CA1290553C - Removal of co -and/or h s from gases - Google Patents
Removal of co -and/or h s from gasesInfo
- Publication number
- CA1290553C CA1290553C CA000496618A CA496618A CA1290553C CA 1290553 C CA1290553 C CA 1290553C CA 000496618 A CA000496618 A CA 000496618A CA 496618 A CA496618 A CA 496618A CA 1290553 C CA1290553 C CA 1290553C
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- Prior art keywords
- stage
- absorption
- fed
- flash
- absorption liquid
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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
- B01D53/14—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
- B01D53/1406—Multiple stage absorption
-
- 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
-
- 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Abstract of the Disclosure: CO2 and/or H2S are removed from gases containing CO2 and/or H2S by means of an aqueous alkanolamine-containing absorption liquid by a process in which the gas containing CO2 and/or H2S is treated in a first absorption stage at from 40 to 100°C
with an aqueous absorption liquid containing from 20 to 70% by weight of methyldiethanolamine, the gas obtained at the top of the first absorption stage is fed to a second absorption stage in which, in order to remove further CO2 and/or H2S, it is treated at from 30 to 90°C with an aqueous absorption liquid which contains from 20 to 70% by weight of methyldiethanolamine and has a lower content of CO2 and/or H2S than the absorption liquid fed to the first absorption stage, the treated gas is taken off at the top of the second absorption stage, the aqueous absorption liquid laden with CO2 and/or H2S and obtained at the bottom of the second absorption stage is fed to the top of the first absorption stage, the aqueous absorp-tion liquid laden with CO2 and/or H2S and obtained in the lower part of the first absorption stage is regenerated by being let down in two or more flash stages, the final flash stage being operated under reduced pressure which is generated by means of a mechanical vacuum-producing apparatus and a steam-jet ejector, which are connected in series, a stream of absorption liquid obtained at the bottom of the final flash stage is recycled to the first absorption stage, a further stream of absorption liquid obtained at the bottom of the final and/or penultimate flash stage or stages is fed to a stripping zone for further regeneration, and the regenerated absorption liquid obtained at the bottom of the stripping zone is recycled to the second absorption stage.
with an aqueous absorption liquid containing from 20 to 70% by weight of methyldiethanolamine, the gas obtained at the top of the first absorption stage is fed to a second absorption stage in which, in order to remove further CO2 and/or H2S, it is treated at from 30 to 90°C with an aqueous absorption liquid which contains from 20 to 70% by weight of methyldiethanolamine and has a lower content of CO2 and/or H2S than the absorption liquid fed to the first absorption stage, the treated gas is taken off at the top of the second absorption stage, the aqueous absorption liquid laden with CO2 and/or H2S and obtained at the bottom of the second absorption stage is fed to the top of the first absorption stage, the aqueous absorp-tion liquid laden with CO2 and/or H2S and obtained in the lower part of the first absorption stage is regenerated by being let down in two or more flash stages, the final flash stage being operated under reduced pressure which is generated by means of a mechanical vacuum-producing apparatus and a steam-jet ejector, which are connected in series, a stream of absorption liquid obtained at the bottom of the final flash stage is recycled to the first absorption stage, a further stream of absorption liquid obtained at the bottom of the final and/or penultimate flash stage or stages is fed to a stripping zone for further regeneration, and the regenerated absorption liquid obtained at the bottom of the stripping zone is recycled to the second absorption stage.
Description
1~9(~SS3 - 1 - O.Z. 0050/3?490 Removal of C0? and/or H S from gases The present invention relates to a process for removing C02 and/or HzS from gases by means of an aqueous absorpt;on liquid contain;ng methyldiethanolamine.
It is disclosed, for example in German Patent 2,551,717, that C02 and/or H2S can be removed from gases by means of aqueous solutions of alkanolamines.
Although the known process is very cost-effective, it is not satisfactory in every case.
It is an object of the present invention to pro-vide a process for removing C02 and/or HzS from ~ases containing C02 and/or H2S by means of a-n aqueous alkanol-am;ne-containing absorption liquid, the said process being capable of being operated at lower energy costs and with greater cost-effectiveness than the known processes.
We have found that this and other objects and advantages are achieved, in accordance with the invention, by a process for removing C02 and/or H2S from gases containing C02 and/or H2S by means of an aqueous alkanol-amine-containing absorption liquid, wherein the gas containing C02 and/or H2S is treated in a first absorption stage at from 40 to 100C with an aqueous absorption liquid containing from 20 to 7ûX by weight of methyldiethanolamine, the gas obtained at the top of the first absorption stage is fed to a second absorption stage in which, in order to remove further C02 and/or H2S, it is treated at from 30 to 90C with an aqueous absorption liquid which contains from 20 to 7ûX by ~eight of methyldiethanolamine and has a lower content of C02 and or H2S than the absorption liquid fed to the f;rst absorption stage, the treated gas ;s taken off at the top of the second absorption stage, the aqueous absorption liquid laden with C02 and/or H2S and obtained a~ the bottom of the second absorption stage is fed to the top of the first absorption stage, the aqueous absorption liquid laden ~ith C~2 and/or HzS and obtained in the lower part of the first absorption stage is regenerated ~290SS~
- 2 - o.z. no50/37490 by being let down in two or more flash stages, the final flash stage being operated under reduced pressure which is generated by means of a mechanical vacuum-producing apparatus and a steam-jet ejector, which are connected S in series, a stream of absorption liquid obtained at the bottom of the final flash stage is recycled to the first absorption stage, a further stream of absorpt~ion liquid obtained at the bottom of the final and/or penult;mate flash stage or stages ;s fed to a str;pp;ng zone for further regeneration, and the regnerated absorption l;qu;d obtained at the bottom of the str;pp;ng zone ;s recycled to the second absorpt;on stage.
