WO2017055067A1 - Aminverbindungen zur selektiven entfernung von schwefelwasserstoff - Google Patents
Aminverbindungen zur selektiven entfernung von schwefelwasserstoff Download PDFInfo
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- WO2017055067A1 WO2017055067A1 PCT/EP2016/071442 EP2016071442W WO2017055067A1 WO 2017055067 A1 WO2017055067 A1 WO 2017055067A1 EP 2016071442 W EP2016071442 W EP 2016071442W WO 2017055067 A1 WO2017055067 A1 WO 2017055067A1
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- absorbent
- acid
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- 0 CC(C)(*N(*)C(C)(C)*N(*)*)N(C)* Chemical compound CC(C)(*N(*)C(C)(C)*N(*)*)N(C)* 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
- B01D53/1493—Selection of liquid materials for use as absorbents
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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
- B01D53/1425—Regeneration of liquid absorbents
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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
- B01D53/1468—Removing hydrogen sulfide
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C217/00—Compounds containing amino and etherified hydroxy groups bound to the same carbon skeleton
- C07C217/02—Compounds containing amino and etherified hydroxy groups bound to the same carbon skeleton having etherified hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton
- C07C217/04—Compounds containing amino and etherified hydroxy groups bound to the same carbon skeleton having etherified hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton the carbon skeleton being acyclic and saturated
- C07C217/06—Compounds containing amino and etherified hydroxy groups bound to the same carbon skeleton having etherified hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton the carbon skeleton being acyclic and saturated having only one etherified hydroxy group and one amino group bound to the carbon skeleton, which is not further substituted
- C07C217/08—Compounds containing amino and etherified hydroxy groups bound to the same carbon skeleton having etherified hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton the carbon skeleton being acyclic and saturated having only one etherified hydroxy group and one amino group bound to the carbon skeleton, which is not further substituted the oxygen atom of the etherified hydroxy group being further bound to an acyclic carbon atom
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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
- B01D2252/202—Alcohols or their derivatives
- B01D2252/2023—Glycols, diols or their derivatives
- B01D2252/2026—Polyethylene glycol, ethers or esters thereof, e.g. Selexol
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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
- B01D2252/20478—Alkanolamines
- B01D2252/20489—Alkanolamines with two or more hydroxyl groups
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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
- B01D2252/205—Other organic compounds not covered by B01D2252/00 - B01D2252/20494
- B01D2252/2056—Sulfur compounds, e.g. Sulfolane, thiols
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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
- B01D2252/40—Absorbents explicitly excluding the presence of water
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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
- B01D2252/50—Combinations of absorbents
- B01D2252/502—Combinations of absorbents having two or more functionalities in the same molecule other than alkanolamine
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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
- B01D2252/50—Combinations of absorbents
- B01D2252/504—Mixtures of two or more absorbents
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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
- B01D2252/60—Additives
Definitions
- the present invention relates to amine compounds useful in the removal of acid gases from a fluid stream, particularly for the selective removal of hydrogen sulfide from a fluid stream.
- the present invention also relates to an absorbent and its use and to a process for removing acid gases from a fluid stream, in particular for the selective removal of hydrogen sulfide from a fluid stream.
- CO2 has to be removed from natural gas, because a high concentration of CO2 when used as a pipeline or sales gas reduces the calorific value of the gas.
- CO2 can lead to corrosion of pipes and fittings.
- too low a concentration of CO2 is also undesirable because it may cause the calorific value of the gas to be too high.
- the CO2 concentrations for pipeline or sales gas are between 1, 5 and 3.5% by volume.
- washes are used with aqueous solutions of inorganic or organic bases.
- ions form with the bases.
- the absorbent may be regenerated by depressurization to a lower pressure and / or stripping whereby the ionic species react back to sour gases and / or are stripped out by steam. After the regeneration process, the absorbent can be reused.
- a process in which all acid gases, especially CO2 and H2S, are removed as far as possible is called "total absorption". In certain cases, however, it may be desirable to preferentially absorb H2S from CO2, e.g. B. to obtain a calorific value-optimized CO I-S ratio for a downstream Claus plant.
- An unfavorable CO I-S ratio can affect the performance and efficiency of the Claus plant by formation of COS / CS 2 and coking of the Claus catalyst or by a too low calorific value.
- Highly hindered secondary amines such as 2- (2-tert-butylaminoethoxy) ethanol, and tertiary amines, such as methyldiethanolamine (MDEA)
- MDEA methyldiethanolamine
- These amines do not react directly with CO2; instead, CO2 reacts slowly with the amine and with water to form bicarbonate - in contrast, H2S reacts instantly in aqueous amine solutions.
- Such amines are therefore particularly suitable for the selective removal of H2S from gas mixtures containing CC "2 and H2S.
- the selective removal of hydrogen sulfide is widely used in fluid streams with low sour gas partial pressures, such.
- AGE Acid Gas Enrichment
- Natural gas treatment for pipeline gas may also require selective removal of H2S from CO2.
- natural gas treatment seeks to simultaneously remove H2S and CO2 while meeting F S limits and eliminating the need for complete removal of CO2.
