EP1828697B1 - Verfahren und installation zur herstellung von behandeltem erdgas aus einem kohlenwasserstoffreichen c3+-schnitt und einem ethanreichen strom - Google Patents

Verfahren und installation zur herstellung von behandeltem erdgas aus einem kohlenwasserstoffreichen c3+-schnitt und einem ethanreichen strom Download PDF

Info

Publication number
EP1828697B1
EP1828697B1 EP05850537A EP05850537A EP1828697B1 EP 1828697 B1 EP1828697 B1 EP 1828697B1 EP 05850537 A EP05850537 A EP 05850537A EP 05850537 A EP05850537 A EP 05850537A EP 1828697 B1 EP1828697 B1 EP 1828697B1
Authority
EP
European Patent Office
Prior art keywords
current
column
stream
reflux
ethane
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.)
Active
Application number
EP05850537A
Other languages
English (en)
French (fr)
Other versions
EP1828697A1 (de
Inventor
Henri Paradowski
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Technip Energies France SAS
Original Assignee
Technip France SAS
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Technip France SAS filed Critical Technip France SAS
Priority to PL05850537T priority Critical patent/PL1828697T3/pl
Publication of EP1828697A1 publication Critical patent/EP1828697A1/de
Application granted granted Critical
Publication of EP1828697B1 publication Critical patent/EP1828697B1/de
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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 according to the preamble of claim 1.
  • 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 method according to claim 1.
  • the method according to the invention may comprise one or more of the features which are the subject of claims 2 to 8.
  • the invention further relates to an installation according to claim 9.
  • the installation according to the invention may comprise one or more of the features which are the subject of claims 10 to 15.
  • 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 section 17 of C 3 + hydrocarbons, 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.
  • 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 heat exchanger 33, and a recovery column 35 provided with 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 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% hydrogen, 0.0049% carbon dioxide, 1.2735 mol% nitrogen, 90.8511 mol% methane, 7.7717 mol% C hydrocarbons. 2 , 0.0232 mol% of C 3 hydrocarbons and a C 4 hydrocarbon content of less than 1 ppm.
  • This treated gas comprises a C 6 + hydrocarbon content 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 content of dioxide. less than 50 ppm carbon.
  • 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 4 + hydrocarbon 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 contents 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 above the level P2.
  • 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 at reflux at the head N4 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 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 implemented.
  • 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, and regardless of the flow rates 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.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • General Engineering & Computer Science (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Gas Separation By Absorption (AREA)
  • Catalysts (AREA)

Claims (15)