In an advantageous embod;ment of the process, the water losses result;ng from removal of water ;n the gas streams taken off at the top of the second absorpt;on stage and/or from the flash stages and/or from the str;pping zone are compensated by feed;ng ;n, at the bottom of the penultimate flash stage, an amount of steam corresponding to the water loss.
In another preferred embodiment of the process, the steam-jet ejector is connected downstream of the mechanical vacuum-producing apparatus. It may be advan-tageous for the gas taken off at the top of the f;nal flash stage to be fed ;n, together with the steam used to operate the steam-jet ejector at the bottom of the penult;mate flash stage.
The procedure according to the ;nvention gives a regenerated absorption l;qu;d hav;ng a lower content of C2 and/or H2S, so that ;t ;s possible to c;rculate smaller amounts of absorpt;on l;qu;d. This results in a corresponding saving ;n the energy requ;red for trans-port;ng the absorption liquid. Th;s procedure perm;ts the use of less compl;cated apparatus, thereby reducing the capital costs. Another advantage of the process is that the ~ater balance of the gas washer can be controlled in a simple manner. Using th;s procedure, it is possible to regulate not only the ~ater balance of the gas ~asher 1~0553 - 3 - O.Z. 0050/37490 but also its heat balance, so that any heat exchanger present in the gas washer for regulating the heat balance can be smaller or, if appropriate, can be omitted.
Examples of gases which can be treated us;ng the novel process are coal gasification gases, coke oven gases, natural gases and synthesis gases.
The gases contain in general from 1 to 90, prefer- -ably from 2 to 90, and in particular from 5 to 60, mol%
of C02~ They can also contain H2S as a further acid gas, or can contain H2S alone, for example in an amount of from a few mol ppm, for example 1 mol ppm, to 50 mol%, preferably from 10 mol ppm to 40mol%.
The solvent used for the novel process is an aqueous absorption liquid containing from 20 to 70, pre-ferably from 3û to 65, in particular from 40 to 60, Z byweight of 0ethyldiethanolamine. Advantageously, an aqueous methyldiethanolam;ne solution is used, for example an aqueous solution of technical grade methyldiethanol-am;ne. In an advantageous embodiment of the process, an aqueous methyLdiethanolamine solution is used which additionally contains from 0.05 to 1, in particular from û.1 to 0.8, in particular from 0.1 to 0.6, mole/l of primary amine or alkanolamine, such as monoethanolamine, or preferably secondary amine or alkanolamine, advantage-ously methylmonoethanolam;ne, very particularly advant-ageously piperazine.
The aqueous absorption liquid containing from 20 to 70X by weight of methyldiethanolamine may addi-t;onally contain a physical solvent. Examples of suitable phys;cal solvents are N-methylpyrrolidone, tetramethylene sulfone, methanol and oligoethylene glycol dialkyl ethers, such as oligoethylene glycol methyl isopropyl ether (SEPASOLV MPE) or oligoethylene glycol dimethyl ether (SELEXOL). The physc;al solvent is present in the absorp-tion liquid in general in an amount of from 1 to 60,preferably from 10 to 50, in particular from ZO to 40, X by weight.
* trademarks .~ .
~29(~5~3 - 4 - O.Z. OOS0/37490 The novel process is carried out as follows: the gas containing C02 and~or H2S is first treated with the methyldiethanolamine-containing absorption liquid in the first absorption stage, where the temperature is main-tained at from 40 to 100C, preferably from S0 to 90C, in particular from 60 to 90C. Advantageously, the gas being treated is fed to the lower part of the first absorption stage, preferably to the lower third, countercurrent to the absorption liquid, ~hich is advan-tageously fed to the upper part of the first absorp-tion stage, preferably to the upper third~ The gas ob-tained at the top of the first absorption stage is fed to a second absorption zone in which, in order to remove further C02 andtor H2S, it is treated at from 30 to 90C, preferably from 40 to 80C, in particular from 50 to 80C, with the methyldiethanolamine-containing absorption Liquid, which has a lower content of C02 and/or H2S than the absorption liquid fed to the first absorption stage. Regarding the second absorption stage too, the gas being treated is advantageously fed to the lower part, preferably to the lower third, of this absorp-t;on stage, countercurrent to the absorption liquid, which is advantageously fed to the upper part, preferabl~ to the upper third, of the second absorption zone. The product gas is taken off at the top of the second absorption zone.
The aqueous absorption liquid laden with C02 and/or H2S and obtained at the bottom of the second absorp-tion stage is fed to the top of the first absorption stage.
The pressures employed in the first and second absorp-tion stages are in general from 5 to 110, preferably from10 to 100, in particular from 20 to 90, bar, and it is pos-sible to use different pressures in the first and second stages. In general, however, the first and second absorp-tion stages are operated under the same, or substantially the same, pressure, the pressure d;fferences being due to, for example, the pressure loss in the absorption stages.
Advantageously used absorption stages are absorption ~9~5S3 - 5 - O.Z. 0050/374~0 columns, in general packed columns or columns equipped with trays. The absorption liquid laden with the acidic gases C02 and/or H2S is taken off in the lo~er part of the first absorption zone, preferably in the lo~er third, in pa^ticuLar at the bottom of this zone.
