WO2011080405A1 - Procede d'elimination de composes acides d'un effluent gazeux avec une solution absorbante a base de diamines - Google Patents
Procede d'elimination de composes acides d'un effluent gazeux avec une solution absorbante a base de diamines Download PDFInfo
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- WO2011080405A1 WO2011080405A1 PCT/FR2010/000785 FR2010000785W WO2011080405A1 WO 2011080405 A1 WO2011080405 A1 WO 2011080405A1 FR 2010000785 W FR2010000785 W FR 2010000785W WO 2011080405 A1 WO2011080405 A1 WO 2011080405A1
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- dimethyl
- propanediamine
- gas
- absorbent solution
- diamine
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- 0 CN(*)C(*)(*)C(*)C(*)(*)CN* Chemical compound CN(*)C(*)(*)C(*)C(*)(*)CN* 0.000 description 1
Classifications
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- 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
- B01D53/14—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 absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
-
- 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
- B01D53/14—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 absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/2041—Diamines
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20426—Secondary amines
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20431—Tertiary amines
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20436—Cyclic amines
- B01D2252/20452—Cyclic amines containing a morpholine-ring
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/304—Hydrogen sulfide
Definitions
- the present invention relates to the elimination of acidic compounds (H 2 S, CO 2 , COS, CS 2 , mercaptans, etc.) in a gaseous effluent by means of an absorbent aqueous solution comprising diamines.
- the invention is advantageously applicable to the treatment of gas of industrial origin and natural gas.
- gaseous effluents that can be treated is various, and may be mentioned without limitation the synthesis gases, the combustion fumes, the refinery gases, the gases obtained at the bottom of the Claus process, the fermentation gases of biomass, cement gases and blast furnace gases.
- All these gases contain acidic compounds such as, for example, carbon dioxide (C0 2 ), hydrogen sulphide (H 2 S), carbon oxysulfide (COS), carbon disulphide (CS 2 ) and mercaptans.
- acidic compounds such as, for example, carbon dioxide (C0 2 ), hydrogen sulphide (H 2 S), carbon oxysulfide (COS), carbon disulphide (CS 2 ) and mercaptans. (SH), mainly methyl mercaptan (CH 3 SH), ethyl mercaptan (CH 3 CH 2 SH) and propylmercaptans (CH 3 CH 2 CH 2 SH).
- the gaseous effluent contains nitrogen, CO 2 , oxygen and some sulfur or nitrogen impurities.
- CO 2 is the acid compound that is to be removed.
- carbon dioxide is one of the greenhouse gases largely produced by different human activities and has a direct impact on air pollution.
- a post-combustion C0 2 capture unit aims to reduce by 90% the C0 2 emissions of a thermal power station.
- Decarbonation is generally carried out by washing the gas with an absorbent solution containing one or more amines.
- the gaseous effluent contains carbon monoxide CO, hydrogen H 2 , water vapor and carbon dioxide C0 2 . It contains, in addition, sulfur (H 2 S, COS, etc.), nitrogen (NH 3 , HCN) and halogenated impurities which must be removed so that the gas contains only residual levels.
- the impurities present in the unpurified synthesis gas can lead to accelerated corrosion of the plants and are likely to poison the catalysts used for chemical synthesis processes such as those used in the Fischer-Tropsch synthesis or methanol, or mitigate the performance of materials used in fuel cells.
- Environmental considerations also require the removal of impurities present in the gases.
- the input specifications of the Fischer-Tropsch unit are particularly severe, the contents present in the synthesis gas generally being less than 10 ppb weight for the sulfur impurities.
- the gas is generally washed with an absorbent solution containing amines, combined with the use of capture masses.
- the deacidification of natural gas aims to eliminate acid compounds such as carbon dioxide (C0 2 ), but also hydrogen sulphide (H 2 S), carbon oxysulfide (COS), carbon disulphide (CS 2 ) and mercaptans (RSH), mainly methyl mercaptan (CH 3 SH), ethyl mercaptan (CH 3 CH 2 SH) and propyl mercaptans (CH 3 CH 2 CH 2 SH).
- the specifications generally carried out on the deacidified gas are 2% of C0 2 , or even 50 ppm volume of C0 2 to subsequently liquefy the natural gas; 4 ppm H 2 S, and 10 to 50 ppm volume of total sulfur.