  1. Verfahren für die gleichzeitige Produktion von behandeltem Erdgas (15), einem Schnitt (17), der reich an C3 +-Kohlenwasserstoffen ist, und, zumindest unter bestimmten Produktionsbedingungen, eines Stroms (19), der reich an Ethan ist, ausgehend von einem Ausgangs-Erdgas (13), das Methan, Ethan und C3 +-Kohlenwasserstoffe aufweist,
    wobei das Verfahren die folgenden Schritte aufweist:
    - Abkühlen und teilweise Kondensieren des Ausgangs-Erdgases (13),
    - Trennen des abgekühlten Erdgases (113) in einen flüssigen Strom (117) und einen gasförmigen Strom (115),
    - Entspannen und Einführen des flüssigen Stroms (117) in eine Kolonne (35) zur Wiedergewinnung der C2 +-Kohlenwasserstoffe auf einer ersten Zwischenebene (N1),
    - Trennen des gasförmigen Stroms (115) in einen Einspeisungsstrom der Kolonne (121) und einen Rückfluss-Strom (123),
    - Entspannen des Einspeisungsstroms (121) in einer Turbine (29) und anschließend Einführen desselben in die Kolonne (35) auf einer zweiten Zwischenebene (N2),
    - Abkühlen und zumindest teilweise Kondensieren des Rückfluss-Stroms (123) und, nach dem Entspannen, Einführen desselben in die Kolonne (35) auf einer dritten Zwischenebene (N3),
    - Wiedergewinnen des Kopfstroms (131) der Kolonne, um das behandelte Erdgas (15) zu bilden, und Wiedergewinnen des Sumpfstroms (171) der Kolonne (35), um einen flüssigen Strom zu bilden, der reich an C2 +-Kohlenwasserstoffen ist,
    - Einführen des Sumpfstroms (171) auf einer Einspeisungsebene (P1) einer Fraktionier-Kolonne (61), die mit einem Kopf-Kondensator (63) versehen ist, wobei der Kopf-Kondensator einen Separator-Ballon aufweist, der eine flüssige Fraktion (187) produziert, wobei die Fraktionier-Kolonne (61) am Kopf den ethanreichen Strom (19) und im Sumpf den Schnitt aus C3 +-kohlenwasserstoffen (17) produziert, und
    - Einführen eines Primär-Rückfluss-Stroms (189), der in dem Kopf-Kondensator (63) beim Rückfluss in die Fraktionier-Kolonne (61) produziert wird,
    - dadurch gekennzeichnet, dass für Ethan-Extraktionsraten, die kleiner als eine vorbestimmte Schwelle sind, mindestens ein sekundärer Rückfluss-Strom (191) ausgehend von dem Kopf-Kondensator (63) produziert wird, durch Trennen der flüssigen Fraktion (187) in den primären Rückfluss-Strom (189) und in den sekundären Rückfluss-Strom (191),
    - und dass der ethanreiche Strom (19) ausgehend von einer Zwischenebene (P2) der Fraktionier-Kolonne (61), die über der Einspeisungs-Ebene (P1) der Kolonne (61) positioniert ist, abgezogen wird,
    - und dass beim Rückfluss der sekundäre Rückfluss (191), der durch Trennen der flüssigen Fraktion produziert wird, am Kopf der Wiedergewinnungs-Kolonne (35) eingeführt wird.
  2. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass der Durchfluss des ethanreichen Stroms (19) durch Regulieren des Durchflusses des sekundären Rückfluss-Stroms (191) und durch Regulieren des Drucks der Wiedergewinnungs-Kolonne (35) gesteuert wird.
  3. Verfahren gemäß Anspruch 1 oder 2, dadurch gekennzeichnet, dass die Fraktionier-Kolonne (61) zwischen 1 und 7 theoretische Böden über der Zwischenebene (P2) aufweist.
  4. Verfahren gemäß einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass der sekundäre Rückfluss-Strom (191) durch Wärmetausch mit mindestens einem ersten Teil (135) des Kopfstroms (131) der Wiedergewinnungs-Kolonne (35) abgekühlt wird.
  5. Verfahren gemäß Anspruch 4, dadurch gekennzeichnet, dass der Rückfluss-Strom (123) der Wiedergewinnungs-Kolonne (35) durch Wärmetausch mit mindestens einem zweiten Teil (133) des Kopfstroms (131) der Wiedergewinnungs-Kolonne (35) abgekühlt wird.
  6. Verfahren gemäß einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass der sekundäre Rückfluss-Strom ausgehend von einem Gemisch aus einem Gas-Strom (201) und einem flüssigen Strom (191) aus dem Kopf-Kondensator (63) produziert wird.
  7. Verfahren gemäß einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass der maximale Gehalt an Methan und Propan in dem ethanreichen Strom (19) mit Hilfe eines Sumpfverdampfers (41) gesteuert wird, der an der Wiedergewinnungs-Kolonne (35) montiert ist.
  8. Verfahren gemäß einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass der Gehalt an C5 +-Kohlenwasserstoffen in dem behandelten Erdgas (15) kleiner als 1 ppm ist.
  9. Anlage (11) für die gleichzeitige Produktion eines behandelten Erdgases (15) und eines Schnitts (17), der reich an C3 +-Kohlenwasserstoffen ist, und unter zumindest bestimmten Produktionsbedingungen eines ethanreichen Stroms (19), ausgehend von einem Ausgangs-Erdgas (13), das Methan, Ethan und C3 +-Kohlenwasserstoffe aufweist, wobei die Anlage (11) aufweist:
    - Mittel (25) zum Abkühlen und zum teilweisen Kondensieren des Ausgangs-Erdgases (13),