The laden absorption liquid obtained from the first absorption stage is then regenerated by being let do~n in 2 or more, advantageously from 2 to 5, prefer-ably 2 or 3, flash stages, the f;nal flash stage being oper-ated under reduced pressure, which is generated by meansof a mechan;cal vacuum-producing apparatus and a steam-jet ejector $onnected in series, and, if necessary, the water losses of the system which result from the removal of water in the gas streams taken off at the top of the second absorption stage and from the flash stages and the stripping zone are compensated at the same time by feeding in, at the bottom of the penultimate flash stage, an amount of steam corresponding to the water loss. Preferably, the-pressure maintained in the final flash stage is from û.3 to about 1, preferably from 0.4 to about 1, in particular from û.6 to about 0.9, bar. Examp~es of mechanical vacuum-producing apparatuses are vacuum pumps and, preferably, com-pressors, eg. screw compressors or centrifugal compressors.
The steam-jet ejector is preferably connected downstream of the mechanical vacuum-producing apparatus. In general, the flash stages are operated at from 35 to 100C, pre-ferabiy from 45 to 9ûC, in particular from 55 to 85C.
To compensate for water losses which arise in the process as a result of water being removed in the gas streams taken off at the top of the second absorption stage and from the flash s~ages and the stripping zone, an amount of steam corresponding to the water loss is advantageously fed in at the bottom of the penultimate flash stage. As a rule, the water present in the gas streams taken off is removed substantially in ~he form of steam. Low-pressure, medium-pressure or high-pressure steam, eg. steam under 1.5 to 100 bar, can be fed to the bottom of the 1~90~S3 - 6 - O.Z. 0050/37490 penultimate flash stage. P~efer3bly, lo~-p~essure steam, eg. steam under 1.5 - 10, advantageously 1.5 - 5, bar, is used, since this steam is in general cheapLy available.
S The gas removed at tne too of the final flash stage can be released into the atmosphere or mixed with the gas stream taken off from the penultimate flash stage, and fed for further treatment. In an advantageous embodiment of the process, the steam-jet ejector is con-nected downstream of the mechanical vacuum-producing apparatus and, advantageously, the gas removed at the top of the final flash stage, togetner with the steam used to operate the steam-jet ejector, is fed to the bottom of the penultimate flash stage.
Where steam from the steam-jet ejector is fed to the bottom of the penultimate flash stage, the steam-jet ejector is advantageously operated with the amount of steam required to compensate the water losses of the process. Ho~ever, it is also possible to operate the steam-jet ejector with an amount of steam smaller than that required to compensate the water losses, and in addition to feed in the lacking amount of steam at the bottom of the penultimate flash stage. The steam-jet ejector can be operated using medium-pressure or hi!gh-pressure steam. Medium-pressure steam, eg. under 5-Z0, preferably 5-10, bar, is preferably used.
The penultimate flash stage is advantageously operated under about 1 - 30, preferably about 1 - 25, and in particular about 1 - 20, bar.
Flashing is advantageously carried out using flash chambers which can, for example, also be in the form of columns. These flash chambers need not contain special baffles, although columns equipped with baffles, eg.
packed columns, may also be used.
The gas stream obtained at the top of the final flash stage essentially contains the acidic gases C02 and/or H2S and is advantageously either combined with the gas removed from the top of the penultimate flash ~29(~S53 - 7 - O.Z. 0050/37490 stage or, preferabLy, fed to the bottom of the penultimate flash stage together ~ith the stsam for operating the steam-jet ejector.
A stream of the absorption liquid which is obtained at the bottom of the final flash stage and has been freed to a great extent, advantageously to more than 50%, pre-ferably more than 60Z, from the acidic gases C2 andlor H2S is then recycled as wash liquid to the first absorp-tion stage, where i~ is advantageously introduced at the topv A further stream obtained at the bottom of the f;nal and/or penultimate flash stage or stages is fed, for further regeneration, to a stripping zone, in which the acidic gases C0z and/or H2S still present in this stream are substantially stripped off. In a preferred embodiment of the procedure described above, all of the absorption liquid obtained at the bottom of the final flash stage is recycled to the first absorption stage, and a bleed stream of the absorption liquid obtained at the bottom of the penultimate flash stage is fed to the stripping zone for further regeneration. In another pre-ferred embodiment, some of the absorption liquid obtained at the bottom of the final flash stage is ecycled as a wash liquid to the first absorption stage, and a further bleed stream of the absorption liquid obtained at the bottom of the final flash stage is fed to the str;pping zone for further regeneration. However, it is also pos-sible for a bleed stream of the absorption liquid obtained at the bottom of the final flash stage to be recycled as wash liquid to the first absorption stage, and a further bleed st eam of the absorption liquid obtained at the bottom of the final flash stage and a bleed stream of the absorption liquid obtained at the bottom of the pen-ultimate flash stage to be fed to the stripping zone for further regeneration. The ratio of the amount recycled to the fir-st absorption stage to the amount fed to the stripping zone is in general from 10:1 to 1:2, preferably from 5:1 to 1:1. The gas st eam obtained at the top of 129~SS;3 _ ~ _ o.z. 0050/37490 the stripping zone and essentially conta;n;ng C02 and/or H2S can be removed from the system. However, ;t may also be advantageous if this gas stream, which contains C2 and/or H2S in addition to steam, is recycled to the lower part, preferably the lower half, in particular the lower third, of the penultimate flash stage, in order to reduce the ~ater losses of the system. The stripping zone used is advantageously a stripping column, in general a packed column or a column equipped with trays.