- Deacidification is therefore often carried out first, in particular in order to eliminate toxic acid gases such as H 2 S in the first stage of the process chain and to avoid the pollution of the different unit operations by these acidic compounds. including the dehydration section and the heavier hydrocarbon condensation and separation section.
- the deacidification is generally carried out by washing the gas with an absorbent solution containing one or more amines.
- natural gases with various acid gas compositions can be found.
- gases containing mainly only rH 2 S, or only CO 2 "or these two gases in a mixture In addition, one can find very rich natural gas (up to 40% vol.) Or very poor (a hundred ppm.) In acid compounds.
- the operator who is brought to deacidify this gas must take into account transport specification constraints (2% C0 2 for a pipeline transport, and 50 ppm volume for a transport by ship after liquefaction) and constraints related to other units in the gas processing chain (eg a Claus-type unit converting toxic H 2 S to inert sulfur, does not tolerate more than 65% C0 2 ).
- transport specification constraints 2% C0 2 for a pipeline transport, and 50 ppm volume for a transport by ship after liquefaction
- constraints related to other units in the gas processing chain eg a Claus-type unit converting toxic H 2 S to inert sulfur, does not tolerate more than 65% C0 2 ).
- the operator may be required to carry out a total deacidification (C0 2 and H 2 S), a selective deacidification of H 2 S, or even a deacidification followed by an enrichment step acid gas in H 2 S.
- the deacidification of the gaseous effluents is generally carried out by washing with an absorbent solution.
- the absorbent solution makes it possible to absorb the acidic compounds present in the gaseous effluent (in particular C0 2 , H 2 S, mercaptans, COS, CS 2 ).
- acidic effluents comprising acidic compounds such as, for example, H 2 S, C0 2 , mercaptans, COS, SO 2 , CS 2
- acidic compounds such as, for example, H 2 S, C0 2 , mercaptans, COS, SO 2 , CS 2
- the use of amine-based compounds is advantageous. because of their ease of use in aqueous solution.
- the solvents commonly used today are aqueous solutions of primary, secondary or tertiary alkanolamine, in combination with a possible physical solvent.
- document FR 2 820 430 can be cited which proposes processes for deacidification of gaseous effluents.
- US Pat. No. 6,852,144 describes a method for removing acidic compounds from hydrocarbons. The method uses a water-methyldiethanolamine or water-triethanolamine absorbent solution containing a high proportion of a compound belonging to the following group: piperazine and / or methylpiperazine and / or morpholine.
- Patent US 4240923 recommends the use of so-called sterically hindered amines for removing acidic compounds from a gaseous effluent comprising, these amines having in particular advantages in terms of absorption capacity and regeneration energy.
- the structures described are in particular nitrogen heterocyclics derived from piperidine, the position of which at the nitrogen atom is congested by an alkyl or alcohol group in particular.
- the absorbed C0 2 reacts more or less rapidly with the alkanolamine present in solution according to a reversible exothermic reaction, well known to those skilled in the art and leading to the formation of hydrogenocarbonates , carbonates and / or carbamates, allowing removal of CO 2 in the gas to be treated.
- the absorbed H 2 S reacts instantaneously with the alkanolamine present in solution according to a reversible exothermic reaction, which is well known to a person skilled in the art and leading to to the formation of hydrogen sulfide.
- H 2 S enrichment unit is needed to concentrate the acid gas in H 2 S.
- the most selective amine will be sought.
- Tertiary amines such as Methyldiethanolamine, or hindered with slow reaction kinetics with C0 2 are commonly used, but have limited selectivities at high H 2 S loading rates.
- the dimensioning of the absorption column is crucial to ensure the proper functioning of the unit. capture of C0 2 is a criterion determining the column height, the cyclic capacity of the solvent is a criterion determining the diameter of the column. Indeed, the more the solvent has a high cyclic capacity, the lower the flow of solvent required to treat the acid gas will be. Thus, the lower the flow of solvent to circulate in the column, the smaller the diameter of the absorption column can be, without the occurrence of clogging phenomenon of the column. In an application where the absorption column is under pressure, such as the treatment of natural gas or synthesis gas, the diameter of the column has a huge impact on the steel mass constituting the absorption column, and therefore its cost.
- the last item concerns the energy to be supplied to break the bond created between the amine used and the C0 2 .
- To reduce the energy consumption associated with the regeneration of the solvent it is therefore preferable to minimize the ⁇ linkage enthalpy.