- the specification typical for pipeline gas requires sour gas removal to about 1.5 to 3.5 vol% CO2 and less than 4 vppm H2S. In these cases maximum F S selectivity is not desired.
- Im et al. describe in Energy Environ. See, 201 1, 4, 4284-4289, the mechanism of CC "2 absorption by sterically hindered alkanolamines. It has been found that CO2 is exclusively associated with the hydroxyl groups of the alkanolamines to give terionic carbonates reacts.
- Xu et al. describe in Ind. Eng. Chem. Res. 2002, 41, 2953-2956, that in the removal of H2S from a fluid stream by means of a methyldiethanolamine solution, a reduced water content requires a higher selectivity.
- US 2015/0027055 A1 describes a process for the selective removal of H 2 S from a CO 2 -containing gas mixture by means of an absorption medium which comprises sterically hindered, terminally etherified alkanolamines. It was found that the terminal etherification of the alkanolamines or the exclusion of water allows a higher F S selectivity.
- the invention is based on the object of specifying further compounds which are suitable for removing acid gases from fluid streams.
- the compounds are said to have thermal stability and low volatility.
- Absorbents based on the compounds should have high loadability, high cyclic capacity and good regenerability.
- the solutions of the compounds in non-aqueous solvents should have low viscosities. It is also intended to provide a method of removing sour gases from fluid streams.
- the object is achieved by a compound of general formula (I)
- Ri and R2 independently of one another are C 1 -C 4 -alkyl;
- R 3 , R 4 , R 5 and R 6 are independently selected from hydrogen and C 1 -C 4 -alkyl;
- R 7 and Rs independently of one another are C 1 -C 4 -alkyl;
- x and y are integers from 2 to 4 and z is an integer from 1 to 3.
- R 4 , R 5 and R 6 are hydrogen.
- R 7 and R 4 independently of one another are methyl or ethyl.
- R1 and R2 are methyl and R3 is hydrogen; or R1, R2 and R3 are methyl; or R1 and R2 are methyl and R3 is ethyl.
- the compound of the general formula (I) is selected from 2- (2-tert-butylaminoethoxy) ethyl-N, N-dimethylamine, 2- (2-tert-butylaminoethoxy) ethyl-N, N-diethylamine, 2- (2 tert-butylaminoethoxy) ethyl-N, N-dipropylamine, 2- (2-isopropylaminoethoxy) ethyl-N, N-dimethylamine, 2- (2-isopropylaminoethoxy) ethyl-N, N -diethylamine, 2- (2- isopropylaminoethoxy) ethyl-N, N-dipropylamine, 2- (2- (2- (2- (2- (2-
- the compound of the general formula (I) is particularly preferably 2- (2-tert-butylaminoethoxy) ethyl-N, N-dimethylamine (TBAEEDA).
- the compounds of the general formula (I) include a secondary amino group and a tertiary amino group.
- the nitrogen atom of the secondary amino group has at least one secondary or tertiary carbon atom in the immediate vicinity.
- the secondary amino group is thus sterically hindered.
- the compounds of general formula (I) also include compounds which are referred to in the art as highly hindered amines and have a steric parameter (taffeta constant) of greater than 1.75.
- the compounds of the general formula (I) comprise, in addition to a tertiary amino group and a sterically hindered secondary amino group, no further amino groups. These amines show kinetic selectivity for H2S over CO2. These amines do not react directly with CO2; rather, CO2 is converted into ionic products in a slow reaction with the amine and with a proton donor, such as water. Hydroxyl groups, which are introduced into the absorbent via compounds of the general formula (I) and / or the solvent, represent proton donors. It is assumed that a low supply of hydroxyl groups in the absorbent impedes CO 2 absorption. A low hydroxyl group density therefore leads to an increase in H2S selectivity.
- the hydroxyl group density can be used to set the desired selectivity of the adsorbent for H2S over CO2. Water has a particularly high hydroxyl group density. The use of non-aqueous solvents therefore causes high H2S selectivities.
- the compounds of general formula (I) are further distinguished by a low viscosity. Low viscosity is advantageous for handleability.
- the compounds of general formula (I) at 25 ° C have a dynamic viscosity in the range of 0.5 to 40 mPa-s, more preferably in the range of 0.6 to 30 mPa-s and most preferably in the range of 0 , 7 to 20 mPa-s. Suitable methods for determining the viscosity are mentioned in the exemplary embodiments.
- the compounds of the general formula (I) also have the advantage that they are completely miscible with water.
- the compounds of the general formula (I) can be prepared in various ways.
- a polyalkylene glycol is reacted with a secondary amine R 7 RsNH according to the following scheme.
- the reaction is suitably carried out in the presence of hydrogen in the presence of a hydrogenation / dehydrogenation catalyst, e.g. Example, a copper-containing hydrogenation / dehydrogenation catalyst, at 160 to 220 ° C:
- the resulting compound can be reacted with a primary amine R 1 R 2 R 3 C-NH 2 to give a compound of the general formula (I) according to the following scheme.
