WO2019141909A1 - Procede de traitement d'un gaz naturel contenant du dioxyde de carbone - Google Patents
Procede de traitement d'un gaz naturel contenant du dioxyde de carbone Download PDFInfo
- Publication number
- WO2019141909A1 WO2019141909A1 PCT/FR2018/050118 FR2018050118W WO2019141909A1 WO 2019141909 A1 WO2019141909 A1 WO 2019141909A1 FR 2018050118 W FR2018050118 W FR 2018050118W WO 2019141909 A1 WO2019141909 A1 WO 2019141909A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- permeate
- retentate
- line
- fluidly connected
- membrane
- Prior art date
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/225—Multiple stage diffusion
- B01D53/226—Multiple stage diffusion in serial connexion
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/02—Elements in series
- B01D2317/022—Reject series
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/02—Elements in series
- B01D2317/025—Permeate series
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/06—Use of membrane modules of the same kind
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/548—Membrane- or permeation-treatment for separating fractions, components or impurities during preparation or upgrading of a fuel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Definitions
- the present invention relates to a membrane-type treatment method of a natural gas from a deposit for extracting the fraction of carbon dioxide that it contains in order to be able to reinject it within the deposit.
- the invention also relates to an installation adapted to the implementation of this method.
- Natural gas purification processes must therefore be able to produce carbon dioxide of sufficient quality and be capable of processing a natural gas comprising an increasing fraction of carbon dioxide.
- carbon dioxide is compressed using a compressor, which can increase the energy bill for this type of process.
- Another type of treatment relies on cryogenic processes. Their energy interest is even greater than the concentration of carbon dioxide in the original gas is high.
- An example of a cryogenic process is given in US 4,152,129.
- a finishing treatment, for example of the amine type is therefore essential if a severe carbon dioxide specification is required.
- this method is difficult to achieve in a modular manner.
- membrane modules are another type of treatment.
- the applications of these membrane modules for medium carbon dioxide gases have greatly increased in recent years.
- the membrane surface required depends on the composition of the natural gas to be treated, the gas pressure at the inlet of the modules and the pressure of the permeate.
- Membrane module treatment is advantageous for relatively high carbon dioxide concentrations and for a certain range of "inlet / permeate" partial pressure ratios. It is also possible to provide several treatment stages by membrane module to concentrate the carbon dioxide in the permeate, which requires the provision of intermediate compressions of the permeate. The reinjection of carbon dioxide requires additional compression, from the low pressure of the final permeate, which further increases the energy bill for this type of process.
- the first stage of treatment extracts carbon dioxide at a moderate rate so as not to cause too much natural gas such as methane to reach the required purity of carbon dioxide.
- the retentate obtained comprising a large fraction of carbon dioxide is sent to the second treatment stage in which the carbon dioxide is extracted at a high rate so that to obtain a retentate having a satisfactory purity.
- a significant amount of natural gas from the second stage of treatment passes into the permeate. The carbon dioxide thus produced does not meet the required specifications and, after compression, is recycled to the inlet of the first treatment stage.
- the first treatment stage allows a strong extraction of the carbon dioxide in order to obtain a fraction of natural gas having directly the required specifications.
- This first stage of treatment results in a significant loss of natural gas in the permeate which is recovered in the second stage of treatment after compression.
- the production of permeate is limited so as not to affect the purity of the carbon dioxide produced in the second permeate.
- the retentate produced is therefore a mixture that does not satisfy any of the purities required for natural gas and carbon dioxide and is recycled to the inlet of the first treatment stage.
- the fraction of gas passing through the membrane and the resulting retentate and permeate compositions depend on the relative partial pressures of CO 2 , methane and other constituents of the gas to be treated.
- the feed of the second treatment stage also depends on the composition of the feed gas.
- the increase in the carbon dioxide content in the feed gas is achieved by increasing the membrane surface of the first treatment stage.
- the surface becomes so large that the gas is sufficiently purified to reduce the need for membrane surface at the second treatment stage, resulting in a total excess membrane as the carbon dioxide content in the feed gas increases.
- the installed surface of the second treatment stage becomes partly unused because the purified natural gas at the first treatment stage requires less treatment at the second treatment stage.
- the total power consumed in the treatment unit is constant, its distribution between the recycle compressor and the carbon dioxide injection in the reservoir varies greatly complicating the design of the machines.
- the membrane surface of the second treatment stage that must be increased to compensate for the increase in the carbon dioxide content in the natural gas to be treated.
- the area required for the first stage of treatment eventually decreases, so that the required total area varies substantially less than in the retentate mode, so that the installed area is almost fully utilized regardless of the evolution of the content of the surface.
- Carbon dioxide in the feed gas allows for efficient use of the invested membrane surface.
- the invention relates to a method for treating a natural gas containing carbon dioxide in an installation that comprises a plurality of membrane modules,
- the first treatment stage and the second treatment stage being fluidly connected in retentate or permeate mode, wherein when one of the treatment stages requires less membrane surface for gas treatment and the other treatment stage requires more membrane surface for gas treatment, then the process includes a reassignment step to the stage requiring more membrane surface of at least one membrane module assigned to the floor requiring less membrane surface.
- the method of treating a natural gas of the present invention overcomes the disadvantages of the state of the art.
- the membrane surface requirement of the treatment stages is a function of the carbon dioxide content in the natural gas to be treated, this content being caused to change over time.
- the method which is the subject of the present invention makes it possible to modulate and optimize the membrane surface required by each treatment stage for the treatment of a natural gas, as a function of the evolution of the carbon dioxide content in this natural gas. by limiting the number of membrane modules to be provided for the entire installation.
- the optimization of the membrane-type natural gas treatment according to the invention is carried out by adapting the membrane surface of the two treatment stages by transfer of at least one membrane module of a stage requiring less than Membrane surface to another floor requiring more membrane surface.
- the number of membrane modules of the stage requiring less membrane surface to be reassigned to the floor requiring more membrane surface may depend on the carbon dioxide content in the natural gas, in particular its increase.
- the number of membrane modules of the stage requiring less membrane surface to be reassigned to the floor requiring more membrane surface may depend on the evolution of the pressure of the natural gas.
- the two treatment stages can be fluidly connected in retentate mode and the installation can furthermore comprise:
- each of the membrane modules comprising an inlet, a permeate outlet and a retentate outlet; wherein, in the first processing stage, all of the module inputs are fluidly connected to the supply line, the set of permeate module outputs are fluidly connected to the permeate collection line, and the all of the retentate module outputs are fluidly connected to the retentate transfer line, itself fluidly connected to the transfer input line;
- the step of reassigning the second treatment stage to the first treatment stage comprising:
- the two treatment stages can be fluidically connected in permeate mode, and the installation can furthermore comprise:
- each of the membrane modules comprising an inlet, a permeate outlet and a retentate outlet;
- the step of reassigning the first treatment stage to the second treatment stage comprising:
- the invention relates to a method of treating a natural gas containing carbon dioxide in an installation which comprises membrane modules,
- the treatment of the natural gas is carried out according to the retentate mode, then when the carbon dioxide content present in the natural gas reaches a given value, the treatment of the natural gas is carried out according to the permeate mode, or -
- the natural gas treatment is performed in the permeate mode, then when the carbon dioxide content in the natural gas reaches a given value, the natural gas treatment is carried out according to the retentate mode.