The stripp;ng column is generally operated at from 85 to 115C, preferably from 85 to 110C, in particular from 90 to 110C.
The regenerated absorption liquid obtained at the bottom of the stripping zone is recycled to the second absorption stage, advantageously to the top of this stage.
The Example which follows illustr'ates the inven-tion in mofe detail, the course of the process being sho~n diagrammatically in the Figure.
In the'Figure, a gas which contains C02 and/or H2S, for example a synthesis gas containing C02 as the acidic gas, is passed under superatmospheric Pressure~
via line 1, ;nto the bottom of the first absorption column 2. At the same time, from 20 to 70Z strengh by ~eight aqueous methyldiethanolamine solution, as the absorption liquid, is passed via line 5 to the top of the first absorption column. The prewashed gas obtained at the top of'the first absorption column is introduced into the bottom of the second absorption column 6 via line 3, for fine purification. At the same time, from 20 to 70X strength by weight aqueous methyldiethanolamine solution, ~hich is obtained from the stripping column 22 and is virtually free of acidic gases, is fed, as absorption liquid, via line 20, to the top of the second absorption column. The washed gas is taken off at the top of the second absorption column 6, via line 7. The aqueous absorption liqu;d obtained at the bottom of the 1~,9(3553 - 9 - O.Z. 0050/37490 second absorption column and laden with the acidic gases is fed via lines 14 and 5, together with the absorption liquid obtained from the final flash stage 11 via lines 12 and 13, to the top of the first absorption column 2.
The aqueous absorption liquid obtained at the bottom of the first absorption column 2 and laden with C02 and/or HzS is regenerated by being let down via line 4 into a first flash chamber 8, for example via a valve or, preferably, in an expansion turbine. In th;s stage, an intermediate flash gas is liberated from the absorption liquid and is taken off via line 26. After passing the heat exchanger 27 and the separation vessel 28, the combined gas streams are removed via line Z5. Liquid which separates out in separation vessel 28 is removed via line 18. The partially let down absorption liquid is removed from the bottom of flash chamber 8 via line 9; in a first version of the process, with valve 16 closed and valve 17 open, the said partially let down absorption liquid is let do~n completely via line 10 into a second flash chamber 11, in whic-h reduced pressure down to, for example, O.S bar is maintained by means of the mechanical vacuum-producing apparatus 29, eg. a compressor, and the steam-jet ejector 15. The steam-jet ejector 15 is advan-tageously supplied, via line 32, with the amount of steam required to compensate the water losses of the system.
~he gas removed at the top of flash chamber 11 is fed, together with the steam used for operating the steam-jet ejector 15, to the bottom of the first flash chamber 8, via l-ne 33. Some of the absorption liquid which has been let down and is removed from the bottom of the flash chamber 11 via line 1Z is recycled via lines 13 and 5 to the top of the absorption column 2, while the other part is fed to the top of the stripping column 22 via line 23.
In a second version of the process, with valve 17 closed and valve 16 open, some of the partially let-down absorption liquid removed via line 9 is let down 1~9(~53 - 10 - O.Z. 0050/3~490 via line 10 into ehe second flash chamber 11, whil2 the remainder is fed to the top of the stripping column 22 via lines 31 and Z3. In the second version, all of ehe let-down absorption liquid removed from the bottom of the flash chamber 11 via line 12 is recycled to the top of the absorption column 2 via lines 13 and 5.
The regenerated absorption liquid obtained at the bottom of the stripping column 22 is recycled via line 20 to the top of the second absorption column ~ pass-ing through the heat exchangers 19 and 2t. The waste gas stream obtained at the top of the stripping column 22 and containing C02 and/or H2S is fed via line 24, advantageously to the lower part of the flash chamber 8.
However, it is also possible for the said waste gas stream to be removed directly from the system without being fed beforehand to the flash chamber 8.
The Example which follows illustrates the invention.
EXAMPLE
The gas washer used is shown in the Figure and comprises two absorption c~lumns in succession, two flash chambers in succession, and a stripping column. In the absorption columns, 98ûO kmol/h of a C02-containing synthesis gas are washed with a 50X strength by weight aqueous methyldiethanolamine solution as the absorption liquid. The synthesis gas being treated is fed, under 28 bar, to the bottom of the first absorption column.
This gas originates from a steam reformer and has the following composition:
C218.3X by volume C00.4X by volume H261.0% by volume N22û.0% by volume 35 CH40.1% by volume Ar0.2X by volume The temperature of the absorption liquid in the feed to the first absorption column is 60C, while the ~ O.Z. OOS0/37490 abso-ption l;qu;d fed to the second absorpt;on column is at 75C. The treated synthesis gas removed at the top of the second absorotion column has the fo~lowing 5 compos;tion:
C2 0.01% by volume C0 0.5X by volume H2 74.6% by volume N2 24.5% by volume 10 CHz 0.2X by volume Ar 0.3X by volume.