- the reaction is suitably carried out in the presence of hydrogen in the presence of a hydrogenation / dehydrogenation catalyst, e.g. Example, a copper-containing hydrogenation / dehydrogenation catalyst, at 160 to 220 ° C.
- an absorbent for removing acid gases from a fluid stream in particular for selectively removing hydrogen sulfide from a fluid stream containing carbon dioxide and hydrogen sulfide, comprising a solution of a compound of general formula (I).
- the absorbent preferably contains from 10 to 70% by weight, more preferably from 15 to 65% by weight, and most preferably from 20 to 60% by weight of a compound of the general formula (I), based on the weight of the absorbent.
- the absorbent comprises a tertiary amine other than the compounds of general formula (I) or strongly hindered primary and / or highly hindered secondary amine.
- a strong steric hindrance is meant a tertiary carbon atom in the immediate vicinity of a primary or secondary nitrogen atom.
- the absorbent comprises the tertiary amine or highly hindered amine other than the compounds of general formula (I), generally in an amount of from 5 to 50% by weight, preferably from 10 to 40% by weight, and more preferably 20% to 40 wt .-%, based on the weight of the absorbent.
- Suitable tertiary amines other than the compounds of general formula (I) include, in particular: 1 .
- DIEA 2-Diisopropylaminoethanol
- MDIPA 2-Diisopropylaminoethanol
- Tertiary aminoethers like
- Suitable highly sterically hindered amines other than the compounds of the general formula (I) include in particular:
- 2-amino-2-methylpropanol (2-AMP); 2-amino-2-ethylpropanol; and 2-amino-2-propylpropanol;
- the absorbent does not contain a sterically unhindered primary amine or sterically unhindered secondary amine.
- a sterically unhindered primary amine is understood to mean compounds which have primary amino groups to which only hydrogen atoms or primary or secondary carbon atoms are bonded.
- a sterically unhindered secondary amine is meant compounds having secondary amino groups to which only hydrogen or primary carbon atoms are attached.
- Sterically unhindered primary amines or sterically unhindered secondary amines act as potent activators of CO 2 absorption. By their presence in the absorbent, the h S selectivity of the absorbent can be lost.
- the viscosity of the absorbent should not exceed certain limits. As the viscosity of the absorbent increases, the thickness of the liquid boundary layer increases due to the lower diffusion rate of the reactants in the more viscous liquid. This causes a reduced mass transfer of compounds from the fluid stream into the absorbent. This can be counteracted by, for example, increasing the number of trays or increasing the packing height, which, however, unfavorably leads to an increase in the absorption apparatus. In addition, higher viscosities of the absorbent can cause pressure losses in the heat exchangers of the apparatus and a poorer heat transfer. Surprisingly, the absorbents according to the invention also exhibit low viscosities as nonaqueous solutions, even at high concentrations of compounds of the general formula (I).
- the viscosity of the absorbent is relatively low.
- the dynamic viscosity of the (unloaded) absorbent at 25 ° C. is preferably in the range from 0.5 to 40 mPa.s, more preferably in the range from 0.6 to 30 mPa.s and most preferably in the range from 0.7 to 20 mPa-s. Suitable methods for determining the viscosity are given in the exemplary embodiments.
- the absorbent is an aqueous solution.
- the aqueous absorbent comprises an acid.
- the absorbent may contain, in addition to water and optionally an acid, one or more water-miscible organic solvents.
- the acid preferably has a pKa of less than 6, in particular less than 5. For acids with several dissociation stages and consequently several pKs values, this requirement is fulfilled if one of the pKs values is in the stated range.
- the acid is suitably selected from protonic acids (Brönstedt acids).
- the acid is preferably added in an amount such that the pH of the aqueous solution measured at 120 ° C is 7.9 to less than 8.8, preferably 8.0 to less than 8.8, more preferably 8.0 to less than 8.5, most preferably from 8.0 to less than 8.2.
- the amount of acid in one embodiment is 0.1 to 5.0 wt%, preferably 0.2 to 4.5 wt%, more preferably 0.5 to 4.0 wt%, and most preferably 1 , 0 to 2.5 wt .-%, based on the weight of the absorbent.
- the acid is selected from organic and inorganic acids.
- Suitable organic acids include, for example, phosphonic acids, sulfonic acids,
- the acid is a polybasic acid.