- the natural gas treatment of the invention can advantageously be optimized by adapting the procedure to be followed during treatment, in particular by sequentially going from one operating mode to another.
- another more economical operating mode for the treatment of a natural gas according to the evolution of the carbon dioxide content in natural gas that is to say to go from the retentate mode permeate mode and vice versa.
- the installation can comprise:
- each of the membrane modules comprising an inlet, a permeate outlet and a retentate outlet
- the first treatment stage and the second treatment stage being in series of permeate so that:
- all the module inputs are fluidly connected to the supply line
- the set of retentate module outputs are fluidly connected to the retentate collection line
- all the outputs permeate modules are fluidly connected to the permeate transfer line, itself fluidly connected to the transfer input line;
- all the module inputs are fluidly connected to the transfer input line
- the set of permeate module outputs are fluidly connected to the permeate collection line
- all retentate module outputs are fluidly connected to the retentate transfer line, itself fluidly connected to the supply line;
- the passage from permeate mode to retentate mode is carried out as follows: the fluidic disconnection of the inlet, the permeate outlet and the retentate outlet of the membrane modules; and fluidically connecting the inlet, the permeate outlet, and the retentate outlet of at least a portion of the membrane modules so that:
- all the module inputs are fluidly connected to the supply line
- the set of permeate module outputs are fluidly connected to the permeate collection line
- all the outputs retentate module are fluidly connected to the retentate transfer line, itself fluidly connected to the transfer input line;
- all of the module inputs are fluidly connected to the transfer input line
- the set of retentate module outputs are fluidly connected to the retentate collection line
- all permeate module outputs are fluidly connected to the permeate transfer line, itself fluidly connected to the supply line.
- the installation implemented may further comprise a compressor adapted to compress the permeate recovered in the permeate transfer line.
- the treatment of the natural gas containing a certain carbon dioxide content requires a total required membrane surface S r , the membrane modules providing a total available area, wherein when the total available membrane area exceeds the total area required for the separation of the carbon dioxide, the pressure of the permeate can be increased on any of the stages of the unit.
- the increase of the pressure of the permeate can be achieved by:
- the natural gas treatment method according to the invention additionally allows the adjustment of the pressure of the permeate in order to make maximum use of the membrane surface installed at the treatment stages and to reduce the energy consumption of this installation.
- the natural gas treatment process according to the invention is particularly advantageous when the content of carbon dioxide present in the natural gas to be treated increases with time.
- the invention also relates to a plant for treating a natural gas containing carbon dioxide, comprising: a supply line;
- each of the membrane modules comprising an input fluidically connectable to the supply line and the transfer input line, a retentate outlet fluidly connectable to the retentate collection line and the transfer line retentate, and a permeate outlet fluidly connectable to the permeate collection line and the permeate transfer line, each of the membrane modules being fluidly isolable from the lines;
- valve system adapted to allocate a portion of the membrane modules to a first treatment stage and another portion of the membrane modules to a second treatment stage so that:
- all the module inputs are fluidly connected to the supply line
- the set of permeate module outputs are fluidly connected to the permeate collection line
- all the outputs retentate module are fluidly connected to the retentate transfer line, itself fluidly connected to the transfer input line;
- all of the module inputs are fluidly connected to the transfer input line
- the set of retentate module outputs are fluidly connected to the retentate collection line
- all permeate module outputs are fluidly connected to the permeate transfer line, itself fluidly connected to the supply line;
- all the module inputs are fluidly connected to the supply line
- the set of retentate module outputs are fluidly connected to the retentate collection line
- all the outputs permeate modules are fluidly connected to the permeate transfer line, itself fluidly connected to the transfer input line;
- all the module inputs are fluidly connected to the transfer input line
- the set of permeate module outputs are fluidly connected to the permeate collection line
- all module outputs retentate are fluidly connected to the retentate transfer line, itself fluidly connected to the feed line.
- Figure la schematically shows a conventional installation in serial operating mode of the retentate in which the first stage of treatment and the second stage of treatment are fluidly connected in retentat mode.
- Fig. 1b schematically shows a conventional plant in serial operating mode of the permeate in which the first process stage and the second process stage are fluidically connected in permeate mode.
- Figure 2 schematically shows an installation for implementing the method of the invention.
- FIGS. 3a, 3b and 3c schematically represent an installation for implementing the method of the invention in which the first treatment stage and the second treatment stage are connected fluidly in retentate mode, and in which a membrane module of the second treatment stage is reassigned to the first stage of treatment.
- FIGS. 4a, 4b and 4c schematically represent an installation for carrying out the method of the invention in which the first treatment stage and the second treatment stage are fluidically connected in permeate mode, and in which a membrane module of the first treatment stage is reassigned to the second stage of treatment.
- FIG. 5 is a graph showing the evolution of the membrane surface used by a method of the invention comprising steps of reallocation of the membrane modules and a step of passing from the permeate mode to the retentate mode.
- Figure 6 is a graph showing the evolution of the total power required for the operation of the method of the invention comprising steps of reallocation of the membrane modules and a step of permeate mode to retentate mode.
- Figure 7 is a graph showing the evolution of membrane surfaces required of a prior art process in which the first treatment stage and the second treatment stage are fluidly connected in retentate mode.
- FIG. 8 is a graph showing the evolution of the power consumed by a method of the prior art in which the first treatment stage and the second treatment stage are fluidly connected in retentate mode.
- Figure 9 is a graph showing the evolution of membrane surfaces required of a prior art process in which the first treatment stage and the second treatment stage are fluidically connected in permeate mode.
- Figure 10 is a graph showing the evolution of the power consumed by a method of the prior art in which the first treatment stage and the second treatment stage are fluidically connected in permeate mode.
- the installation I comprises:
- Each of the membrane modules M comprises an input EM fluidly connectable to the supply line LA and to the transfer input line LET, a retentate output SR fluidically connectable to the retentate collecting line LCR and to the transfer line. LTR retentate, and a permeate outlet SP fluidly connectable to the LCP permeate collection line and the LTP permeate transfer line.
- Each of the membrane modules M can be fluidly isolated from the lines.
- the valve system SV is adapted to allocate a part of the membrane modules M to a first treatment stage El and another part of the membrane modules M to a second treatment stage E2 according to a retentate series procedure (or "retentate mode") or a series procedure of the permeate (or "permeate mode").
- membrane module means a unit comprising an inlet EM, a permeate outlet SP and a retentate outlet SR connectable to lines described above.
- Each of the membrane modules M may comprise one or more membrane elements connected in series or in parallel and making it possible to purify the natural gas by separating it from the impurities it comprises, in particular C0 2 .
- a membrane module M is the smallest gas permeation object that can be isolated from the others, in particular by the SV valve system.
- the membrane module M may be of the frontal membrane separation type, with tangential membrane separation at cocurrent, with tangential membrane separation with counterflow or with tangential membrane separation with cross currents.
- a membrane module M is composed of one or more membrane elements that can be chosen from a spiral planar membrane or a hollow fiber membrane.
- Such an installation I allows both the allocation of membrane modules M to one or other of the treatment stages E1, E2, the reassignment to one of the treatment stages of one or more membrane modules M previously assigned to the other of the treatment stages according to the evolution of the operating parameters, and the passage of the operating mode between a retentate mode or a permeate mode.