The laden absorption liquid leaving the bottom of the first absorption column is let down to 5 bar in the first flash chamber, from the top of which 1150 kmol/h of a flash gas are removed. The absorption liquid taken off at the bottom of the second flash chamber is then let down into the second f~ash chamber, in which a pressure of 0.7 bar is maintained by means of a steam-jet ejector and a compressor. About 3/4 of the ~et-down absorption liquid obtained at the bottom of the second flash chambe is recycled to the first absorption column, the remainder being regenerated in the st ipping column and then recycled to the second absorption column.
The novel process permits the use of absorption columns which have a substantially smaller diameter and contain fewer trays, so that the capital costs for the gas washer can be considerably reduced.
Drawing.
It is disclosed, for example in German Patent 2,551,717, that C02 and/or H2S can be removed from gases by means of aqueous solutions of alkanolamines.
Although the known process is very cost-effective, it is not satisfactory in every case.
It is an object of the present invention to pro-vide a process for removing C02 and/or HzS from ~ases containing C02 and/or H2S by means of a-n aqueous alkanol-am;ne-containing absorption liquid, the said process being capable of being operated at lower energy costs and with greater cost-effectiveness than the known processes.
We have found that this and other objects and advantages are achieved, in accordance with the invention, by a process for removing C02 and/or H2S from gases containing C02 and/or H2S by means of an aqueous alkanol-amine-containing absorption liquid, wherein the gas containing C02 and/or H2S is treated in a first absorption stage at from 40 to 100C with an aqueous absorption liquid containing from 20 to 7ûX by weight of methyldiethanolamine, the gas obtained at the top of the first absorption stage is fed to a second absorption stage in which, in order to remove further C02 and/or H2S, it is treated at from 30 to 90C with an aqueous absorption liquid which contains from 20 to 7ûX by ~eight of methyldiethanolamine and has a lower content of C02 and or H2S than the absorption liquid fed to the f;rst absorption stage, the treated gas ;s taken off at the top of the second absorption stage, the aqueous absorption liquid laden with C02 and/or H2S and obtained a~ the bottom of the second absorption stage is fed to the top of the first absorption stage, the aqueous absorption liquid laden ~ith C~2 and/or HzS and obtained in the lower part of the first absorption stage is regenerated ~290SS~
- 2 - o.z. no50/37490 by being let down in two or more flash stages, the final flash stage being operated under reduced pressure which is generated by means of a mechanical vacuum-producing apparatus and a steam-jet ejector, which are connected S in series, a stream of absorption liquid obtained at the bottom of the final flash stage is recycled to the first absorption stage, a further stream of absorpt~ion liquid obtained at the bottom of the final and/or penult;mate flash stage or stages ;s fed to a str;pp;ng zone for further regeneration, and the regnerated absorption l;qu;d obtained at the bottom of the str;pp;ng zone ;s recycled to the second absorpt;on stage.
In an advantageous embod;ment of the process, the water losses result;ng from removal of water ;n the gas streams taken off at the top of the second absorpt;on stage and/or from the flash stages and/or from the str;pping zone are compensated by feed;ng ;n, at the bottom of the penultimate flash stage, an amount of steam corresponding to the water loss.
In another preferred embodiment of the process, the steam-jet ejector is connected downstream of the mechanical vacuum-producing apparatus. It may be advan-tageous for the gas taken off at the top of the f;nal flash stage to be fed ;n, together with the steam used to operate the steam-jet ejector at the bottom of the penult;mate flash stage.
The procedure according to the ;nvention gives a regenerated absorption l;qu;d hav;ng a lower content of C2 and/or H2S, so that ;t ;s possible to c;rculate smaller amounts of absorpt;on l;qu;d. This results in a corresponding saving ;n the energy requ;red for trans-port;ng the absorption liquid. Th;s procedure perm;ts the use of less compl;cated apparatus, thereby reducing the capital costs. Another advantage of the process is that the ~ater balance of the gas washer can be controlled in a simple manner. Using th;s procedure, it is possible to regulate not only the ~ater balance of the gas ~asher 1~0553 - 3 - O.Z. 0050/37490 but also its heat balance, so that any heat exchanger present in the gas washer for regulating the heat balance can be smaller or, if appropriate, can be omitted.
Examples of gases which can be treated us;ng the novel process are coal gasification gases, coke oven gases, natural gases and synthesis gases.
The gases contain in general from 1 to 90, prefer- -ably from 2 to 90, and in particular from 5 to 60, mol%
of C02~ They can also contain H2S as a further acid gas, or can contain H2S alone, for example in an amount of from a few mol ppm, for example 1 mol ppm, to 50 mol%, preferably from 10 mol ppm to 40mol%.
The solvent used for the novel process is an aqueous absorption liquid containing from 20 to 70, pre-ferably from 3û to 65, in particular from 40 to 60, Z byweight of 0ethyldiethanolamine. Advantageously, an aqueous methyldiethanolam;ne solution is used, for example an aqueous solution of technical grade methyldiethanol-am;ne. In an advantageous embodiment of the process, an aqueous methyLdiethanolamine solution is used which additionally contains from 0.05 to 1, in particular from û.1 to 0.8, in particular from 0.1 to 0.6, mole/l of primary amine or alkanolamine, such as monoethanolamine, or preferably secondary amine or alkanolamine, advantage-ously methylmonoethanolam;ne, very particularly advant-ageously piperazine.
The aqueous absorption liquid containing from 20 to 70X by weight of methyldiethanolamine may addi-t;onally contain a physical solvent. Examples of suitable phys;cal solvents are N-methylpyrrolidone, tetramethylene sulfone, methanol and oligoethylene glycol dialkyl ethers, such as oligoethylene glycol methyl isopropyl ether (SEPASOLV MPE) or oligoethylene glycol dimethyl ether (SELEXOL). The physc;al solvent is present in the absorp-tion liquid in general in an amount of from 1 to 60,preferably from 10 to 50, in particular from ZO to 40, X by weight.