- the best solvent from an energy point of view is therefore that which will have the best compromise between a strong cyclic capacity ⁇ and a low enthalpy of connection ⁇ .
- the present invention therefore aims to overcome one or more of the disadvantages of the prior art by providing a method for removing acidic compounds, such as C0 2 , H 2 S, COS, CS 2 , S0 2 and mercaptans, a gas by the use of a specific amine whose absorbing properties are greater than those of the reference amines used in post-combustion C0 2 capture applications and in treatment applications.
- acidic compounds such as C0 2 , H 2 S, COS, CS 2 , S0 2 and mercaptans
- natural gas namely monoethanolamine (MEA) and methyldiethanolamine (MDEA) respectively.
- the present invention describes a process for removing the acidic compounds contained in a gaseous effluent, in which a step of absorption of the acidic compounds is carried out. contacting the effluent with an absorbent solution comprising:
- Each of the radicals R 1 and R 2 is independently selected from a C 1 -C 12 alkyl group or a C 1 -C 12 alkoxyalkyl group,
- Each of the radicals R3, R4, R5, R6 and R7 is chosen from a hydrogen atom, a C1-C12 alkyl group and a C1-C12 alkoxyalkyl group.
- R 1 and R 2 can be linked together to form a heterocycle of piperidine, pyrolidine, homopiperidine or morpholine type, the ring being composed of 5 to 8 atoms.
- the radical R3 may be chosen from a C1-C12 alkyl group and a C1-C12 alkoxyalkyl group.
- the diamine may be selected from the group consisting of (N-morpholinoethyl) isopropylamine, (N-piperidinoethyl) isopropylamine, [N, N-dimethyl-N '- (3-methoxypropyl)] -1,2 propanediamine, [N, N-dimethyl-N '- (methane-2-tetrahydrofurfuryl)] -1,2-propanediamine, [N, N-dimethyl-N' - (2-butyl)] - 1, 3-propanediamine, [N, N-dimethyl-N '- (2-butyl)] -1,3-propanediamine, [N, N-dimethyl-N'-butyl] -1,3-propanediamine, [N, N-dimethyl-N'-butyl] -1,3-propanediamine, [N, N-dimethyl-N '-butyl] -1,3-prop
- the primary or secondary amine function can be linked to at least one quaternary carbon or two tertiary carbons.
- the diamine may be selected from the group consisting of (N-morpholinoethyl) tert-butylamine, [N, N-dimethyl-N'-isopropyl] -1,2-propanediamine, [N, N- dimethyl-N'-tert-butyl] -1,2-propanediamine, [N, N-dimethyl-N'-tert-octyl] -1,2-propanediamine, [ ⁇ , ⁇ -dimethyl-N '- (2- butyl)] -1,2-propanediamine and [N, N-dimethyl-N'-tertbutyl] -1,3-propanediamine.
- the absorbent solution may comprise between 10% and 60% by weight of diamine and between 10 and 90% by weight of water.
- the absorbent solution may further comprise a non-zero amount and less than 20% by weight of an activator compound, said compound comprising a primary or secondary amine function.
- the activator compound may be selected from the group consisting of:
- the absorbent solution may further comprise a physical solvent selected from methanol and sulfolane.
- the absorption step of the acidic compounds can be carried out at a pressure of between 1 bar and 120 bar and at a temperature of between 20 ° C. and 100 ° C.
- a regeneration step of the absorbent solution loaded with acid compounds in which at least one of the following operations is carried out: heating, expansion, distillation.
- the regeneration step can be carried out at a pressure of between 1 bar and 10 bar and a temperature of between 100 ° C. and 180 ° C.
- the gaseous effluent may be chosen from natural gas, synthesis gases, combustion fumes, refinery gases, bottoms gases from the Claus process, biomass fermentation gases, cement gases, fumes. incinerator.
- the process according to the invention can be implemented for the selective removal of H 2 S from a gaseous effluent comprising H 2 S and CO 2 .
- the Applicant has discovered that the compounds corresponding to the definition of the diamines according to the invention make it possible to obtain larger cyclic capacities than the reference amines, both in applications where the partial pressure of acid gas is low (for example for the capture of C0 2 contained in combustion fumes), only in applications where the partial pressure of acid gas is high (for example the treatment of natural gas).