    - Mittel (27) zum Trennen des abgekühlten Erdgases (113), um einen flüssigen Strom (117) und einen gasförmigen Strom (115) zu bilden,
    - eine Kolonne (35) zur Wiedergewinnung der C2 +-Kohlenwasserstoffe,
    - Mittel (119) zum Entspannen und Einführen des flüssigen Stroms (117) in die Wiedergewinnungs-Kolonne (35), der in eine erste Zwischenebene (N1) der Kolonne (35) mündet, und
    - Mittel zum Trennen des gasförmigen Stroms (115), um einen Strom (125) zum Einspeisen in Kolonne (35) und einen Rückfluss-Strom (123) zu bilden,
    - eine Turbine (29) zum Entspannen des Einspeisungs-Stroms (121) und Mittel zum Einführen des Stroms (125), der aus der Turbine (29) stammt, auf einer zweiten Zwischenebene (N2) der Wiedergewinnungs-Kolonne (35),
    - Mittel (33) zum Abkühlen und zumindest teilweisen Kondensieren des Rückfluss-Stroms (123), der in Mittel zum Entspannen (127) des abgekühlten Rückfluss-Stroms mündet,
    - Mittel zum Einführen des abgekühlten Rückfluss-Stroms (128), der von den Mitteln zum Entspannen (127) des abgekühlten Rückfluss-Stroms kommt, auf einer dritten Ebene (N3) der Wiedergewinnungs-Kolonne (35),
    - Mittel (131) zur Wiedergewinnung des Kopfstroms der Kolonne, um das behandelte Erdgas (15) zu bilden,
    - Mittel (171) zur Wiedergewinnung des Sumpfstroms der Kolonne, um einen flüssigen Strom zu bilden, der reich an C2 +-Kohlenwasserstoffen ist,
    - eine Fraktionier-Kolonne (61), die mit einem Kopf-Kondensator (63) versehen ist, wobei der Kopf-Kondensator einen Separator-Ballon aufweist, der eine flüssige Fraktion produziert,
    - Mittel (47) zum Einführen des Sumpfstroms (171) in einer Einspeisungsebene (P1) der Fraktionier-Kolonne (61),
    - Mittel zur Wiedergewinnung des ethanreichen Stroms (19), die am Kopf der Fraktionier-Kolonne (61) positioniert sind, und Mittel zur Wiedergewinnung des Schnitts (17) von C3 +-Kohlenwasserstoffen, die im Sumpf der Fraktionier-Kolonne (61) positioniert sind, und
    - Mittel (71) zum Einführen eines primären Rückfluss-Stroms (189), der in dem Kopf-Kondensator (63) produziert wird, als Rückfluss in die Fraktionier-Kolonne (61),
    dadurch gekennzeichnet, dass die Anlage aufweist: Mittel zur Produktion für Ethan-Extraktionsraten des Ausgangs-Erdgases, die kleiner als eine vorbestimmte Schwelle sind, eines sekundären Rückfluss-Stroms (191), der aus dem Kopf-Kondensator (63) stammt, durch Teilen der flüssigen Fraktion in den primären Rückfluss-Strom und in den sekundären Rückfluss-Strom,
    und dass die Mittel zur Wiedergewinnung eines ethanreichen Stroms (19) auf einer Zwischenebene (P2) der Fraktionier-Kolonne (61), die über der Einspeisungsebene (P1) der Kolonne (61) positioniert ist, angezapft sind,
    und dass die Anlage (11) Mittel (193) aufweist, zum Einführen des sekundären Rückfluss-Stroms (191), der durch Trennen der flüssigen Fraktion hergestellt wird, in den Rückfluss in der Wiedergewinnungs-Kolonne (35).
  10. Anlage (11) gemäß Anspruch 9, dadurch gekennzeichnet, dass sie Mittel zum Steuern des Durchflusses des ethanreichen Stroms aufweist, die Mittel (193) zum Regulieren des Durchflusses des sekundären Rückfluss-Stroms (191) und Mittel zum Regulieren (43, 31) des Drucks in der Wiedergewinnungs-Kolonne (35) aufweisen.
  11. Anlage (11) gemäß Anspruch 9 oder 10, dadurch gekennzeichnet, dass die Fraktionier-Kolonne (61) zwischen 1 und 7 theoretische Böden über der Zwischenebene (P2) aufweist.
  12. Anlage (11) gemäß einem der Ansprüche 9 bis 11, dadurch gekennzeichnet, dass sie Mittel (73) zum Abkühlen des sekundären Rückfluss-Stroms (191) aufweist, die den Strom (191) in ein Wärmetausch-Verhältnis mit zumindest einem Teil (135) des Kopfstroms (131) der Wiedergewinnungs-Kolonne (35) setzen.
  13. Anlage (11) gemäß Anspruch 12, dadurch gekennzeichnet, dass sie Mittel (33) zum Abkühlen des Rückfluss-Stroms (123) der Wiedergewinnungs-Kolonne (35) aufweist, die den Strom (123) in ein Wärmetausch-Verhältnis mit zumindest einem Teil (133) des Kopfstroms (131) der Wiedergewinnungs-Kolonne (35) setzen.
  14. Anlage (11) gemäß einem der Ansprüche 9 bis 13, dadurch gekennzeichnet, dass die Mittel zur Produktion des sekundären Rückfluss-Stroms (191) Mittel zum Mischen eines Gas-Stroms (201) und eines flüssigen Stroms (191) aus dem Kopf-Kondensator (63) aufweisen.
  15. Anlage gemäß einem der Ansprüche 9 bis 14, dadurch gekennzeichnet, dass sie Mittel (167,169) zum Steuern des maximalen Gehaltes an Methan und Propan in dem ethanreichen Strom (19) aufweist, einen Sumpfverdampfer (41) aufweisend, der an der Wiedergewinnungs-Kolonne (35) montiert ist.
EP05850537A 2004-12-22 2005-12-19 Verfahren und installation zur herstellung von behandeltem erdgas aus einem kohlenwasserstoffreichen c3+-schnitt und einem ethanreichen strom Active EP1828697B1 (de)