* trademarks .~ .
~29(~5~3 - 4 - O.Z. OOS0/37490 The novel process is carried out as follows: the gas containing C02 and~or H2S is first treated with the methyldiethanolamine-containing absorption liquid in the first absorption stage, where the temperature is main-tained at from 40 to 100C, preferably from S0 to 90C, in particular from 60 to 90C. Advantageously, the gas being treated is fed to the lower part of the first absorption stage, preferably to the lower third, countercurrent to the absorption liquid, ~hich is advan-tageously fed to the upper part of the first absorp-tion stage, preferably to the upper third~ The gas ob-tained at the top of the first absorption stage is fed to a second absorption zone in which, in order to remove further C02 andtor H2S, it is treated at from 30 to 90C, preferably from 40 to 80C, in particular from 50 to 80C, with the methyldiethanolamine-containing absorption Liquid, which has a lower content of C02 and/or H2S than the absorption liquid fed to the first absorption stage. Regarding the second absorption stage too, the gas being treated is advantageously fed to the lower part, preferably to the lower third, of this absorp-t;on stage, countercurrent to the absorption liquid, which is advantageously fed to the upper part, preferabl~ to the upper third, of the second absorption zone. The product gas is taken off at the top of the second absorption zone.
The aqueous absorption liquid laden with C02 and/or H2S and obtained at the bottom of the second absorp-tion stage is fed to the top of the first absorption stage.
The pressures employed in the first and second absorp-tion stages are in general from 5 to 110, preferably from10 to 100, in particular from 20 to 90, bar, and it is pos-sible to use different pressures in the first and second stages. In general, however, the first and second absorp-tion stages are operated under the same, or substantially the same, pressure, the pressure d;fferences being due to, for example, the pressure loss in the absorption stages.
Advantageously used absorption stages are absorption ~9~5S3 - 5 - O.Z. 0050/374~0 columns, in general packed columns or columns equipped with trays. The absorption liquid laden with the acidic gases C02 and/or H2S is taken off in the lo~er part of the first absorption zone, preferably in the lo~er third, in pa^ticuLar at the bottom of this zone.
The laden absorption liquid obtained from the first absorption stage is then regenerated by being let do~n in 2 or more, advantageously from 2 to 5, prefer-ably 2 or 3, flash stages, the f;nal flash stage being oper-ated under reduced pressure, which is generated by meansof a mechan;cal vacuum-producing apparatus and a steam-jet ejector $onnected in series, and, if necessary, the water losses of the system which result from the removal of water in the gas streams taken off at the top of the second absorption stage and from the flash stages and the stripping zone are compensated at the same time by feeding in, at the bottom of the penultimate flash stage, an amount of steam corresponding to the water loss. Preferably, the-pressure maintained in the final flash stage is from û.3 to about 1, preferably from 0.4 to about 1, in particular from û.6 to about 0.9, bar. Examp~es of mechanical vacuum-producing apparatuses are vacuum pumps and, preferably, com-pressors, eg. screw compressors or centrifugal compressors.
The steam-jet ejector is preferably connected downstream of the mechanical vacuum-producing apparatus. In general, the flash stages are operated at from 35 to 100C, pre-ferabiy from 45 to 9ûC, in particular from 55 to 85C.
To compensate for water losses which arise in the process as a result of water being removed in the gas streams taken off at the top of the second absorption stage and from the flash s~ages and the stripping zone, an amount of steam corresponding to the water loss is advantageously fed in at the bottom of the penultimate flash stage. As a rule, the water present in the gas streams taken off is removed substantially in ~he form of steam. Low-pressure, medium-pressure or high-pressure steam, eg. steam under 1.5 to 100 bar, can be fed to the bottom of the 1~90~S3 - 6 - O.Z. 0050/37490 penultimate flash stage. P~efer3bly, lo~-p~essure steam, eg. steam under 1.5 - 10, advantageously 1.5 - 5, bar, is used, since this steam is in general cheapLy available.
S The gas removed at tne too of the final flash stage can be released into the atmosphere or mixed with the gas stream taken off from the penultimate flash stage, and fed for further treatment. In an advantageous embodiment of the process, the steam-jet ejector is con-nected downstream of the mechanical vacuum-producing apparatus and, advantageously, the gas removed at the top of the final flash stage, togetner with the steam used to operate the steam-jet ejector, is fed to the bottom of the penultimate flash stage.
Where steam from the steam-jet ejector is fed to the bottom of the penultimate flash stage, the steam-jet ejector is advantageously operated with the amount of steam required to compensate the water losses of the process. Ho~ever, it is also possible to operate the steam-jet ejector with an amount of steam smaller than that required to compensate the water losses, and in addition to feed in the lacking amount of steam at the bottom of the penultimate flash stage. The steam-jet ejector can be operated using medium-pressure or hi!gh-pressure steam. Medium-pressure steam, eg. under 5-Z0, preferably 5-10, bar, is preferably used.
The penultimate flash stage is advantageously operated under about 1 - 30, preferably about 1 - 25, and in particular about 1 - 20, bar.