- This performance is certainly increased because of a higher density of amine sites relative to the molar mass of the molecules, but also of having on the same molecule, a primary or secondary amine function, and a tertiary function that can not form of carbamates.
- a primary or secondary amine function by varying the steric hindrance of the primary or secondary amine function, it is possible to obtain high performance amines both in total deacidification applications, and in applications where selective elimination of 'H 2 S.
- FIG. 1 showing a schematic diagram of a process for the treatment of effluents from acid gases.
- the invention relates to a method for absorbing acidic compounds from a gaseous effluent by contacting the gaseous effluent with a liquid absorbent solution comprising:
- the diamine in which the two amine functions are not linked together by cycles and whose amine function in position a is always tertiary and the amine function in position ⁇ is always either primary or secondary, this function being more or less hindered sterically depending on the intended application, the diamine corresponding to the following general formula (I) and conditioned by the rules specified below.
- R1 and R2 are selected from C1 to C12, preferably C1 to C6, alkyl and / or C1 to C12, preferably C1 to C6, alkoxyalkyl, linear, branched or cyclic.
- R 1 and R 2 are independently selected from a methyl group and an ethyl group.
- R 1 and R 2 are independent, that is to say that they are not interconnected.
- R 1 and R 2 can be linked together to form a heterocycle, for example of the piperidine, pyrolidine, homopiperidine or morpholine type, the ring consisting of 5 to 8 atoms, preferably a 5-membered ring or 6 atoms.
- R3 is selected from
- R3 is different from R1 and R2.
- R4, R5, R6 and R7 are indifferently chosen from hydrogen atoms or linear or branched or cyclic Cl to C12 alkyl or alkoxyalkyl groups.
- R4 and R5 are hydrogen atoms.
- R6 and R7 are independently selected from hydrogen and methyl.
- R3 is selected from C1 to C12 alkyl or alkoxyalkyl, preferably C1 to C6, linear, branched or cyclic.
- alkoxyalkyl group is intended to mean a hydrocarbon group containing one or more oxygen atoms, at least one of which is in the form of an ether function.
- the absorbing solution used in the process according to the invention does not have TMHDA.
- the absorbing solution used in the process according to the invention comprises a diamine according to the invention corresponding to the formula (I) previously described, with the exception of the alkyl derivatives of 1,6-hexanediamine.
- the alkyl derivatives of 1,6-hexanediamine denote compounds corresponding to formula (I) in which each of R 1 and R 2 is independently selected from an alkyl group containing from 1 to 4 carbon atoms and in which the radical R3 is chosen from a hydrogen atom or an alkyl group containing from 1 to 4 carbon atoms.
- the absorbing solution used in the process according to the invention comprises a diamine according to the invention corresponding to the formula (I) previously described, with the exception of the following compounds: N, N-dimethylhexane-1, 6-diamine and N, N, N'-trimethylhexane-1,6-diamine.
- the invention relates to a method for selectively removing H 2 S in a gas containing H 2 S and CO 2 .
- the diamine according to the invention is chosen such that the primary or secondary amine function is severely congested, that is to say that the primary or secondary amine function is connected to at least one quaternary carbon or two tertiary carbons.
- the severely hindered primary or secondary amine function is connected to a quaternary carbon, a quaternary carbon and a tertiary carbon, two tertiary carbons, or two quaternary carbons.
- the severely hindered diamine according to the invention comprises a secondary amine function.
- the compound of general formula (I) is such that the groups R6 and R.7 are hydrogens and the group R3 is a tert-butyl group
- (I) is such that the R6 group is a methyl group, the R7 group is hydrogen and the R3 group is an isopropyl group.
- the compound of general formula (I) is such that R3 is a hydrogen atom and where R6 and R7 are each a methyl radical.
- the compounds of general formulas (I) are of interest in all processes for treating acid gases (natural gas, combustion fumes, synthesis gas, etc.) in an aqueous absorbent solution composition.
- the present invention proposes to eliminate the acidic compounds of a gaseous effluent by using an absorbent compound in aqueous solution.
- the diamines according to the invention have a greater absorption capacity with acidic compounds (in particular CO 2 , H 2 S, COS, SO 2 , CS 2 and mercaptans) than monoethanolamine (MEA ) and methyldiethanolamine (MDEA), conventionally used.