- Suitable acids are, for example
- Mineral acids such as hydrochloric acid, sulfuric acid, amidosulfuric acid, phosphoric acid, partial esters of phosphoric acid, eg. B. mono- and dialkyl and -arylphosphate as Tridecyl phosphate, dibutyl phosphate, diphenyl phosphate and bis (2-ethylhexyl) phosphate; boric acid;
- Carboxylic acids for example, saturated aliphatic monocarboxylic acids such as
- Glutaric acid adipic acid, pimelic acid, suberic acid, azelaic acid, sebacic acid, dodecanedioic acid; cycloaliphatic mono- and polycarboxylic acids such as
- aromatic mono- and polycarboxylic acids such as benzoic acid, salicylic acid,
- Gallic acid the positionally isomeric tolylic acids, methoxybenzoic acids,
- isophthalic acid technical carboxylic acid mixtures such as Versatic acids;
- Sulfonic acids such as methylsulfonic acid, butylsulfonic acid, 3-hydroxypropylsulfonic acid, sulfoacetic acid, benzenesulfonic acid, p-toluenesulfonic acid, p-xylenesulfonic acid, 4-dodecylbenzenesulfonic acid, 1-naphthalenesulfonic acid, dinonylnaphthalenesulfonic acid and dinonylnaphthalenedisulfonic acid, trifluoromethyl- or nonafluoro-n-butylsulfonic acid, camphorsulfonic acid, 2- (4- (2-hydroxyethyl) -1-piperazinyl) ethanesulfonic acid (HEPES); organic phosphonic acids, for example phosphonic acids of the formula (II) wherein Rg is Ci_i8-alkyl which is optionally substituted by up to four substituents independently selected from carboxy,
- alkylphosphonic acids such as methylphosphonic acid
- Hydroxyalkylphosphonic acids such as hydroxymethylphosphonic acid, 1 - Hydroxyethylphosphonic acid, 2-hydroxyethylphosphonic acid;
- Arylphosphonic acids such as phenylphosphonic acid, toluylphosphonic acid, xylylphosphonic acid,
- Aminoalkylphosphonic acids such as aminomethylphosphonic acid, 1-aminoethylphosphonic acid, 1-dimethylaminoethylphosphonic acid, 2-aminoethylphosphonic acid, 2- (N-methylamino) ethylphosphonic acid, 3-aminopropylphosphonic acid, 2-aminopropylphosphonic acid, 1-aminopropylphosphonic acid, 1-aminopropyl-2-chloropropylphosphonic acid, 2 -Aminobutylphosphonic acid, 3-aminobutylphosphonic acid, 1-aminobutylphosphonic acid, 4-aminobutylphosphonic acid, 2-aminopentylphosphonic acid, 5-aminopentylphosphonic acid, 2-aminohexylphosphonic acid, 5-aminohexylphosphonic acid, 2-aminooctylphosphonic acid, 1-aminooctylphosphonic acid, 1-aminobutylphosphonic acid
- R10 is H or Ci-6-alkyl
- Q is H, OH or NY2
- Y is H or CH2PO3H2, such as 1-hydroxyethane-1, 1-diphosphonic acid
- Z is C2-6-alkylene, cycloalkanediyl, phenylene, or C2-6-alkylene, by
- Y is CH 2 PO 3 H 2 and m is 0 to 4, such as ethylenediaminetetra (methylenephosphonic acid), diethylenetriaminepenta (methylenephosphonic acid) and bis (hexamethylene) triaminepenta (methylenephosphonic acid);
- Aminocarboxylic acids having tertiary amino groups or amino groups which at least one secondary or tertiary carbon atom in the immediate
- ⁇ -amino acids having tertiary amino groups or amino groups having at least one secondary or tertiary carbon atom in close proximity to the amino group such as ⁇ , ⁇ -dimethylglycine (dimethylaminoacetic acid), N, N-diethylglycine, alanine (2-aminopropionic ), N-methylalanine (2- (methylamino) propionic acid), ⁇ , ⁇ -dimethylalanine, N-ethylalanine, 2-methylalanine (2-aminoisobutyric acid), leucine (2-amino-4-methyl-pentane-1 - acid), N-methylleucine, N, N-dimethyl-leucine, isoleucine (1-amino-2-methylpentanoic acid), N-methylisoleucine, N, N-dimethyl-isoleucine, valine (2-aminoisovaleric acid), ⁇ -methylva
- the inorganic acids phosphoric acid and sulfuric acid are preferable.
- carboxylic acids are formic acid, acetic acid, benzoic acid,
- Succinic acid and adipic acid are preferred.
- sulfonic acids methanesulfonic acid, p-toluenesulfonic acid and 2- (4- (2-hydroxyethyl) -1-piperazinyl) ethanesulfonic acid (HEPES) are preferable.
- phosphonic acids are 2-hydroxyphosphonoacetic acid, 2-phosphonobutane-1, 2,4-tricarboxylic acid, 1-hydroxyethane-1,1-diphosphonic acid, ethylenediamine-tetra- (methylenephosphonic acid), diethylenetriamine-penta (methylenephosphonic acid),
- HDTMP Bis (hexamethylene) triamine penta (methylenephosphonic acid)
- nitrilotris methylenephosphonic acid
- aminocarboxylic acids having tertiary amino groups or amino groups which have at least one secondary or tertiary carbon atom in the immediate vicinity of the amino group ⁇ , ⁇ -dimethylglycine and N-methylalanine are preferred.
- the acid is an inorganic acid.
- the absorbent contains at least one organic solvent. It may be desirable to limit the water content of the absorbent, e.g. B. to a maximum of 20 wt .-% or at most 10 wt .-% or at most 5 wt .-%.