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 EP1828697A1 (de) 2007-09-05
EP1828697B1 true EP1828697B1 (de) 2008-12-03

Family

ID=34953803

Family Applications (1)

Application Number Title Priority Date Filing Date
EP05850537A Active EP1828697B1 (de) 2004-12-22 2005-12-19 Verfahren und installation zur herstellung von behandeltem erdgas aus einem kohlenwasserstoffreichen c3+-schnitt und einem ethanreichen strom

Country Status (18)

Country Link
US (1) US7458232B2 (de)
EP (1) EP1828697B1 (de)
CN (1) CN100547326C (de)
AT (1) ATE416352T1 (de)
AU (1) AU2005321162B2 (de)
BR (1) BRPI0519380B1 (de)
CA (1) CA2592012C (de)
DE (1) DE602005011482D1 (de)
DK (1) DK1828697T3 (de)
EA (1) EA010386B1 (de)
EG (1) EG24056A (de)
ES (1) ES2318587T3 (de)
FR (1) FR2879729B1 (de)
MX (1) MX2007007351A (de)
MY (1) MY145312A (de)
PL (1) PL1828697T3 (de)
PT (1) PT1828697E (de)
WO (1) WO2006070097A1 (de)

Families Citing this family (16)

* Cited by examiner, † Cited by third party
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
US20110174017A1 (en) * 2008-10-07 2011-07-21 Donald Victory Helium Recovery From Natural Gas Integrated With NGL Recovery
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
CN105074370B (zh) * 2012-12-28 2017-04-19 林德工程北美股份有限公司 一种ngl(液化天然气回收)和lng(液化天然气)的组合工艺
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)