- charge rate n gas cide n mine
- the invention makes it possible to reduce the amount of CO 2 captured for a higher H 2 S loading rate relative to the MDEA. This gain in capacity and selectivity results in savings in the capital costs and operating costs of the deacidification unit as well as the downstream Claus unit which processes a gas richer in H 2 S.
- the absorbent solutions according to the invention can be used to deacidify the following gaseous effluents: natural gas, synthesis gases, combustion fumes, gases. Refinery gas, tail gas Claus process, biomass fermentation gas, cement gas, incinerator fumes. These gaseous effluents contain one or more of the following acidic compounds: C0 2 , H 2 S, mercaptans, COS, CS 2 , SO 2 .
- the combustion fumes are produced in particular by the combustion of hydrocarbons, biogas, coal in a boiler or for a combustion gas turbine, for example for the purpose of producing electricity.
- These fumes have a temperature of between 20 and 60 ° C., a pressure of between 1 and 5 bar and can comprise between 50 and 80% of nitrogen, between 5 and 40% of carbon dioxide, between 1 and 20% of oxygen, and some impurities such as SOx and NOx, if they have not been removed downstream of the deacidification process.
- the synthesis gas contains carbon monoxide CO, hydrogen H 2 (generally in a ratio H 2 / CO equal to 2), water vapor (generally at saturation at the temperature where the washing is carried out) and carbon dioxide C0 2 (of the order of ten percent).
- the pressure is generally between 20 and 30 bar, but can reach up to 70 bar. It contains, in addition, sulfur impurities (H 2 S, COS, etc.), nitrogen (NH 3 , HCN) and halogenated impurities.
- Natural gas consists mainly of gaseous hydrocarbons, but may contain several of the following acidic compounds: C0 2 , rH 2 S, mercaptans, COS, CS 2 .
- the content of these acidic compounds is very variable and can be up to 40% for C0 2 and H 2 S.
- the temperature of the natural gas can be between 20 ° C and 100 ° C.
- the pressure of the natural gas to be treated may be between 10 and 120 bar.
- W is a releasable group in the sense of organic chemistry. It is generally chosen from a halogen atom, especially a chlorine, bromine or iodine atom. W may also be a tosylate or mesylate radical well known as releasable groups. In some cases the nitro groups can satisfy the reaction.
- one of the precursors of these reactions still carries a tertiary amine function.
- these functions may be present in the form of hydrohalides, for example hydrochlorides.
- B for example the following routes which can lead to diamines according to the invention. It is the addition of a primary amine on the unsaturation of an acrylamide derivative or on the unsaturation of acrylonitrile followed by the hydrogenation of the carbonyl function which converts amide function to amine or the hydrogenation of the nitrile function which converts it into a primary amine function
- diamines according to the invention can be obtained by partially alkylating a primary or secondary diamine by means known to carry out this type of reaction, such as the reaction of a primary or secondary amine with an aldehyde or a ketone in the presence of hydrogen and with the aid of a catalyst.
- the following diagram illustrates this synthetic route represented by way of example from a diamine having two primary amine functions, formaldehyde and hydrogen.
- 8 products of different degrees of alkylation can be obtained. 2 of them correspond to a diamine according to the invention.
- the following diagram illustrates this synthesis route represented by way of example from a diamine of which one of the functions is tertiary and the other primary, formaldehyde and hydrogen.
- 2 products of different degrees of alkylation can be obtained.
- One of them corresponds to a diamine according to the invention.
- the molecules of the list a) having a low or moderate bulk of the -NH- function are distinguished from the list b) of molecules having a severe encumbrance of the -NH- function.
- the molecules of list b) are particularly suitable for selective removal of H 2 S in a gas containing H 2 S and CO 2 a) Molecules with a small or moderate bulk H
- the diamines according to the invention may be in variable concentration, for example between 21% and 80% by weight, preferably between 25% and 60% by weight, very preferably between 30% and 50% by weight, in the aqueous solution.
- the absorbent solution may contain from 10% to 90% by weight of water, preferably from 50% to 70% water.
- the compounds of general formula (I) may be formulated with another amine, containing at least one primary or secondary amine function (activator), up to a concentration of 20% by weight, of preferably less than 15% by weight, preferably less than 10% by weight.
- This type of formulation is particularly advantageous in the case of capture of C0 2 in industrial fumes, or the treatment of natural gas containing CO 2 and / or COS above the desired specification. Indeed, for this type of applications, it is sought to increase the capture kinetics of C0 2 and / or COS to reduce the size of equipment.