Flashing is advantageously carried out using flash chambers which can, for example, also be in the form of columns. These flash chambers need not contain special baffles, although columns equipped with baffles, eg.
packed columns, may also be used.
The gas stream obtained at the top of the final flash stage essentially contains the acidic gases C02 and/or H2S and is advantageously either combined with the gas removed from the top of the penultimate flash ~29(~S53 - 7 - O.Z. 0050/37490 stage or, preferabLy, fed to the bottom of the penultimate flash stage together ~ith the stsam for operating the steam-jet ejector.
A stream of the absorption liquid which is obtained at the bottom of the final flash stage and has been freed to a great extent, advantageously to more than 50%, pre-ferably more than 60Z, from the acidic gases C2 andlor H2S is then recycled as wash liquid to the first absorp-tion stage, where i~ is advantageously introduced at the topv A further stream obtained at the bottom of the f;nal and/or penultimate flash stage or stages is fed, for further regeneration, to a stripping zone, in which the acidic gases C0z and/or H2S still present in this stream are substantially stripped off. In a preferred embodiment of the procedure described above, all of the absorption liquid obtained at the bottom of the final flash stage is recycled to the first absorption stage, and a bleed stream of the absorption liquid obtained at the bottom of the penultimate flash stage is fed to the stripping zone for further regeneration. In another pre-ferred embodiment, some of the absorption liquid obtained at the bottom of the final flash stage is ecycled as a wash liquid to the first absorption stage, and a further bleed stream of the absorption liquid obtained at the bottom of the final flash stage is fed to the str;pping zone for further regeneration. However, it is also pos-sible for a bleed stream of the absorption liquid obtained at the bottom of the final flash stage to be recycled as wash liquid to the first absorption stage, and a further bleed st eam of the absorption liquid obtained at the bottom of the final flash stage and a bleed stream of the absorption liquid obtained at the bottom of the pen-ultimate flash stage to be fed to the stripping zone for further regeneration. The ratio of the amount recycled to the fir-st absorption stage to the amount fed to the stripping zone is in general from 10:1 to 1:2, preferably from 5:1 to 1:1. The gas st eam obtained at the top of 129~SS;3 _ ~ _ o.z. 0050/37490 the stripping zone and essentially conta;n;ng C02 and/or H2S can be removed from the system. However, ;t may also be advantageous if this gas stream, which contains C2 and/or H2S in addition to steam, is recycled to the lower part, preferably the lower half, in particular the lower third, of the penultimate flash stage, in order to reduce the ~ater losses of the system. The stripping zone used is advantageously a stripping column, in general a packed column or a column equipped with trays.
The stripp;ng column is generally operated at from 85 to 115C, preferably from 85 to 110C, in particular from 90 to 110C.
The regenerated absorption liquid obtained at the bottom of the stripping zone is recycled to the second absorption stage, advantageously to the top of this stage.
The Example which follows illustr'ates the inven-tion in mofe detail, the course of the process being sho~n diagrammatically in the Figure.
In the'Figure, a gas which contains C02 and/or H2S, for example a synthesis gas containing C02 as the acidic gas, is passed under superatmospheric Pressure~
via line 1, ;nto the bottom of the first absorption column 2. At the same time, from 20 to 70Z strengh by ~eight aqueous methyldiethanolamine solution, as the absorption liquid, is passed via line 5 to the top of the first absorption column. The prewashed gas obtained at the top of'the first absorption column is introduced into the bottom of the second absorption column 6 via line 3, for fine purification. At the same time, from 20 to 70X strength by weight aqueous methyldiethanolamine solution, ~hich is obtained from the stripping column 22 and is virtually free of acidic gases, is fed, as absorption liquid, via line 20, to the top of the second absorption column. The washed gas is taken off at the top of the second absorption column 6, via line 7. The aqueous absorption liqu;d obtained at the bottom of the 1~,9(3553 - 9 - O.Z. 0050/37490 second absorption column and laden with the acidic gases is fed via lines 14 and 5, together with the absorption liquid obtained from the final flash stage 11 via lines 12 and 13, to the top of the first absorption column 2.
The aqueous absorption liquid obtained at the bottom of the first absorption column 2 and laden with C02 and/or HzS is regenerated by being let down via line 4 into a first flash chamber 8, for example via a valve or, preferably, in an expansion turbine. In th;s stage, an intermediate flash gas is liberated from the absorption liquid and is taken off via line 26. After passing the heat exchanger 27 and the separation vessel 28, the combined gas streams are removed via line Z5. Liquid which separates out in separation vessel 28 is removed via line 18. The partially let down absorption liquid is removed from the bottom of flash chamber 8 via line 9; in a first version of the process, with valve 16 closed and valve 17 open, the said partially let down absorption liquid is let do~n completely via line 10 into a second flash chamber 11, in whic-h reduced pressure down to, for example, O.S bar is maintained by means of the mechanical vacuum-producing apparatus 29, eg. a compressor, and the steam-jet ejector 15. The steam-jet ejector 15 is advan-tageously supplied, via line 32, with the amount of steam required to compensate the water losses of the system.
~he gas removed at the top of flash chamber 11 is fed, together with the steam used for operating the steam-jet ejector 15, to the bottom of the first flash chamber 8, via l-ne 33. Some of the absorption liquid which has been let down and is removed from the bottom of the flash chamber 11 via line 1Z is recycled via lines 13 and 5 to the top of the absorption column 2, while the other part is fed to the top of the stripping column 22 via line 23.