- the valve system SV may further comprise for each of the membrane modules M:
- a feed-module pipe CAM fixed at one of its ends to the feed line LA and at the other end thereof to the inlet EM of the membrane module M, the supply-module pipe CAM comprising a valve VAM allowing flow control within it, including its obstruction;
- a transfer-module line CTM fixed at one of its ends to the transfer input line LET and at the other of its ends to the input EM of the membrane module M, the transfer-module line CTM comprising a valve VTM allowing flow control within it, including its obstruction;
- a CTR retentate transfer-modulus conduit attached at one of its ends to the retentate output SR of the membrane module M and attached at the other end thereof to the retentate transfer line LTR, the module-transfer conduit retentate CTR comprising a VTR valve for controlling the flow rate of the retentate circulating therein, including its obstruction;
- the module-collection conduit CCR retentate comprising a VCR valve for controlling the flow rate of the retentate circulating therein, including its obstruction;
- a CTP permeate transfer-modulus conduit attached at one of its ends to the permeate outlet SP of the membrane module M and attached at the other end thereof to the permeate transfer line LTP, the module-transfer conduit permeate CTP comprising a VTP valve for controlling the flow rate of the permeate circulating therein, including its obstruction;
- the module-collection conduit of permeate PCC comprising a VCP valve for controlling the flow of permeate circulating therein, including its obstruction.
- the SV valve system may further include:
- a CAR retentate transfer-supply line attached at one of its ends to the LTR retentate transfer line and at the other end thereof to the LA feed line, the CAR retentate transfer-feed line comprising a VAR valve for controlling the flow of the retentate circulating therein, including its obstruction;
- CER retentate transfer-inlet line attached at one end to the LTR retentate transfer line and at the other end to the LET transfer line, the CER retentate transfer-inlet line comprising a VER valve for controlling the flow rate of the retentate circulating therein, including its obstruction;
- a CAP permeate transfer-feed line attached at one end to the LTP permeate transfer line and at the other end to the LA feed line, the CAP permeate transfer-feed line comprising a VAP valve for controlling the flow rate of the permeate circulating therein, including its obstruction; and a CEP permeate transfer-inlet conduit attached at one end to the LTP permeate transfer line and at the other end thereof to the LET transfer line, the permeate transfer-inlet conduit CEP comprising a VEP valve for controlling the flow of permeate circulating therein, including its obstruction.
- each valve may be selected from a gate valve, a gate valve, a plug valve, a gate valve, a butterfly valve, a piston valve, a needle valve and a diaphragm valve.
- the valves mentioned above are all-or-nothing valves (with the exception of the valves of the bypass lines if they are provided which are preferably valves for regulating the flow rate including the obstruction) .
- valve system SV may further include a valve control for electrical control of the opening and closing of the valves.
- valves are coupled in pairs so that if one of them is open, the other is closed. Coupling pairs are:
- valves VAR and VER the valves VAR and VER;
- valves VAP and VEP are the valves VAP and VEP.
- valves VTR, VCR, VTP, and VCP can also be coupled together so that only one or the other of the following configurations can be achieved when the membrane module Corresponding M is in operating mode:
- VTR and VCP valves are open, the VTP and VCR valves are closed; and the VTP and VCR valves are open, the VTR and VCP valves are closed.
- the plant I may further comprise a recycle compressor CompTR in the permeate transfer line LTP in order to compress the permeate recovered therein.
- the recirculation compressor CompTR is adapted to increase the pressure of the permeate recovered via the permeate outlet SP of the membrane module M of the second treatment stage E2 in the permeate transfer line LTP, this compressed permeate can then be injected into the membrane module M of the first treatment stage El.
- the recirculation compressor CompTR is adapted to increase the pressure of the permeate recovered via the permeate outlet SP of the membrane module M of the first treatment stage E1 in the LTP permeate transfer line, this compressed permeate can then be injected into the membrane module M of the second treatment stage E2.
- the installation I may further comprise a CompTP reinjection compressor in the LCP permeate collection line for compressing the permeate recovered therein. This compressed permeate comprising CO 2 can then be injected into a petroleum deposit.
- the CompTP reinjection compressor is adapted to increase the pressure of the permeate recovered via the permeate outlet SP of the membrane module M of the first treatment stage E1 in the LCP permeate collection line, this compressed permeate can then be reinjected into the gas field.
- the CompTP reinjection compressor is adapted to increase the pressure of the permeate recovered via the permeate outlet SP of the membrane module M of the second treatment stage E2 in the LCP permeate collection line, this compressed permeate can then be reinjected into the gas field.
- compressor means a device for increasing the pressure of a gas.
- first and second compressors may be rotary compressors comprising separately selected blades from a centrifugal compressor, an axial compressor or a helical compressor.
- the installation I may also comprise at least one of: a BAP bypass line of the membrane modules connecting the feed line LA directly to the permeate collection line LCP (bypass BAP) for sampling a part of the gas present in the feed line and bring it directly to the permeate collection line; a BAR bypass line of the membrane modules connecting the feed line LA directly to the collection line of the retentate LCR (bypass BAR) for the removal of a portion of the gas present in the feed line LA and bring it directly at the LCR retentate collection line; a BTP bypass line of the membrane modules connecting the LET transfer input line directly to the LCP permeate collection line (BTP bypass) for the removal of a portion of the gas present in the LET transfer input line and bring it directly to the LCP permeate collection line; and a BTR bypass line of the membrane modules connecting the LET transfer input line directly to the collection line of the LCR retentate (bypass BTR) for the removal of a portion of the gas present in the LET transfer input line and
- each bypass comprises a pipe and a corresponding valve: the ends of the pipe of the BAP bypass are connected to the supply line LA and the permeate collection line LCP; the ends of the BAR bypass line are connected to the LA feed line and the LCR retentate collection line; the ends of the BTP bypass line are connected to the LET transfer line and the LCP permeate collection line; and the ends of the BTR bypass line are connected to the LET transfer input line and the LCR retentate collection line.
- FIG. 2 A second possibility is illustrated in FIG. 2: the BAP bypass and BTP bypass share a BPP bypass line to the LCP permeate collection line, one of its ends being connected to this permeate collection line LCP, the another of its ends being bifurcated to connect to both the LA feed line and the LET transfer line, a valve being provided on each of the bifurcations; and bypass BAP and bypass BTR shares an BPR bypass line to the LCR retentate collection line, one of its ends being connected to this LCR retentate collection line, the other of its ends being bifurcated to connect at both the LA feed line and the LET transfer line, a valve being provided on each of the bifurcations.
- bypass BAP and bypass BAR share a bypass line from the feed line LA, one of its ends being connected to this feed line LA, the other of its ends being bifurcated to connect to both the LCP permeate collection line and the LCR retentate collection line, a valve being provided on each of the bifurcations; and the BTP and bypass bypass BTR share a bypass line from the LET transfer input line, one of its ends being connected to this LET transfer input line, the other of its ends being bifurcated to connect to both the LCP permeate collection line and the LCR retentate collection line, with one valve provided on each of the bifurcations.
- the allocation of the membrane modules M in the retentate mode is carried out in the following manner (see FIGS. 1a and 3a).
- the set of inputs EM of the membrane modules M are fluidly connected to the supply line LA
- the set of permeate outputs SP are fluidly connected to the permeate collection line LCP
- the set of retentate outputs SR are fluidly connected to the retentate transfer line LTR, itself fluidly connected to the LET transfer input line.