- the absorbent solution may comprise a physical solvent, for example methanol or sulfolane.
- the compounds of general formula (I) may be formulated with another amine, having a slow CO 2 capture kinetics, such as for example a tertiary amine. In this embodiment, it is the compound of general formula (I) which acts as an activator.
- an absorbent solution for deacidifying a gaseous effluent is carried out schematically by performing an absorption step followed by a regeneration step, for example as represented FIG. 1.
- the absorption step consists of contacting the gaseous effluent containing the acidic compounds to be removed with the absorbing solution in an absorption column C1.
- the gaseous effluent to be treated 1 and the absorbing solution 4 feed the Cl column.
- the organic compounds provided with an amine function of the absorbent solution 4 react with the acidic compounds contained in the effluent 1 so as to obtain a gaseous effluent depleted in acidic compounds 2 which leaves at the top of column C1 and a solution Absorbent enriched in acidic compounds 3 which leaves at the bottom of the column Cl.
- the acid-enriched absorbent solution 3 is sent to an exchanger E1, where it is heated by the stream 6 coming from the regeneration column C2.
- the absorbent solution 5 charged and heated at the outlet of the exchanger E1 feeds the distillation column (or regeneration column) C2 in which the regeneration of the absorbent solution loaded with acidic compounds takes place.
- the absorbent solution 3 or 5 loaded with acidic compounds can be relaxed.
- the regeneration step may therefore consist of heating, optionally to relax, or distilling the acid-enriched absorbent solution in order to release the acidic compounds which come out at the top of column C2 in gaseous form 7.
- the regenerated absorbent solution that is to say, depleted in acidic compounds 6, leaves at the bottom of the column C2, then passes into the exchanger E1, in which it gives up heat to the flow 3 as previously described.
- the regenerated and cooled absorbent solution 4 is then recycled to the absorption column Cl.
- the absorption step of the acidic compounds can be carried out at a pressure of between 1 bar and 120 bar, preferably between 20 bar and 100 bar.
- the treatment of a natural gas preferably between 1 bar and 3 bar for the treatment of industrial fumes, and at a temperature between 20 ° C and 100 ° C, preferably between 30 ° C and 90 ° C, or between 30 and 60 ° C.
- the regeneration step of the process according to the invention can be carried out by thermal regeneration, optionally supplemented by one or more expansion steps.
- the regeneration can be carried out at a pressure of between 1 bar and 5 bar, or even up to 10 bar and at a temperature of between 100 ° C. and 180 ° C., preferably between 130 ° C. and 170 ° C.
- the regeneration temperature is between 155 ° C. and 180 ° C. in the case where it is desired to reinject the acid gases.
- the regeneration temperature is between 115 ° C. and 130 ° C. in the cases where the acid gas is sent to the atmosphere or in a downstream treatment process, such as a Claus process or a tail gas treatment process.
- Absorbent solutions used in these examples are aqueous solutions containing 30% by weight of diamine according to the invention.
- the performances are compared in particular with that of an aqueous solution of MonoEthanolAmine at 30% by weight, which constitutes the reference absorbent solution for post-combustion fume capture application and that of 40% wt.% aqueous solution of MethylDiethanolAmin, which constitutes the reference absorbent solution for a natural gas treatment application.
- This molecule can also be prepared by condensation of one mole of 3-methoxypropylamine with 1.5 moles of dimethylaminoacetone at a temperature slightly above 100 ° C., in order to eliminate condensation water continuously by means of a Dean & Separator. Strark. Then, after evaporation of the excess dimethylaminoacetone and drying of the medium, the hydrogenation of the imine obtained with a stoichiometric amount of sodium tetrahydroborate is carried out at room temperature. This operation leads to the desired molecule.
- EXAMPLE 2 Capacity for Capturing Amines of General Formula (I) in Which the Two Nitrogen Atoms Are Separated by Two or Three Carbon atoms
- the partial pressures of C0 2 in the effluent to be treated are typically 0.1 bar with a temperature of 40 ° C., and it is desired to cut down 90% of the acid gas.
- the partial pressures of CO 2 in the gas to be treated are for example 0.3 bar and 1 bar with a temperature of 40 ° C. It is desired here to achieve a specification of 50 ppm, which in first approximation corresponds to a completely regenerated solvent (at 50 ppm ⁇ 0).
