 (fr) * | 2011-01-06 | 2014-02-07 | Technip France | Procede de production d'une coupe riche en hydrocarbures en c3+ et d'un courant riche en methane et ethane a partir d'un courant d'alimentation riche en hydrocarbures et installation associee. |
CN102603457B (zh) * | 2012-01-17 | 2014-01-08 | 马俊杰 | C3、c4生成丙烯的液化气深加工的生产装置及工艺 |
FR2992972B1 (fr) * | 2012-07-05 | 2014-08-15 | Technip France | Procede de production d'un gaz naturel traite, d'une coupe riche en hydrocarbures en c3+, et eventuellement d'un courant riche en ethane, et installation associee |
US9726426B2 (en) * | 2012-07-11 | 2017-08-08 | Butts Properties, Ltd. | System and method for removing excess nitrogen from gas subcooled expander operations |
CA2895257C (fr) * | 2012-12-28 | 2022-06-21 | Linde Process Plants, Inc. | Procede integre de lgn (recuperation de liquides du gaz naturel) et de gnl (liquefaction du gaz naturel) |
FR3007408B1 (fr) * | 2013-06-25 | 2015-07-31 | Technip France | Procede de recuperation d'un courant d'ethylene a partir d'un courant de charge riche en monoxyde de carbone, et installation associee |
US11402155B2 (en) * | 2016-09-06 | 2022-08-02 | Lummus Technology Inc. | Pretreatment of natural gas prior to liquefaction |
FR3072162B1 (fr) * | 2017-10-10 | 2020-06-19 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | <P>PROCEDE DE RECUPERATION DE PROPANE ET D'UNE QUANTITE AJUSTABLE D'ETHANE A PARTIR DE GAZ NATUREL</P> |
US11015865B2 (en) | 2018-08-27 | 2021-05-25 | Bcck Holding Company | System and method for natural gas liquid production with flexible ethane recovery or rejection |
US11378333B2 (en) * | 2019-12-13 | 2022-07-05 | Bcck Holding Company | System and method for separating methane and nitrogen with reduced horsepower demands |
CN113899161B (zh) * | 2021-10-12 | 2023-04-18 | 中石化石油工程技术服务有限公司 | 一种从天然气中提取乙烷的方法 |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1551609A1 (de) * | 1967-12-15 | 1972-03-02 | Messer Griesheim Gmbh | Verfahren zur Zerlegung von fluessigem Erdgas |
FR2458525A1 (fr) * | 1979-06-06 | 1981-01-02 | Technip Cie | Procede perfectionne de fabrication de l'ethylene et installation de production d'ethylene comportant application de ce procede |
US4529484A (en) * | 1982-01-29 | 1985-07-16 | Phillips Petroleum Company | Fractional distillation column control |
US6116050A (en) * | 1998-12-04 | 2000-09-12 | Ipsi Llc | Propane recovery methods |
FR2796858B1 (fr) * | 1999-07-28 | 2002-05-31 | Technip Cie | Procede et installation de purification d'un gaz et produits ainsi obtenus |
US6516631B1 (en) * | 2001-08-10 | 2003-02-11 | Mark A. Trebble | Hydrocarbon gas processing |
EP1508010B1 (fr) * | 2002-05-20 | 2008-01-09 | Fluor Corporation | Procede a deux reflux et configurations de recuperation de liquides gazeux naturels |
US7051553B2 (en) * | 2002-05-20 | 2006-05-30 | Floor Technologies Corporation | Twin reflux process and configurations for improved natural gas liquids recovery |
-
2004
- 2004-12-22 FR FR0413751A patent/FR2879729B1/fr not_active Expired - Fee Related
-
2005
- 2005-12-19 CN CNB200580047003XA patent/CN100547326C/zh active Active
- 2005-12-19 AT AT05850537T patent/ATE416352T1/de active
- 2005-12-19 DE DE602005011482T patent/DE602005011482D1/de active Active
- 2005-12-19 PL PL05850537T patent/PL1828697T3/pl unknown
- 2005-12-19 EP EP05850537A patent/EP1828697B1/fr active Active
- 2005-12-19 MX MX2007007351A patent/MX2007007351A/es active IP Right Grant
- 2005-12-19 WO PCT/FR2005/003186 patent/WO2006070097A1/fr active Application Filing
- 2005-12-19 AU AU2005321162A patent/AU2005321162B2/en active Active
- 2005-12-19 ES ES05850537T patent/ES2318587T3/es active Active
- 2005-12-19 BR BRPI0519380-0A patent/BRPI0519380B1/pt active IP Right Grant
- 2005-12-19 EA EA200701340A patent/EA010386B1/ru not_active IP Right Cessation
- 2005-12-19 CA CA2592012A patent/CA2592012C/fr active Active
- 2005-12-19 PT PT05850537T patent/PT1828697E/pt unknown
- 2005-12-19 DK DK05850537T patent/DK1828697T3/da active
- 2005-12-21 US US11/316,083 patent/US7458232B2/en active Active
- 2005-12-21 EG EG2005120536A patent/EG24056A/xx active
- 2005-12-21 MY MYPI20056083A patent/MY145312A/en unknown
Non-Patent Citations (1)
Title |
---|
See references of WO2006070097A1 * |
Also Published As
Publication number | Publication date |
---|---|
EG24056A (en) | 2008-04-30 |
CN100547326C (zh) | 2009-10-07 |
CN101103239A (zh) | 2008-01-09 |
CA2592012A1 (fr) | 2006-07-06 |
DK1828697T3 (da) | 2009-03-09 |
BRPI0519380A2 (pt) | 2009-01-20 |
WO2006070097A1 (fr) | 2006-07-06 |
AU2005321162A1 (en) | 2006-07-06 |
PL1828697T3 (pl) | 2009-06-30 |
CA2592012C (fr) | 2013-10-15 |
ATE416352T1 (de) | 2008-12-15 |
FR2879729A1 (fr) | 2006-06-23 |
US7458232B2 (en) | 2008-12-02 |
ES2318587T3 (es) | 2009-05-01 |
EA010386B1 (ru) | 2008-08-29 |
DE602005011482D1 (de) | 2009-01-15 |
MX2007007351A (es) | 2007-08-14 |
BRPI0519380B1 (pt) | 2018-03-06 |
EA200701340A1 (ru) | 2007-10-26 |
US20060144081A1 (en) | 2006-07-06 |
EP1828697B1 (fr) | 2008-12-03 |
MY145312A (en) | 2012-01-13 |
PT1828697E (pt) | 2009-02-12 |
AU2005321162B2 (en) | 2010-07-15 |
FR2879729B1 (fr) | 2008-11-21 |
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