- the allocation of membrane modules M to the first treatment stage El can be easily performed by:
- the set of inputs EM of the membrane modules M are fluidly connected to the transfer input line LET
- the set of retentate outputs SR are fluidly connected to the LCR retentate collection line.
- the set of permeate outlets SP are fluidly connected to the permeate transfer line LTP, itself fluidly connected to the feed line LA.
- the allocation of membrane modules M to the second treatment stage E2 can be easily performed by:
- the retentate outputs SR of the membrane modules M of the first processing stage E1 are fluidly connected to the inputs EM of the membrane modules M of the second treatment stage E2.
- the table below summarizes the different connections in retentat mode:
- the table below summarizes the open or closed state of the valves in retentate mode:
- the allocation of the membrane modules M in the permeate mode is carried out as follows (see FIGS. 1b and 4a).
- the set of inputs EM of the membrane modules M are fluidly connected to the supply line LA
- the set of retentate outputs SR are fluidly connected to the collection line of retentate LCR
- the set of permeate outlets SP are fluidly connected to the permeate transfer line LTP, itself fluidly connected to the transfer input line LET.
- the allocation of membrane modules M to the first treatment stage El can be easily performed by:
- the set of inputs EM of the membrane modules M are fluidly connected to the transfer input line LET
- the set of permeate outputs SP are fluidly connected to the LCP permeate collection line.
- all of the retentate outputs SR are fluidly connected to the retentate transfer line LTR, itself fluidly connected to the LA feed line.
- the allocation of membrane modules M to the second treatment stage E2 can be easily performed by:
- the permeate outlets SP of the membrane modules M of the first treatment stage are fluidly connected to the module EM inputs of the membrane modules M of the second treatment stage E2.
- the table below summarizes the different connections in the permeate mode:
- the present invention relates to a method of treating a natural gas containing carbon dioxide in an installation I which comprises a plurality of membrane modules M, for example as described above.
- the term "natural gas” a gaseous mixture comprising hydrocarbons such as methane, ethane, propane and butane and impurities such as carbon dioxide (C0 2 ).
- the CO 2 content in the natural gas to be treated by the process of the present invention may be 10 mol%. at 80 mol%. In the vast majority of cases, this C0 2 content in natural gas increases over time. However, the present invention is not limited to this case can be used also in the case where the CO 2 content in natural gas decreases over time, or more generally fluctuates with time.
- the natural gas to be treated by the process of the present invention is introduced into the membrane module M via the inlet EM.
- a permeate comprising CO 2 is recovered at the permeate outlet SP while a retentate comprising the natural gas is recovered at the SR retentate outlet.
- the permeate and the retentate are thus recovered separately at the outlet of the membrane module M thus allowing purification of the natural gas.
- the C0 2 recovered can be injected into a petroleum field and the purified natural gas can be marketed after possible treatments.
- Part of the membrane modules M are assigned to a first treatment stage E1 defining a membrane surface and another part of the membrane modules M are assigned to a second treatment stage E2 defining a membrane surface.
- the membrane surface of each of the treatment stages necessary for treating the natural gas to be treated depends on the content of CO 2 in the gas to be treated.
- the first treatment stage E1 and the second treatment stage E2 can be connected fluidically either in retentate mode or in permeate mode.
- the CO 2 content in the natural gas may require a total required membrane surface S r , the membrane modules M providing a total available surface, when the total available membrane area exceeds the total area required for the separation of C0 2 , while the pressure of the permeate can be increased on any of the stages of the installation I.
- This pressure increase can be carried out by the CompTR recycle compressor or the CompTP reinjection compressor.
- the natural gas to be treated comprising CO 2 is introduced into each membrane module M of the first treatment stage El via their inputs EM via the feed line LA.
- the permeate of the first treatment stage El comprising the CO 2 is recovered at the permeate outlet SP of each membrane module M of the first treatment stage E1 in the permeate collection line LCP.
- the retentate of the first treatment stage comprising the natural gas and residual CO 2 is recovered via the retentate outlet SR of each membrane module M of the first treatment stage E1 in the retentate transfer line LTR.
- the retentate of the first treatment stage E1 is then introduced into each membrane module M of the second treatment stage E2 via their inputs EM by the transfer input line LET.
- the membrane module (s) M of the second treatment stage E2 make it possible to improve the purification of the natural gas by separating it from the residual C0 2 .
- the retentate of the second treatment stage E2 comprising the purified natural gas is recovered via the retentate outlet SR of each membrane module M of the second treatment stage E2 in the LCR retentate collection line.
- the permeate of the second treatment stage E2 comprising the residual C0 2 is in turn recovered via the permeate outlet SP of each membrane module M of the second treatment stage E2 in the permeate transfer line LTP. This permeate is then introduced into each membrane module M of the first treatment stage E1 via the feed line LA to increase the amount of C0 2 recovered in the permeate collection line LCP.
- the permeate of the first treatment stage E1 may comprise more than 75 mol%. of C0 2 , in particular of 80 mol%. at 99 mol%. of C0 2 , especially 94% mol. at 97 mol% CO 2 , for example about 95 mol%
- the retentate of the second treatment stage E 2 may comprise more than 75 mol%. natural gas, in particular 80 mol%. at 99 mol%. natural gas, especially 94 mol%. at 98 mol%. of natural gas.
- the permeate of the first treatment stage E1 comprising C0 2 can be reinjected into a petroleum deposit.
- the retentate of the second treatment stage E2 comprising purified natural gas may be marketed.
- the retentate method may further comprise increasing the pressure of the permeate recovered via the permeate outlet SP of the membrane module M of the second treatment stage E2 in the LTP permeate transfer line.
- the method according to the retentate mode further comprises increasing the pressure of the permeate recovered via the permeate outlet SP of the membrane module M of the first treatment stage E1 in the permeate collection line LCP.
- the natural gas to be treated comprising CO 2 is introduced into each membrane module M of the first treatment stage El via their input EM via the feed line LA.
- the retentate of the first treatment stage E1 comprising purified natural gas is recovered via the retentate outlet SR of each membrane module M of the first treatment stage E1 in the retentate collecting line LCR.
- the permeate of the first treatment stage E1 comprising C0 2 and residual natural gas is recovered via the permeate outlet SP of each membrane module M of the first treatment stage E1 in the LTP permeate transfer line. This permeate is then introduced into the membrane modules M of the second treatment stage E2 via their input EM via the transfer input line LET.
- the membrane module (s) M of the second treatment stage E2 makes it possible to reduce the content of residual natural gas in the C0 2 by separating the residual natural gas from the C0 2 .
- the membrane module (s) M of the second treatment stage E2 therefore makes it possible to improve the quality of the C0 2 so that it can be injected into a petroleum deposit.
- the permeate of the second treatment stage E2 comprising C0 2 is recovered via the permeate outlet SP of each membrane module M of the second treatment stage E2 in the permeate collection line LCP.
- the retentate of the second treatment stage E2 comprising natural gas is recovered via the output of the retentate module SR of each membrane module M of the second treatment stage E2 in the retentate transfer line LTR. This retentate is then introduced into each membrane module M of the first treatment stage E1 via the feed line LA to increase the amount of purified natural gas recovered in the LCR retentate collection line.