- [A] is the concentration of amine, expressed in% by weight
- M is the molar mass of the amine in g / mol.
- This example shows the higher loading rates that can be obtained thanks to an absorbent solution according to the invention, comprising 30% by weight of molecules of general formula (I) both at low and at high partial pressures of acid gases. .
- this example illustrates the greatest cyclical capacity in moles of C0 2 per kilogram of solvent obtained thanks to an absorbent solution according to the invention, comprising 30% by weight of molecules of general formula (I) to achieve a felling rate of 90% at the outlet of the absorber.
- the energy associated with the regeneration of the solvent is critical, it can be observed that the amines corresponding to the general formula (I) make it possible to obtain a much better compromise than the MEA, in terms of cyclic capacity and enthalpy of reaction.
- the absorption is carried out in a liquid volume of 50 cm 3 by bubbling a gaseous stream consisting of a nitrogen mixture: carbon dioxide: hydrogen sulphide of 89: 10: 1 in volume proportions, of a flow rate of 30NL / h for 90 minutes.
- This selectivity S is defined as follows: . (Concentration of the CO gas mixture). , ⁇ ...
- This example illustrates the gains in charge ratio and selectivity that can be achieved with an absorbent solution according to the invention, comprising 40% by weight of molecules of general formula (I) with a severe bulk of the secondary amine function.
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP10805246A EP2512630A1 (fr) | 2009-12-16 | 2010-11-25 | Procede d'elimination de composes acides d'un effluent gazeux avec une solution absorbante a base de diamines |
CA2783697A CA2783697A1 (fr) | 2009-12-16 | 2010-11-25 | Procede d'elimination de composes acides d'un effluent gazeux avec une solution absorbante a base de diamines |
AU2010338156A AU2010338156A1 (en) | 2009-12-16 | 2010-11-25 | Method for removing acid compounds from a gaseous effluent using a diamine-based absorbent solution |
US13/515,334 US20130011314A1 (en) | 2009-12-16 | 2010-11-25 | Method of removing acid compounds from a gaseous effluent with an absorbent solution based on i, ii/iii diamines |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0906098A FR2953735B1 (fr) | 2009-12-16 | 2009-12-16 | Procede d'elimination de composes acides d'un effluent gazeux avec une solution absorbante a base de diamines i,ii/iii. |
FR0906098 | 2009-12-16 |
Publications (1)
Publication Number | Publication Date |
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WO2011080405A1 true WO2011080405A1 (fr) | 2011-07-07 |
Family
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Family Applications (1)
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PCT/FR2010/000785 WO2011080405A1 (fr) | 2009-12-16 | 2010-11-25 | Procede d'elimination de composes acides d'un effluent gazeux avec une solution absorbante a base de diamines |
Country Status (6)
Country | Link |
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US (1) | US20130011314A1 (fr) |
EP (1) | EP2512630A1 (fr) |
AU (1) | AU2010338156A1 (fr) |
CA (1) | CA2783697A1 (fr) |
FR (1) | FR2953735B1 (fr) |
WO (1) | WO2011080405A1 (fr) |
Cited By (2)
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DE102012200566A1 (de) | 2012-01-16 | 2013-07-18 | Evonik Degussa Gmbh | Verfahren zur Absorption von CO2 aus einer Gasmischung |
DE102012222157A1 (de) | 2012-12-04 | 2014-06-05 | Evonik Industries Ag | Verfahren zur Absorption von CO2 aus einer Gasmischung |
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FR2981860B1 (fr) * | 2011-10-28 | 2013-11-08 | IFP Energies Nouvelles | Solution absorbante a base de monoalcanolamines tertiaires appartenant a la famille des 3-alcoxypropylamines et procede d'elimination de composes acides contenus dans un effluent gazeux |