* Cited by examiner, † Cited by third party
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
DE60224585T2 (de) * 2002-05-20 2009-04-02 Fluor Corp., Aliso Viejo Doppelrückflussverfahren und konfigurationen für verbesserte erdgaskondensatgewinnung
US7051553B2 (en) * 2002-05-20 2006-05-30 Floor Technologies Corporation Twin reflux process and configurations for improved natural gas liquids recovery

Also Published As

Publication number Publication date
FR2879729B1 (fr) 2008-11-21
EA200701340A1 (ru) 2007-10-26
CN101103239A (zh) 2008-01-09
DK1828697T3 (da) 2009-03-09
PL1828697T3 (pl) 2009-06-30
CA2592012A1 (fr) 2006-07-06
FR2879729A1 (fr) 2006-06-23
DE602005011482D1 (de) 2009-01-15
AU2005321162A1 (en) 2006-07-06
MX2007007351A (es) 2007-08-14
US20060144081A1 (en) 2006-07-06
ES2318587T3 (es) 2009-05-01
CN100547326C (zh) 2009-10-07
BRPI0519380B1 (pt) 2018-03-06
PT1828697E (pt) 2009-02-12
WO2006070097A1 (fr) 2006-07-06
EA010386B1 (ru) 2008-08-29
ATE416352T1 (de) 2008-12-15
BRPI0519380A2 (pt) 2009-01-20
AU2005321162B2 (en) 2010-07-15
CA2592012C (fr) 2013-10-15
EG24056A (en) 2008-04-30
MY145312A (en) 2012-01-13
US7458232B2 (en) 2008-12-02
EP1828697A1 (de) 2007-09-05

Similar Documents

Publication Publication Date Title
EP1828697B1 (de) Verfahren und installation zur herstellung von behandeltem erdgas aus einem kohlenwasserstoffreichen c3+-schnitt und einem ethanreichen strom
EP1454104B1 (de) Verfahren und vorrichutng zur zerlegung eines methan enthaltenden gasgemisches durch rektifikation
EP1639062B1 (de) Verfahren und vorrichtung zur gleichzeitigen produktion eines erdgases zur verflüssigung und einer flüssigen fraktion aus erdgas
EP2422152B1 (de) Verfahren zur herstellung eines methanreichen stroms und einer c2+-kohlenwasserstoffreichen fraktion aus einem erdgaseinsatzstrom und entsprechende einrichtung
EP2205920B1 (de) Verfahren zur verflüssigung von erdgas mit hochdruckfraktionierung
EP2870226B1 (de) Prozess und apparat zur produktion von behandelten erdagas sowie einer fraktion angereichert mit c3+ kohlenwasserstoffen und einer fraktion angereichert mit ethan
EP3625196B1 (de) Verfahren zur rückgewinnung eines stroms von c2+-kohlenwasserstoffen in einem raffinerierestgas und zugehörige anlage
EP2630428B1 (de) Vereinfachtes verfahren zur erzeugung eines methanreichen stroms und einer c2+kohlenwasserstoffreichen fraktion aus einem erdgaszustrom und entsprechende anlage
WO2008087318A2 (fr) Procédé de séparation d'un mélange de monoxyde de carbone, de méthane, d'hydrogène et éventuellement d'azote par distillation cryogénique
EP2553055B1 (de) Verfahren zur behandlung eines gekrackten gasstroms aus einem kohlenwasserstoff-pyrolyse-reaktor und zugehörige anlage
WO2010109130A1 (fr) Procédé de traitement d'un gaz naturel de charge pour obtenir un gaz naturel traité et une coupe d'hydrocarbures en c5 +, et installation associée
EP2494295B1 (de) Verfahren zur fraktionierung eines gerissenen gasflusses zur gewinnung eines ethylenreichen ausschnitts und eines kraftstoffflusses sowie entsprechende anlage
EP2661479A1 (de) Verfahren zur herstellung eines kohlenwasserstoffreichen c3 +-fraktion und eine methan-und ethanreichen strom aus einer kohlenwasserstoff-reichen einsatzstroms und zugehörige anlage
EP3060629B1 (de) Verfahren zur fraktionierung eines stromes von spaltgas unter verwendung eines zwischensrückführungsstromes und zugehörige anlage
CA3119860A1 (fr) Procede de traitement d'un flux de gaz d'alimentation et installation associee