- the purified natural gas recovered in the LCR retentate collection line may be marketed after possible subsequent treatments.
- the C0 2 recovered in the permeate collection line LCP can be injected into a petroleum deposit.
- the permeate of the second treatment stage E2 may comprise more than 75 mol%. of C0 2 , in particular of 80 mol%. at 99 mol%. of C0 2 , especially 94% mol. at 97 mol% C0 2 ,
- the retentate of the first treatment stage E1 may comprise more than 75 mol%. natural gas, in particular 80 mol%. at 99 mol%. natural gas, especially 94 mol%. at 95 mol%. of natural gas.
- the permeate of the second treatment stage E2 comprising CO 2 can be re-injected into a petroleum deposit.
- the retentate of the first treatment stage E1 comprising natural gas may be marketed.
- the permeate method may further comprise increasing the pressure of the permeate recovered via the permeate outlet SP of the membrane module M of the first treatment stage E1 in the permeate transfer line LTP.
- the method according to the retentate mode further comprises increasing the pressure of the permeate recovered via the permeate outlet SP of the membrane module M of the first treatment stage E1 in the permeate collection line LCP.
- all the membrane modules M for the first and second treatment stages E1, E2 are pooled.
- the method comprises a stage reassignment step requiring more membrane surface of at least one membrane module M assigned to the stage requiring less membrane surface.
- the membrane surface of each of the treatment stages depends on the number of membrane modules M allocated to each stage.
- the number of membrane modules M to be reassigned from one stage to another may depend on the C0 2 content in natural gas, mainly the increase in this content, but may also depend on the decrease or variation in this content.
- the number of membrane modules M of the floor requiring less membrane surface to be reassigned to the floor requiring more membrane surface may also depend on the evolution of the pressure of the natural gas.
- the step of reallocating the process that is the subject of the present invention makes it possible to modulate the membrane surface required by each treatment stage and thus to optimize the total membrane surface of the plant I.
- the total membrane surface installed can be decreased.
- the step of reallocating the process makes it possible to optimize the power consumed by the method (see the examples).
- the reallocation of membrane modules M according to the needs is not necessarily carried out continuously, but is preferably carried out in steps, the steps corresponding for example to the intervals (in% mol.) Of C0 2 content of the gas to be treated. following:] 10; 20]; ] 20; 30] ; ]30 ; 40]; ] 40; 50]; ] 50; 60]; ] 60; 70]; and] 70; 80]
- Others bearings may be provided, for example in place of the bearings] 30; 40]; ] 40; 50] and] 50; 60], it is possible to have] 30; 44]; ] 44; 60] instead (1 step less).
- a bypass of the second permeate treatment stage or of the first retentat treatment stage may be provided. This bypass takes a portion of the gas arriving at the inlet of the second treatment stage E2 in permeate mode or the first treatment stage El in retentate mode to direct it to the LCP permeate collection line.
- a bypass of the first permeate processing stage or the second retentat processing stage may be provided. This bypass takes a portion of the gas arriving at the entrance of the first treatment stage El in permeate mode or the second treatment stage E2 in retentate mode to direct it directly to the collection line of the retentate LCR.
- the reallocation step of the process of the invention can be implemented when the content of C0 2 in the natural gas reaches a threshold value, Tco2 Sem1 ⁇
- the threshold value Tco2 Seml depends on various parameters such as the pressure of CO 2 , the content of C0 2 , the specifications, the membrane system, the performance of the membranes ....
- the threshold value T C o2 Seml is 10 mol%. at 75 mol%, especially 20 mol%. at 60 mol%, especially 30 mol%. at 50 mol%.
- the method may comprise increasing the pressure of the permeate which is recirculated, in particular via the recycle compressor CompTR, that is to say the pressure of the permeate recovered at the permeate outlet SP of the second treatment stage E2, in which case the method may further comprise injecting the compressed permeate, in particular via the CompTR recycle compressor, at the inlet of the first treatment stage El.
- the method may furthermore comprise increasing the pressure of the permeate recovered at the permeate outlet SP of the first treatment stage E1. This compressed permeate, in particular via the CompTP reinjection compressor, comprising C0 2 can then be injected into a deposit. oil.
- the increase in permeate pressure can be achieved by decreasing the speed of rotation of the CompTR recycle compressor or by changing the orientation of the bladders of the CompTR recycle compressor.
- the increase in permeate pressure can be achieved by decreasing the rotational speed of the CompTP feedback compressor or by changing the orientation of the blades of the CompTP feedback compressor.
- the permeate pressure at the permeate outlet SP of the membrane module M of the first treatment stage E1 can be from 0.1 bar to 10 bar, in particular from 1 bar to 7 bar, more particularly from 1.5 bar to 5 bar.
- the permeate pressure at the permeate outlet SP of the membrane module M of the second treatment stage E2 can be from 0.1 bar to 10 bar, in particular from 1 bar to 7 bar, more particularly from 1.5 bar to 5 bar.
- the inlet pressure EM of the membrane module M of the first treatment stage E1 or of the membrane module M of the second treatment stage E2 can be from 20 bar to 120 bar, in particular from 40 bar to 100 bar, more particularly from 60 bar to 90bar.
- the reassignment stage of the second treatment stage E 2 to the first processing stage E1 comprises the following steps: the fluidic disconnection of the input EM, the retentate output SR and the permeate output SP of the membrane module or modules M to be reassigned; the fluidic connection of the input EM of the membrane module (s) M to reassign to the power supply line LA;
- the step of reallocating one or more membrane modules M from the second processing stage E2 to the first processing stage E1 can be implemented very simply in the following manner.
- each membrane module M to be reassigned can be achieved by closing the open valves which establish the fluidic connection:
- each membrane module M to be reassigned can be achieved by opening the closed valves establishing the fluidic connection:
- the step of reassigning the first treatment stage El to the second stage of treatment E2 comprises the following steps:
- the step of reallocating one or more membrane modules M from the first treatment stage E1 to the second treatment stage E2 can be implemented very simply, in particular by means of the valve system SV, in the following manner.
- each membrane module M to be reassigned can be achieved by closing the open valves which establish the fluidic connection:
- each membrane module M to be reassigned can be achieved by opening the closed valves establishing the fluidic connection:
- the first treatment stage El and the second treatment stage E2 are fluidically connected in permeate mode.
- the realignment step of the process of the invention can be carried out when the C0 2 content in the natural gas reaches a threshold value, T C o 2.
- the threshold value T C o 2 Seml depends on various parameters such as C0 2 pressure, the content of C0 2, the specifications, the membrane system, the membrane performance ....
- the tCO2 SEML threshold value is 10% mol. at 75 mol%, especially 20 mol%. at 60 mol%, especially 30 mol%. at 50 mol%.
- the method may comprise increasing the pressure of the permeate recovered at the permeate outlet SP of the first treatment stage E1, in particular via the recirculation compressor CompTR, in which case the process may also comprise the injection of the compressed permeate via the compressor COMPTR recycle at the entrance of the second stage of treatment E2.
- the method may furthermore comprise increasing the pressure of the permeate recovered at the permeate outlet SP of the second treatment stage E2, in particular via the CompTP reinjection compressor.
- This permeate compressed via CompTP reinjection compressor comprising C0 2 can then be injected into a petroleum deposit.
- the increase in permeate pressure can be achieved by decreasing the speed of rotation of the CompTR recycle compressor or by changing the orientation of the bladders of the CompTR recycle compressor.