- the non-aqueous solvent is preferably selected from C 4 -C 10 -alcohols, such as n-butanol, n-pentanol and n-hexanol; Ketones, such as cyclohexanone;
- Esters such as ethyl acetate and butyl acetate; Lactones such as ⁇ -butyrolactone, ⁇ -valerolactone and ⁇ -caprolactone;
- Amides such as tertiary carboxylic acid amides, for example N, N-dimethylformamide; or N-formylmorpholine and N-acetylmorpholine; Lactams such as ⁇ -butyrolactam, ⁇ -valerolactam and ⁇ -caprolactam and N-methyl-2-pyrrolidone (NMP);
- Sulfones such as sulfolane
- Sulfoxides such as dimethylsulfoxide (DMSO);
- Glycols such as ethylene glycol (EG) and propylene glycol
- Polyalkylene glycols such as diethylene glycol (DEG) and triethylene glycol (TEG);
- Di- or mono (C 1-4 -alkyl ether) -glycols such as ethylene glycol dimethyl ether;
- Di- or mono (C 1-4 -alkyl ether) -polyalkylene glycols such as diethylene glycol dimethyl ether, dipropylene glycol monomethyl ether and triethylene glycol dimethyl ether; cyclic ureas such as N, N-dimethylimidazolidin-2-one and dimethylpropyl-urea (DMPU); Thioalkanols such as ethylenedithioethanol, thiodiethyleneglycol (thiodiglycol, TDG) and methylthioethanol; and mixtures thereof.
- the non-aqueous solvent is selected from sulfones, glycols and polyalkylene glycols.
- the non-aqueous solvent is selected from sulfones.
- a preferred nonaqueous solvent is sulfolane.
- the absorbent may also contain additives such as corrosion inhibitors, enzymes, antifoams, etc. In general, the amount of such additives ranges from about 0.005 to 3% by weight of the absorbent.
- the absorbent preferably has a H 2 S: CO 2 loading ratio of at least 1.1, more preferably at least 2, and most preferably at least 5.
- H2S CO2 loading ratio
- the ratio of the maximum H2S loading to the maximum CO2 load under equilibrium conditions becomes Loading the absorbent with CO2 or H2S at 40 ° C and ambient pressure (about 1 bar) understood. Suitable test methods are mentioned in the exemplary embodiments.
- the H2S: C02 loading ratio serves as an indication of the expected H S selectivity; the higher the H2S: C02 loading ratio, the higher the expected h S selectivity.
- the maximum h S loading capacity of the absorbent is at least 5 Nm 3 / t, more preferably at least 8 Nm 3 / t, and most preferably at least 12 Nm 3 / t.
- the present invention also relates to the use of the absorbent of the invention for removing acid gases from a fluid stream, in particular for the selective removal of hydrogen sulfide from a fluid stream containing carbon dioxide and hydrogen sulfide.
- the inventive method is suitable for removing acid gases from a fluid stream; in particular for the selective removal of hydrogen sulphide against CO2.
- selective removal of hydrogen sulphide herein is meant the value of the following quotient: y (H2S) feed -y (H2S) treat
- the method is considered to be selective for the removal of H2S from CO2.
- the value of the above quotient for the Process according to the invention is preferably at least 1, 1, very particularly preferably at least 2 and most preferably at least 4.
- the removal of sour gas from natural gas for use as a pipeline or sales gas total absorption of carbon dioxide is undesirable.
- the residual content of carbon dioxide in the treated fluid stream is at least 0.5% by volume, preferably at least 1.0% by volume and more preferably at least 1.5% by volume.
- the process according to the invention is suitable for the treatment of fluids of all kinds. Fluids are on the one hand gases such as natural gas, synthesis gas, coke oven gas, cracked gas, coal gasification gas, cycle gas, landfill gas and combustion gases, and on the other hand with the absorbent substantially immiscible liquids such as LPG (Liquefied Petroleum Gas) or NGL (Natural Gas Liquids).
- the process according to the invention is particularly suitable for the treatment of hydrocarbon-containing fluid streams.
- the hydrocarbons contained are z.
- aliphatic hydrocarbons such as Ci-C4 hydrocarbons such as methane, unsaturated hydrocarbons such as ethylene or propylene, or aromatic hydrocarbons such as benzene, toluene or xylene.
- the inventive method is suitable for the removal of acid gases, for example, CO2, H2S, SO3, SO2, CS2, HCN, COS and mercaptans.
- acid gases may also be present in the fluid stream, such as COS and mercaptans.
- the method is particularly suitable for the selective removal of hydrogen sulfide from a fluid stream containing carbon dioxide and hydrogen sulfide.
- the fluid stream is a hydrocarbon-containing fluid stream; in particular a natural gas stream. More preferably, the fluid stream contains more than 1.0% by volume of hydrocarbons, more preferably more than 5.0% by volume of hydrocarbons, most preferably more than 15% by volume of hydrocarbons.
- the hydrogen sulfide partial pressure in the fluid stream is usually at least 2.5 mbar.
- a hydrogen sulfide partial pressure of at least 0.1 bar, in particular at least 1 bar, and a carbon dioxide partial pressure of at least 0.2 bar, in particular at least 1 bar are present in the fluid stream.
- the stated partial pressures refer to the fluid flow upon first contact with the absorbent in the absorption step.