AU2012339061B2 (en) | 2011-11-14 | 2016-10-13 | Evonik Degussa Gmbh | Method and device for the separation of acidic gases from a gas mixture |
DE102012200907A1 (de) | 2012-01-23 | 2013-07-25 | Evonik Industries Ag | Verfahren und Absorptionsmedium zur Absorption von CO2 aus einer Gasmischung |
DE102012207509A1 (de) | 2012-05-07 | 2013-11-07 | Evonik Degussa Gmbh | Verfahren zur Absorption von CO2 aus einer Gasmischung |
FR2992229B1 (fr) * | 2012-06-26 | 2015-10-30 | IFP Energies Nouvelles | Solution absorbante a base de diamines tertiaires appartenant a la famille des aminoethylmorpholines encombrees et procede d'elimination de composes acides d'un effluent gazeux |
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US20170312681A1 (en) | 2014-10-27 | 2017-11-02 | Carbonoro B.V. | Process and apparatus for separating entrained amines from a gas stream |
EP3212308A1 (fr) | 2014-10-27 | 2017-09-06 | CarbonOro B.V. | Procédé et appareil pour séparer des amines entraînées d'un flux de gaz |
DE102015212749A1 (de) | 2015-07-08 | 2017-01-12 | Evonik Degussa Gmbh | Verfahren zur Entfeuchtung von feuchten Gasgemischen |
FR3045401B1 (fr) * | 2015-12-17 | 2018-02-02 | IFP Energies Nouvelles | Solution absorbante a base de derives hydroxyles de la 1,6-hexanediamine et procede d'elimination de composes acides d'un effluent gazeux |
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DE102016210478A1 (de) | 2016-06-14 | 2017-12-14 | Evonik Degussa Gmbh | Verfahren zur Entfeuchtung von feuchten Gasgemischen |
DE102016210484A1 (de) | 2016-06-14 | 2017-12-14 | Evonik Degussa Gmbh | Verfahren zur Entfeuchtung von feuchten Gasgemischen |
EP3257843A1 (fr) | 2016-06-14 | 2017-12-20 | Evonik Degussa GmbH | Procédé pour préparer un sel tres pur d'imidazolium |
DE102016210481B3 (de) | 2016-06-14 | 2017-06-08 | Evonik Degussa Gmbh | Verfahren zum Reinigen einer ionischen Flüssigkeit |
DE102016210483A1 (de) | 2016-06-14 | 2017-12-14 | Evonik Degussa Gmbh | Verfahren und Absorptionsmittel zur Entfeuchtung von feuchten Gasgemischen |
EP3257568B1 (fr) | 2016-06-14 | 2019-09-18 | Evonik Degussa GmbH | Procede de deshumidification de melanges gazeux humides par des liquides ioniques |
JP6841676B2 (ja) | 2017-01-31 | 2021-03-10 | 三菱重工エンジニアリング株式会社 | 複合アミン吸収液、co2又はh2s又はその双方の除去装置及び方法 |
CN111093803B (zh) | 2017-09-04 | 2022-06-24 | 巴斯夫欧洲公司 | 用于选择性去除硫化氢的吸收剂和方法 |
US11266947B2 (en) * | 2019-03-25 | 2022-03-08 | Battelle Memorial Institute | Diamine solvent system for CO2 capture |
BR112021023742A2 (pt) | 2019-09-10 | 2022-04-12 | Basf Se | Processo para a remoção de gases ácidos de uma corrente de fluido, uso de um absorvente e processo para a fabricação de um composto de fórmula (i) |
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-
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- 2010-11-25 AU AU2010338156A patent/AU2010338156A1/en not_active Abandoned
- 2010-11-25 CA CA2783697A patent/CA2783697A1/fr not_active Abandoned
- 2010-11-25 WO PCT/FR2010/000785 patent/WO2011080405A1/fr active Application Filing
- 2010-11-25 EP EP10805246A patent/EP2512630A1/fr not_active Withdrawn
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Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102012200566A1 (de) | 2012-01-16 | 2013-07-18 | Evonik Degussa Gmbh | Verfahren zur Absorption von CO2 aus einer Gasmischung |
WO2013107551A1 (fr) | 2012-01-16 | 2013-07-25 | Evonik Degussa Gmbh | Procédé d'absorption de co2 d'un mélange gazeux contenant des amines |
DE102012222157A1 (de) | 2012-12-04 | 2014-06-05 | Evonik Industries Ag | Verfahren zur Absorption von CO2 aus einer Gasmischung |
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Also Published As
Publication number | Publication date |
---|---|
AU2010338156A1 (en) | 2012-07-12 |
EP2512630A1 (fr) | 2012-10-24 |
FR2953735B1 (fr) | 2013-03-29 |
FR2953735A1 (fr) | 2011-06-17 |
CA2783697A1 (fr) | 2011-07-07 |
US20130011314A1 (en) | 2013-01-10 |
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