- the increase in permeate pressure can be achieved by decreasing the rotational speed of the CompTP feedback compressor or by changing the orientation of the blades of the CompTP feedback compressor.
- the permeate pressure at the permeate outlet SP of the membrane module M of the first treatment stage E1 can be from 0.1 bar to 10 bar, in particular from 1 bar to 7 bar, more particularly from 1.5 bar to 5 bar.
- the permeate pressure at the permeate outlet SP of the membrane module M of the second treatment stage E2 may be from 0.1 bar to 10 bar, in particular from 1 bar to 7 bar, more particularly from 15 bar to 5 bar.
- the inlet pressure EM of the membrane module M of the first treatment stage E1 or of the membrane module M of the second treatment stage may be from 20 bar to 120 bar, in particular from 40 bar to 100 bar, in particular from 60 bar to 90 bar. bar.
- the step of reassigning the first treatment stage El to the second stage of treatment E2 comprises the following steps:
- the step of reassigning the first processing stage E1 to the second processing stage E2 can be implemented very simply by means of the valve system SV in the following manner.
- each membrane module M to be reassigned can thus be achieved by closing the open valves which establish the fluidic connection: between the input EM of each membrane module M to reassign and the feed line LA,
- each membrane module M to be reassigned can be achieved by opening the closed valves establishing the fluidic connection:
- the step of reassigning the second treatment stage E 2 to the first treatment stage E 1 comprises the steps following:
- the step of reallocating one or more membrane modules M from the second processing stage E2 to the first processing stage E1 can be implemented very simply in the following manner.
- each membrane module M to be reassigned can be achieved by closing the open valves which establish the fluidic connection:
- each membrane module M to be reassigned can be achieved by opening the closed valves establishing the fluidic connection:
- the treatment of natural gas is carried out either in the retentate mode (FIGS. 1a and 3a to 3c), sometimes in the permeate mode (FIGS. 1b and 4a to 4c) as described above.
- the natural gas treatment is first carried out the retentate mode. Then, when the content of CO 2 present in the natural gas reaches a given value, the treatment of natural gas is carried out according to the permeate mode. In a second variant, the treatment of natural gas is carried out according to the permeate mode. Then when the content of C0 2 present in the natural gas reaches a given value, the treatment of natural gas is carried out according to the retentate mode.
- the method according to the second aspect of the invention comprises a step of passing from one operating mode to another.
- this method makes it possible to benefit from the advantages of the two operating modes as a function of the evolution of the CO 2 content in the natural gas to be treated. Indeed, when the C0 2 content in the gas to be treated is less than T C o2 decl, the permeate mode is more advantageous in terms of membrane area and power consumption. When the content of C0 2 is greater than Tco2 decl, then the retentate mode becomes more economical in terms of membrane surface and the consumed power becomes stable. In addition, by combining the two procedures, the total membrane surface to be installed is lower than using either of the two operating modes alone and the total power consumed is stabilized.
- Tco2 decl The given value, Tco2 decl , of the content of C0 2 present in the natural gas that triggers the gas treatment according to the retentate mode or the permeate mode depends on various parameters such as the pressure of C0 2 , the content of C0 2 , specifications, membrane system, membrane performance ...
- Tco2 decl can be 20 mol%. at 80 mol%, in particular 30 mol%. at 70 mol%, especially 40 mol%. at 60 mol%.
- the membrane modules M are connected as described above (1.2.).
- the step from permeate to retentate can be carried out very simply thanks to the valve system SV described above in connection with the method according to the first aspect of the invention.
- each membrane module M can thus be realized by closing the open valves which make the fluidic connection:
- each membrane module M can thus be made by opening the closed valves that make the fluid connection between:
- the other membrane modules M that are not reconnected remain isolated.
- the transition from retentate to permeate mode can be achieved by: disconnecting the input EM from at least a portion of the membrane modules M from the first processing stage E1 of the supply line LA and connecting them to the transfer input line LET, thereby assigning them to the second stage of treatment E2 permeate mode, the other part, if there is membrane modules M of the first treatment stage El being isolated;
- transition from retentate to permeate mode can be achieved by:
- membrane modules M reused after switching to permeate mode are never fully insulated allowing savings in closing operation and opening of valves.
- the CO 2 content in the natural gas may require a total required membrane surface S r , the membrane modules M providing a total available surface, when the total available membrane area exceeds the total area required for the separation of C0 2 , while the permeate pressure can be increased on any of the stages of the installation I.
- This pressure increase can be achieved by CompTR recycle compressors or CompTP recompression compressors.
- the step from permeate to retentate can be carried out very simply thanks to the valve system SV described above in connection with the method according to the first aspect of the invention.
- each membrane module M can thus be realized by closing the open valves which make the fluidic connection:
- each membrane module M can thus be made by opening the closed valves that make the fluid connection between:
- the other membrane modules M that are not reconnected remain isolated.
- the transition from permeate mode to retentate mode can be achieved by:
- the transition from permeate mode to retentate mode can be achieved by:
- the CO 2 content in the natural gas may require a total required membrane surface S r , the membrane modules EM providing a total available surface, when the total available membrane area exceeds the total area required for the separation of C0 2 , then the permeate pressure can be increased on any of the stages of the installation. This pressure increase can be achieved by CompTR recycle compressors or CompTP recompression compressors.
- modules Membrane M can be reassigned from one of the treatment stages to another.
- the skilled person will achieve all the embodiments by combining the different steps described above.
- Natural gas initially contains about 10 mol%. of C0 2 , then its C0 2 content of natural gas is increased to 80 mol%. by injection of C0 2 in the deposit.
- MMSCFD means "million standard cubicfeet per day" and is 1177.17 Sm 3 / h at 15 ° C.
- Example 1 A process that only implements the retentate mode
- Figure 7 shows the evolution of the required membrane surfaces (in base 100, 100 being the membrane surface required in total to be installed at the beginning of treatment for a gas comprising approximately 10 mol% of C0 2 ) for the first treatment stage El the second treatment stage E2 and the effective total membrane surface as a function of the CO 2 content in the gas to be treated for the retentate mode.
- the required membrane area of the first treatment stage E 1 increases from 2 to 34, thus allowing better separation of the gases at this stage and thus inducing less membrane surface for the second treatment stage E 2 which decreases from 98 to almost 0.
- the total membrane surface therefore decreases when the content of CO 2 increases in the gas to be treated.
- the membrane unit is constructed with membrane modules having a fixed surface. Arbitrary, it is assumed that a membrane module has a surface of 1 in base 100.
- the total number of membrane modules to be installed is 98 for the second treatment stage and 34 for the first treatment stage, which makes a total number of membrane modules to install from 132.
- Figure 8 shows the evolution of the total power consumed (in base 100, 100 being the total power consumed maximum permeate mode at the end of field life) by the recycle compressor in the membrane process but also for the reinjection compressor for the reinjection of C0 2 in the field.
- the power for the feedback compressor increases as the C0 2 flow rate increases.
- the flow rate to be recycled at the second treatment stage decreases because the The amount of hydrocarbon is decreasing in the field and the separation of gases at the first stage of treatment is becoming more efficient, which explains a decrease in the power consumed by the recycle compressor.
- the total power consumed remains relatively stable throughout the life of the field.