- the fluid stream has a total pressure of at least 1.0 bar, more preferably at least 3.0 bar, even more preferably at least 5.0 bar, and most preferably at least 20 bar.
- the fluid flow has a total pressure of at most 180 bar. The total pressure refers to the fluid flow upon initial contact with the absorbent in the absorption step.
- the fluid stream is brought into contact with the absorbent in an absorption step in an absorber, whereby carbon dioxide and hydrogen sulfide are at least partially washed out.
- the absorber is a washing device used in conventional gas scrubbing processes. Suitable washing devices are, for example, packed, packed and tray columns, membrane contactors, radial flow scrubbers, jet scrubbers, venturi scrubbers and rotary scrubbers, preferably packed, packed and tray columns, particularly preferably tray and packed columns.
- the treatment of the fluid stream with the absorbent is preferably carried out in a column in countercurrent.
- the fluid is generally fed into the lower region and the absorbent in the upper region of the column.
- tray columns sieve bell or valve trays are installed, over which the liquid flows.
- Packed columns can be filled with different moldings. Heat and mass transfer are improved by the enlargement of the surface due to the usually about 25 to 80 mm large moldings.
- Raschig ring a hollow cylinder
- Pall ring a hollow cylinder
- Hiflow ring Hiflow ring
- Intalox saddle the like.
- the packing can be ordered, but also random (as a bed) are introduced into the column.
- Possible materials are glass, ceramics, metal and plastics.
- Structured packings are a further development of the ordered packing. They have a regularly shaped structure. This makes it possible for packings to reduce pressure losses in the gas flow.
- the material used can be metal, plastic, glass and ceramics.
- the temperature of the absorbent in the absorption step is generally about 30 to 100 ° C, using a column, for example 30 to 70 ° C at the top of the column and 50 to 100 ° C at the bottom of the column.
- the process according to the invention may comprise one or more, in particular two, successive absorption steps.
- the absorption can be carried out in several successive sub-steps, wherein the raw gas containing the acidic gas constituents in each of the substeps is brought into contact with a partial stream of the absorbent.
- the absorbent with which the raw gas is brought into contact may already be partially laden with acidic gases, ie it may be, for example, an absorbent which has been recycled from a subsequent absorption step to the first absorption step, or a partially regenerated absorbent.
- the performance of the two-stage absorption reference is made to the publications EP 0 159 495, EP 0 190 434, EP 0 359 991 and WO 00100271.
- the person skilled in the art can achieve a high degree of separation of hydrogen sulfide at a defined selectivity by determining the conditions in the absorption step, in particular the absorber / fluid flow ratio, the column height of the absorber, the type of contact-promoting internals in the absorber, such as fillers, trays or packings, and / or the residual loading of the regenerated absorbent varies.
- a low absorber / fluid flow ratio leads to increased selectivity, a higher absorber / fluid flow ratio leads to a more unselective absorption. Since CO2 is absorbed at a slower rate than H2S, more CO 2 is absorbed with a longer residence time than with a shorter residence time. A higher column therefore causes a more selective absorption. Bottoms or packs with larger liquid holdup also result in less selective absorption. About the introduced during the regeneration heating energy, the residual load of the regenerated absorbent can be adjusted. A lower residual loading of the regenerated absorbent leads to improved absorption.
- the method preferably comprises a regeneration step in which the CO2 and F S-laden absorbent is regenerated.
- the regeneration step CO2 and H2S and possibly other acidic gas constituents are released from the CO2- and Fs-laden absorption medium, a regenerated absorption medium being obtained.
- the regenerated absorbent is subsequently introduced into attributed the absorption step.
- the regeneration step comprises at least one of heating, relaxing and stripping with an inert fluid.
- the regeneration step preferably comprises heating the absorbent laden with the acidic gas constituents, e.g. B. by means of a Aufkochers, natural circulation evaporator, forced circulation evaporator, or
- the absorbed acid gases are stripped off by means of the vapor obtained by heating the solution.
- an inert fluid such as nitrogen may also be used.
- the absolute pressure in the desorber is normally 0.1 to 3.5 bar, preferably 1, 0 to 2.5 bar.
- the temperature is usually from 50 ° C to 170 ° C, preferably from 80 ° C to 130 ° C, the temperature of course being dependent on the pressure.
- the regeneration step may alternatively or additionally include a pressure release. This involves at least a pressure release of the loaded absorbent from a high pressure, as it prevails in the implementation of the absorption step, to a lower pressure.
- the pressure release can be done for example by means of a throttle valve and / or an expansion turbine.
- the regeneration with a relaxation stage is described, for example, in the publications US Pat. Nos. 4,537,753 and 4,553,984.
- the release of the acidic gas constituents in the regeneration step for example, in a flash column, z. B. a vertically or horizontally installed flash tank or a countercurrent column with internals, done.
- the regeneration column may likewise be a packed, packed or tray column.
- the regeneration column has a heater at the bottom, z. B. a forced circulation evaporator with circulation pump. At the top, the regeneration column has an outlet for the liberated acid gases. Entrained absorbent vapors are condensed in a condenser and returned to the column.