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20070612

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LT LU LV MC NL PL PT RO SE SI SK TR

17Q First examination report despatched

Effective date: 20071029

DAX Request for extension of the european patent (deleted)
GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LT LU LV MC NL PL PT RO SE SI SK TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: LANGUAGE OF EP DOCUMENT: FRENCH

REF Corresponds to:

Ref document number: 602005011482

Country of ref document: DE

Date of ref document: 20090115

Kind code of ref document: P

REG Reference to a national code

Ref country code: RO

Ref legal event code: EPE

REG Reference to a national code

Ref country code: PT

Ref legal event code: SC4A

Free format text: AVAILABILITY OF NATIONAL TRANSLATION

Effective date: 20090130

REG Reference to a national code

Ref country code: DK

Ref legal event code: T3

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20081203

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2318587

Country of ref document: ES

Kind code of ref document: T3

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20081203

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20081203

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20081203

REG Reference to a national code

Ref country code: HU

Ref legal event code: AG4A

Ref document number: E005139

Country of ref document: HU

BERE Be: lapsed

Owner name: TECHNIP FRANCE SA

Effective date: 20081231

REG Reference to a national code

Ref country code: PL

Ref legal event code: T3

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20081231

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20090303

Ref country code: IS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20090403

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20081231

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed

Effective date: 20090904

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20081203

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20081219

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20091231

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20090304

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20091231

REG Reference to a national code

Ref country code: FR

Ref legal event code: PLFP

Year of fee payment: 11

REG Reference to a national code

Ref country code: FR

Ref legal event code: PLFP

Year of fee payment: 12

REG Reference to a national code

Ref country code: FR

Ref legal event code: PLFP

Year of fee payment: 13

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20201116

Year of fee payment: 16

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20201210

Year of fee payment: 16

Ref country code: FR

Payment date: 20201218

Year of fee payment: 16

Ref country code: PT

Payment date: 20201117

Year of fee payment: 16

Ref country code: HU

Payment date: 20201201

Year of fee payment: 16

Ref country code: IE

Payment date: 20201127

Year of fee payment: 16

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: PL

Payment date: 20201120

Year of fee payment: 16

Ref country code: SK

Payment date: 20201119

Year of fee payment: 16

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 20210107

Year of fee payment: 16

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: PT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20220620

REG Reference to a national code

Ref country code: NL

Ref legal event code: MM

Effective date: 20220101

REG Reference to a national code

Ref country code: SK

Ref legal event code: MM4A

Ref document number: E 5594

Country of ref document: SK

Effective date: 20211219

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20220101

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SK

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211219

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211219

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: HU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211220

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211231

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211219

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20230221

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211220

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: PL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211219

P01 Opt-out of the competence of the unified patent court (upc) registered

Effective date: 20230601

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20231116

Year of fee payment: 19

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: RO

Payment date: 20231127

Year of fee payment: 19

Ref country code: EE

Payment date: 20231121

Year of fee payment: 19

Ref country code: DK

Payment date: 20231215

Year of fee payment: 19

Ref country code: DE

Payment date: 20231121

Year of fee payment: 19

Ref country code: CZ

Payment date: 20231129

Year of fee payment: 19

Ref country code: BG

Payment date: 20231204

Year of fee payment: 19

Ref country code: AT

Payment date: 20231127

Year of fee payment: 19

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: TR

Payment date: 20231218

Year of fee payment: 19