- FIG. 9 shows the evolution of the required membrane surfaces (in base 100, same base as Example 1) for the first treatment stage E1, the second treatment stage E2 and the total effective membrane surface and to be installed according to of the CO 2 content in the gas to be treated for the permeate mode.
- the membrane surface of the first treatment stage increases (with a maximum at about 30% relative to the initial value) and then decreases with the increase of the CO 2 content in the gas to be treated.
- the minimum membrane area required is 37 and the maximum required membrane area is 49 for the first treatment stage (base 100, same base as for Example 1).
- the membrane surface of the second treatment stage increases, for its part, continuously because the quantity of CO 2 to be removed increases in the time from 1 to 28 (in base 100).
- the total membrane surface to be installed if there is no reallocation of membrane modules from one treatment stage to another is 77 (base 100).
- the membrane surface to be installed for this process is less than Example 1.
- Example 3 Process Comprising Reassignment Steps for Membrane Modules and a Stage for Passing Permeate Mode to Retentate Mode
- the installation I implementing the method comprises 66 membrane modules M (in base 100, same basis as for Example 1).
- Table 2 Evolution of the allocation of the membrane modules M and the operating mode of the installation I as a function of the CO 2 content in the natural gas to be treated.
- the plant I operates according to the permeate mode, 46 membrane modules M are assigned to the first treatment stage E1, 6 membrane modules M are assigned to the second treatment stage E2 and 14 membrane modules M are isolated, the. they are not fluidly connected.
- an isolated membrane module M is reassigned to the first treatment stage E1 and 6 isolated membrane modules M are reassigned to the second treatment stage E2, all the membrane modules M are then used.
- a permeate step 50 membrane modules M at the first treatment stage El and 16 modules membrane M at the second stage of treatment E2 of the permeate mode
- the retentate mode (16 membrane modules M at the first treatment stage E1 and 50 membrane modules M at the second treatment stage E2 of the retentate mode) is produced by inverting the treatment stages.
- This step is followed by a step of reallocating a membrane module M from the second treatment stage E2 to the first treatment stage E1.
- 44% mol. at 60 mol% 17 membrane modules M are assigned to the first treatment stage E1 and 49 membrane modules M are assigned to the second treatment stage E2.
- the step of reallocating a membrane module M can be performed before the step of permeate mode to retentate mode.
- a membrane module M of the first treatment stage E1 is first reassigned to the second treatment stage E2, then the two treatment stages are inverted to carry out the transition from the permeate mode to the retentate mode.
- the combined use of the two procedures as well as the transfer of membrane modules M from one treatment stage to the other makes it possible to limit the total membrane surface installed to 66 (in base 100) and to optimal use of the total membrane surface installed.
- the optimization of the installed membrane surface induces a gas separation quality higher than that required.
- the combined use of the two operating modes as well as the transfer of membrane modules M from one stage to the other makes it possible to limit the total power consumed, ie the total power necessary for the operation of the process. Indeed, the total power consumed is less than that of both Examples 1 and 2.
- a bypass may be realized, it can be a bypass of the first stage of treatment in retentate mode in order to deplete the gas to reinject in C0 2 and / or a bypass of the second stage of treatment still in retentate mode in order to enrich the gas recovered at the end treatment in C0 2 .
- the specifications are reached for the gas to be reinjected and the gas recovered at the end of the treatment.
- the expected specifications are exceeded: the gas to be reinjected contains more than 96 mol%. of C0 2 instead of 95 mol%. and the gas recovered at the end of the treatment only contains 2.4% mol. of C0 2 instead of 5 mol%.
- the total membrane surface to be installed according to Example 3, and thus invested corresponds to 66 (in base 100) whereas the required surface area appears in stages to be unused when the required surfaces are less than the surface. total membrane to install.
- the membrane modules corresponding to this difference are then isolated and condemned and represent an unexploited capital. There is therefore interest in taking advantage of these unused surfaces. It is then possible to operate on the pressure of the permeate at the outlet of one or both stages of treatment in order to meet the specifications of the acid gas and the treated gas while keeping a constant membrane surface (bearing) and realizing a gain on the power consumed.
- Table 3 below illustrates this option: for 70 mol%. of C0 2 in the gas to be treated, 52 membrane modules are required and the total power consumed is 56.1 (in base 100). When the content of C0 2 reaches 80 mol%, the 52 membrane modules are kept in use and the pressure of the permeate (initially set at 1.8 bar, see penultimate column) of the two treatment stages (respectively 5, 4 bar and 2.2 bar for first and second treatment stage, see last column). A 7% bypass of the gas is required on the first stage of treatment to meet the specification on the gas to be reinjected. In the end, we reduce the power consumed by 16%. Note that this calculation is done for illustration on a single level but the principle remains the same for all levels, saving energy will be higher on average.
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/FR2018/050118 WO2019141909A1 (fr) | 2018-01-17 | 2018-01-17 | Procede de traitement d'un gaz naturel contenant du dioxyde de carbone |
AU2018402639A AU2018402639B2 (en) | 2018-01-17 | 2018-01-17 | Process for treating a natural gas containing carbon dioxide |
US16/963,142 US11389764B2 (en) | 2018-01-17 | 2018-01-17 | Process for treating a natural gas containing carbon dioxide |
BR112020014475-4A BR112020014475A2 (pt) | 2018-01-17 | 2018-01-17 | métodos e instalação para processamento de um gás natural contendo dióxido de carbono |
ARP190100090A AR114509A1 (es) | 2018-01-17 | 2019-01-17 | Procedimiento para tratar un gas natural que contiene dióxido de carbono |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/FR2018/050118 WO2019141909A1 (fr) | 2018-01-17 | 2018-01-17 | Procede de traitement d'un gaz naturel contenant du dioxyde de carbone |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2019141909A1 true WO2019141909A1 (fr) | 2019-07-25 |
Family
ID=61168124
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2018/050118 WO2019141909A1 (fr) | 2018-01-17 | 2018-01-17 | Procede de traitement d'un gaz naturel contenant du dioxyde de carbone |
Country Status (5)
Country | Link |
---|---|
US (1) | US11389764B2 (fr) |
AR (1) | AR114509A1 (fr) |
AU (1) | AU2018402639B2 (fr) |
BR (1) | BR112020014475A2 (fr) |
WO (1) | WO2019141909A1 (fr) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP3892357A1 (fr) * | 2020-04-09 | 2021-10-13 | L'air Liquide Société Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Installation pour le traitement par perméation membranaire de biogaz avec adaptation de la surface membranaire en fonction de la pression de biogaz |