- the absorbent according to the invention has a high loadability with acidic gases, which can also be easily desorbed again. As a result, the energy consumption and the solvent circulation can be significantly reduced in the process according to the invention.
- Fig. 1 is a schematic representation of an apparatus suitable for carrying out the method according to the invention.
- a suitably pretreated gas containing hydrogen sulphide and carbon dioxide is brought into contact, via the supply line Z, in an absorber A1 with regenerated absorption medium, which is supplied via the absorption medium line 1.01, in countercurrent.
- the absorbent removes hydrogen sulfide and carbon dioxide by absorption from the gas; In this case, via the exhaust pipe 1.02 a depleted in hydrogen sulfide and carbon dioxide clean gas.
- the heat exchanger 1.04 in which the CO2 and F S-laden absorbent is heated with the heat of the regenerated absorbent fed via the absorption line 1 .05, and the absorbent line 1.06 is filled with CO2 and F s. loaded absorbent the desorption column D fed and regenerated.
- one or more expansion tank can be provided (not shown in Fig. 1), in which the CO2 and F S-laden absorbent on z. B. 3 to 15 bar is relaxed.
- the absorbent is fed to the reboiler 1 .07, where it is heated.
- the resulting vapor is returned to the desorption column D, while the regenerated absorbent via the absorbent tube 1 .05, the heat exchanger 1 .04 in which the regenerated absorbent heats the CO2 and F S-laden absorbent and thereby cools the absorbent line. 1 .08, the radiator 1 .09 and the Absorptionsmitte ein 1.01 the absorber A1 is fed back.
- other types of heat exchangers can be used for energy input, such as a natural circulation evaporator, forced circulation evaporator, or forced circulation evaporator.
- a mixed phase stream of regenerated absorbent and steam is returned to the bottom of the desorption column D, where the phase separation between the vapor and the absorbent takes place.
- the regenerated absorbent to the heat exchanger 1 .04 is either withdrawn from the recycle stream from the bottom of the desorption column D to the evaporator, or passed through a separate line directly from the bottom of the desorption column D to the heat exchanger 1 .04.
- the released in the desorption column D CO2 and h S-containing gas leaves the desorption column D via the exhaust pipe 1 .10. It is fed into a capacitor with integrated phase separation 1 .1 1, where it is separated by entrained absorbent vapor.
- condensation and phase separation may also be present separately from one another.
- the condensate is passed through the absorbent line 1 .12 in the upper region of the desorption column D, and carried out a CO2 and h S-containing gas via the gas line 1 .13.
- TBAAEDA 2- (2-tert-butylaminoethoxy) ethyl-N, N-dimethylamine
- the GC analysis shows a conversion of 96% based on DMAEE used, whereby 2- (2-tert-butylaminoethoxy) ethyl-N, N-dimethylamine (TBAEEDA) was obtained in a selectivity of 73%.
- TSAEEDA 2- (2-tert-butylaminoethoxy) ethyl-N, N-dimethylamine
- the crude product was purified by distillation. After removal of excess tert-butylamine at atmospheric pressure, the target product was isolated at a bottom temperature of 95 ° C and a transition temperature of 84 ° C at 8 mbar in a purity of> 97%.
- Example 2 pKs values and temperature dependence of the pKs values
- the pKa values of the two amino groups of 2- (2-tert-butylaminoethoxy) ethyl-N, N-dimethylamine (TBAEEDA) were determined by titration with hydrochloric acid at 20 ° C.
- the pKa value of the tertiary amine MDEA is given for comparison.
- the temperature dependence of the pKs value of TBAEEDA was investigated in comparison to MDEA.
- the temperature dependence of the pKa value of aqueous amine solutions in the temperature range from 20 ° C to 120 ° C was determined.
- a pressure apparatus was used in which the pKs value can be measured up to 120 ° C.
- the concentrations of the solutions were 0.010 mol / L.
- a pronounced temperature-dependence of the pKs value means that at relatively lower temperatures, as prevail in the absorption step, the higher pKa value promotes efficient acid gas absorption, while at relatively higher temperatures, as prevail in the desorption step, the lower pKs Value supports the release of the absorbed acid gases. It is expected that a large pKs value difference of an amine between absorption and desorption temperatures will cause a lower regeneration energy.
- Example 3 Loading capacity and cyclic capacity
- the h S determination was carried out by titration with silver nitrate solution.
- the sample to be analyzed was weighed into an aqueous solution containing about 2% by weight of sodium acetate and about 3% by weight of ammonia.
- the H2S content was determined by a potentiometric inflection point titration using silver nitrate solution. At the inflection point, H2S is completely bound as Ag2S.
- the C02 content was determined as Total Inorganic Carbon (TOC-V Series Shimadzu).
- TOC-V Series Shimadzu Total Inorganic Carbon
- Example 3 The same apparatus as in Example 3 was used. Amine solutions having an amine content of 10% by weight and various solvents were used. The difference between the load at the end of the loading test and the load at the end of the stripping test results in the respective cyclic capacities.
- the H2S: C02 loading ratio was calculated as the quotient of the h S loading by the CO 2 loading and serves as an indication of the expected h S selectivity. The results are shown in Table 2.
- Example 4 From the comparison of Example 4 with Comparative Example 5 it can be seen that the compound of the invention TBAEEDA compared to TBAEE causes an increased H2S: C02 loading ratio and thus tends to increased h S selectivity in a sulfolane solution.
- TBAEEDA and DI MAP dimethylamino-1-propanol
- Example 3 The same apparatus as in Example 3 was used, except that the condensate accumulating in the glass cooler was not returned to the glass cooler, but separated and analyzed for its composition after the end of the experiment.
- the glass cylinder was thermostated at 50 ° C and filled each 100 mL of the absorbent. Over a period of 8 h, 50 Nl / h of N 2 were passed through the absorbent at ambient pressure.
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- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
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- Chemical Kinetics & Catalysis (AREA)
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Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
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JP2018516466A JP2018531242A (ja) | 2015-09-29 | 2016-09-12 | 硫化水素の選択的除去のためのアミン化合物 |
EP16766906.8A EP3356012A1 (de) | 2015-09-29 | 2016-09-12 | Aminverbindungen zur selektiven entfernung von schwefelwasserstoff |
US15/763,981 US20180272270A1 (en) | 2015-09-29 | 2016-09-12 | Amine compounds for selectively removing hydrogen sulphide |
KR1020187008433A KR20180059783A (ko) | 2015-09-29 | 2016-09-12 | 황화수소를 선택적으로 제거하기 위한 아민 화합물 |
CA3000284A CA3000284A1 (en) | 2015-09-29 | 2016-09-12 | Amine compounds for selectively removing hydrogen sulphide |
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EP15187404 | 2015-09-29 | ||
EP15187404.7 | 2015-09-29 |
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PCT/EP2016/071442 WO2017055067A1 (de) | 2015-09-29 | 2016-09-12 | Aminverbindungen zur selektiven entfernung von schwefelwasserstoff |
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US (1) | US20180272270A1 (de) |
EP (1) | EP3356012A1 (de) |
JP (1) | JP2018531242A (de) |
KR (1) | KR20180059783A (de) |
CA (1) | CA3000284A1 (de) |
WO (1) | WO2017055067A1 (de) |
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EP3579946B1 (de) | 2017-02-10 | 2021-04-07 | Basf Se | Verfahren zur entfernung von sauergasen aus einem fluidstrom sowie entsprechende verwendungen |
KR102433565B1 (ko) * | 2021-10-20 | 2022-08-18 | 주식회사 씨이텍 | 저수계형 이산화탄소 흡수제 및 이를 이용한 이산화탄소 포집방법 |
CN114699882B (zh) * | 2022-03-11 | 2024-06-14 | 华东理工大学 | 高效吸收脱除有机硫化合物的醚胺类化合物及其设计方法和应用 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0087856A1 (de) * | 1982-01-18 | 1983-09-07 | Exxon Research And Engineering Company | Verfahren zur Entfernung von H2S aus Gasmischungen unter Verwendung von Diaminoäthern |
US4405582A (en) * | 1982-01-18 | 1983-09-20 | Exxon Research And Engineering Co. | Process for selective removal of H2 S from mixtures containing H22 using diaminoether solutions |
EP0134948A2 (de) * | 1983-06-30 | 1985-03-27 | Union Carbide Corporation | Absorbentformulierung zur verstärkten Entfernung saurer Gase aus Gasmischungen und Verfahren zu ihrer Verwendung |
-
2016
- 2016-09-12 WO PCT/EP2016/071442 patent/WO2017055067A1/de active Application Filing
- 2016-09-12 US US15/763,981 patent/US20180272270A1/en not_active Abandoned
- 2016-09-12 EP EP16766906.8A patent/EP3356012A1/de not_active Withdrawn
- 2016-09-12 CA CA3000284A patent/CA3000284A1/en not_active Abandoned
- 2016-09-12 KR KR1020187008433A patent/KR20180059783A/ko unknown
- 2016-09-12 JP JP2018516466A patent/JP2018531242A/ja active Pending
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0087856A1 (de) * | 1982-01-18 | 1983-09-07 | Exxon Research And Engineering Company | Verfahren zur Entfernung von H2S aus Gasmischungen unter Verwendung von Diaminoäthern |
US4405582A (en) * | 1982-01-18 | 1983-09-20 | Exxon Research And Engineering Co. | Process for selective removal of H2 S from mixtures containing H22 using diaminoether solutions |
EP0134948A2 (de) * | 1983-06-30 | 1985-03-27 | Union Carbide Corporation | Absorbentformulierung zur verstärkten Entfernung saurer Gase aus Gasmischungen und Verfahren zu ihrer Verwendung |
Non-Patent Citations (1)
Title |
---|
DATABASE PubChem Compound [online] 22 October 2012 (2012-10-22), "PubChem Compound Summary for CID 62460368", XP002764845, Database accession no. AKOS011748617 * |
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CA3000284A1 (en) | 2017-04-06 |
EP3356012A1 (de) | 2018-08-08 |
KR20180059783A (ko) | 2018-06-05 |
US20180272270A1 (en) | 2018-09-27 |
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