EP3981500A1 (fr) * | 2020-10-09 | 2022-04-13 | NeuroBodyTech GmbH | Système et procédé de séparation de gaz comprenant un système de membranes et une vanne de contrôle |
US11851625B2 (en) | 2021-05-20 | 2023-12-26 | Saudi Arabian Oil Company | Reservoir management by controlling acid gas build-up in reservoir by partial CO2 removal processes |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4152129A (en) | 1977-02-04 | 1979-05-01 | Trentham Corporation | Method for separating carbon dioxide from methane |
US20070125537A1 (en) * | 2005-12-02 | 2007-06-07 | Membrane Technology And Research Inc. | Natural gas treatment process for stimulated well |
US20110009684A1 (en) * | 2008-01-08 | 2011-01-13 | Shell Internationale Research Maatschappij B.V. | Multi-stage membrane separation process |
US20120000355A1 (en) * | 2010-06-30 | 2012-01-05 | Uop Llc | Flexible System To Remove Carbon Dioxide From A Feed Natural Gas |
US20170327758A1 (en) * | 2014-12-04 | 2017-11-16 | Mitsubishi Heavy Industries, Ltd. | Natural gas refining apparatus and system |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6645380B2 (en) * | 2001-12-19 | 2003-11-11 | Petro Sep International Ltd. | Membrane separation apparatus |
US8192524B2 (en) * | 2009-01-29 | 2012-06-05 | Chevron U.S.A. Inc. | Process for upgrading natural gas with improved management of CO2 |
JP5830989B2 (ja) * | 2011-07-08 | 2015-12-09 | 宇部興産株式会社 | 混合ガス分離装置 |
US9714925B2 (en) * | 2014-11-20 | 2017-07-25 | Saudi Arabian Oil Company | Simulataneous gas chromatograph analysis of a multi-stream natural gas upgrade generated through a multi-membrane process |
US10843127B2 (en) * | 2017-11-15 | 2020-11-24 | Generon Igs, Inc. | Compact membrane module system for gas separation |
-
2018
- 2018-01-17 AU AU2018402639A patent/AU2018402639B2/en active Active
- 2018-01-17 BR BR112020014475-4A patent/BR112020014475A2/pt active Search and Examination
- 2018-01-17 WO PCT/FR2018/050118 patent/WO2019141909A1/fr active Application Filing
- 2018-01-17 US US16/963,142 patent/US11389764B2/en active Active
-
2019
- 2019-01-17 AR ARP190100090A patent/AR114509A1/es active IP Right Grant
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4152129A (en) | 1977-02-04 | 1979-05-01 | Trentham Corporation | Method for separating carbon dioxide from methane |
US20070125537A1 (en) * | 2005-12-02 | 2007-06-07 | Membrane Technology And Research Inc. | Natural gas treatment process for stimulated well |
US20110009684A1 (en) * | 2008-01-08 | 2011-01-13 | Shell Internationale Research Maatschappij B.V. | Multi-stage membrane separation process |
US20120000355A1 (en) * | 2010-06-30 | 2012-01-05 | Uop Llc | Flexible System To Remove Carbon Dioxide From A Feed Natural Gas |
US20170327758A1 (en) * | 2014-12-04 | 2017-11-16 | Mitsubishi Heavy Industries, Ltd. | Natural gas refining apparatus and system |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP3892357A1 (fr) * | 2020-04-09 | 2021-10-13 | L'air Liquide Société Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Installation pour le traitement par perméation membranaire de biogaz avec adaptation de la surface membranaire en fonction de la pression de biogaz |
FR3109101A1 (fr) * | 2020-04-09 | 2021-10-15 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Installation pour le traitement par perméation membranaire de biogaz avec adaptation de la surface membranaire en fonction de la pression de biogaz |
EP3981500A1 (fr) * | 2020-10-09 | 2022-04-13 | NeuroBodyTech GmbH | Système et procédé de séparation de gaz comprenant un système de membranes et une vanne de contrôle |
US11779880B2 (en) | 2020-10-09 | 2023-10-10 | 12M Invent Gmbh | Gas separation system and gas separation method |
US11851625B2 (en) | 2021-05-20 | 2023-12-26 | Saudi Arabian Oil Company | Reservoir management by controlling acid gas build-up in reservoir by partial CO2 removal processes |
Also Published As
Publication number | Publication date |
---|---|
BR112020014475A2 (pt) | 2020-12-01 |
AU2018402639A1 (en) | 2020-07-23 |
AR114509A1 (es) | 2020-09-16 |
US11389764B2 (en) | 2022-07-19 |
US20210236986A1 (en) | 2021-08-05 |
AU2018402639B2 (en) | 2021-06-10 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2019141909A1 (fr) | Procede de traitement d'un gaz naturel contenant du dioxyde de carbone | |
EP1890961B1 (fr) | Procede pour la production simultanee d'hydrogene et de monoxyde de carbone | |
FR2540396A1 (fr) | Procede de deshydratation de gaz | |
FR2904821A1 (fr) | Procede de purification d'hydrogene | |
FR2852310A1 (fr) | Procede et systeme de purification d'eau, ainsi que module pour un tel systeme | |
FR2953505A1 (fr) | Procede pour une production d'hydrogene combinee a une capture de dioxyde de carbone | |
EP0358551B1 (fr) | Procédé et installation de séparation d'un constituant d'un mélange gazeux | |
WO2011135538A2 (fr) | Procede de traitement d'un gaz naturel contenant du dioxyde de carbone | |
CA2136659A1 (fr) | Procede et installation de fourniture d'azote au moyen de membranes semi-permeables utilisant une geometrie membranaire variable | |
EP0770576A1 (fr) | Procédé et installation de production d'hydrogène et d'énergie | |
FR2961802A1 (fr) | Procede de production d'hydrogene combinee a une capture de dioxyde de carbone | |
EP0465298A1 (fr) | Procédé et installation de production d'un composant gazeux à partir d'un mélange gazeux | |
EP1018488A1 (fr) | Procédé et installation de production de monoxyde de carbone | |
WO2013164541A2 (fr) | Production d'energie par osmose directe | |
FR2969136A1 (fr) | Procede pour une production de monoxyde de carbone avec alimentation de boite froide stabilisee | |
EP3613493A1 (fr) | Traitement par perméation membranaire avec ajustement du nombre de membranes mises en oeuvre en fonction de la pression du flux gazeux d'alimentation | |
EP4368274A1 (fr) | Procede de traitement d'un gaz issu d'un gisement pour obtenir de l'helium et systeme de mise en oeuvre d'un tel procede | |
WO2023041755A1 (fr) | Unité d'épuration de biogaz | |
WO2020239707A1 (fr) | Installation de filtration membranaire de liquides et procede de production d'eau potable avec celle-ci sans post-mineralisation | |
EP3964280B1 (fr) | Dispositif de régulation d'une installation pour le traitement par perméation membranaire de biogaz | |
WO2023002038A1 (fr) | Dispositif et procédé de séparation d'un mélange gazeux comportant au moins du gaz naturel et du dihydrogène | |
EP3892357A1 (fr) | Installation pour le traitement par perméation membranaire de biogaz avec adaptation de la surface membranaire en fonction de la pression de biogaz | |
FR3106136A1 (fr) | Procédé de dégazolinage d’un gaz contenant des hydrocarbures condensables | |
WO2018224763A1 (fr) | Méthode de purification de gaz naturel mettant en oeuvre des membranes | |
WO2024064250A1 (fr) | Système et procédé améliorés de récupération de gaz combustible à partir d'une purification de pétrole brut |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 18703617 Country of ref document: EP Kind code of ref document: A1 |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
ENP | Entry into the national phase |
Ref document number: 2018402639 Country of ref document: AU Date of ref document: 20180117 Kind code of ref document: A |
|
REG | Reference to national code |
Ref country code: BR Ref legal event code: B01A Ref document number: 112020014475 Country of ref document: BR |
|
ENP | Entry into the national phase |
Ref document number: 112020014475 Country of ref document: BR Kind code of ref document: A2 Effective date: 20200715 |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 18703617 Country of ref document: EP Kind code of ref document: A1 |