In a second version of the process, with valve 17 closed and valve 16 open, some of the partially let-down absorption liquid removed via line 9 is let down 1~9(~53 - 10 - O.Z. 0050/3~490 via line 10 into ehe second flash chamber 11, whil2 the remainder is fed to the top of the stripping column 22 via lines 31 and Z3. In the second version, all of ehe let-down absorption liquid removed from the bottom of the flash chamber 11 via line 12 is recycled to the top of the absorption column 2 via lines 13 and 5.
The regenerated absorption liquid obtained at the bottom of the stripping column 22 is recycled via line 20 to the top of the second absorption column ~ pass-ing through the heat exchangers 19 and 2t. The waste gas stream obtained at the top of the stripping column 22 and containing C02 and/or H2S is fed via line 24, advantageously to the lower part of the flash chamber 8.
However, it is also possible for the said waste gas stream to be removed directly from the system without being fed beforehand to the flash chamber 8.
The Example which follows illustrates the invention.
EXAMPLE
The gas washer used is shown in the Figure and comprises two absorption c~lumns in succession, two flash chambers in succession, and a stripping column. In the absorption columns, 98ûO kmol/h of a C02-containing synthesis gas are washed with a 50X strength by weight aqueous methyldiethanolamine solution as the absorption liquid. The synthesis gas being treated is fed, under 28 bar, to the bottom of the first absorption column.
This gas originates from a steam reformer and has the following composition:
C218.3X by volume C00.4X by volume H261.0% by volume N22û.0% by volume 35 CH40.1% by volume Ar0.2X by volume The temperature of the absorption liquid in the feed to the first absorption column is 60C, while the ~ O.Z. OOS0/37490 abso-ption l;qu;d fed to the second absorpt;on column is at 75C. The treated synthesis gas removed at the top of the second absorotion column has the fo~lowing 5 compos;tion:
C2 0.01% by volume C0 0.5X by volume H2 74.6% by volume N2 24.5% by volume 10 CHz 0.2X by volume Ar 0.3X by volume.
The laden absorption liquid leaving the bottom of the first absorption column is let down to 5 bar in the first flash chamber, from the top of which 1150 kmol/h of a flash gas are removed. The absorption liquid taken off at the bottom of the second flash chamber is then let down into the second f~ash chamber, in which a pressure of 0.7 bar is maintained by means of a steam-jet ejector and a compressor. About 3/4 of the ~et-down absorption liquid obtained at the bottom of the second flash chambe is recycled to the first absorption column, the remainder being regenerated in the st ipping column and then recycled to the second absorption column.
The novel process permits the use of absorption columns which have a substantially smaller diameter and contain fewer trays, so that the capital costs for the gas washer can be considerably reduced.
Drawing.
Claims (4)
1. A process for removing CO2 and/or H2S from a gas containing CO2 and/or H2S by means of an aqueous alkanolamine-containing absorption liquid, wherein the gas containing CO2 and/or H2S is treated in a first absorption stage at from 40 to 100°C with an aqueous absorption liquid containing from 20 to 70% by weight of methyldiethanolamine, the gas obtained at the top of the first absorption stage is fed to a second absorp-tion stage in which, in order to remove further CO2 and/or H2S, it is treated at from 30 to 90°C with an aqueous absorption liquid which contains from 20 to 70%
by weight of methyldiethanolamine and has a lower content of CO2 and/or H2S than the absorption liquid fed to the first absorption stage, the treated gas is taken off at the top of the second absorption stage, the aqueous absorption liquid laden with CO2 and/or H2S and obtained at the bottom of the second absorption stage is fed to the top of the first absorption stage, the aqueous absorp-tion liquid laden with CO2 and/or H2S and obtained in the lower part of the first absorption stage is regenerated by being let down in two or more flash stages, the final flash stage being operated under reduced pressure which is generated by means of a mechanical vacuum-producing apparatus and a steam-jet ejector, which are connected in series, a stream of absorption liquid obtained at the bottom of the final flash stage is recycled to the first absorption stage, a further stream of absorption liquid obtained at the bottom of the final and/or penultimate flash stage or stages is fed to a stripping zone for further regeneration, and the regenerated absorption liquid obtained at the bottom of the stripping zone is recycled to the second absorption stage.
by weight of methyldiethanolamine and has a lower content of CO2 and/or H2S than the absorption liquid fed to the first absorption stage, the treated gas is taken off at the top of the second absorption stage, the aqueous absorption liquid laden with CO2 and/or H2S and obtained at the bottom of the second absorption stage is fed to the top of the first absorption stage, the aqueous absorp-tion liquid laden with CO2 and/or H2S and obtained in the lower part of the first absorption stage is regenerated by being let down in two or more flash stages, the final flash stage being operated under reduced pressure which is generated by means of a mechanical vacuum-producing apparatus and a steam-jet ejector, which are connected in series, a stream of absorption liquid obtained at the bottom of the final flash stage is recycled to the first absorption stage, a further stream of absorption liquid obtained at the bottom of the final and/or penultimate flash stage or stages is fed to a stripping zone for further regeneration, and the regenerated absorption liquid obtained at the bottom of the stripping zone is recycled to the second absorption stage.
2. A process as claimed in claim 1, wherein, to com-pensate water losses resulting from removal of water in the gas streams taken off at the top of the second absorp-tion stage and/or from the flash stages and/or from the O.Z. 0050/37490 stripping zone, an amount of steam corresponding to the water loss is fed in at the bottom of the penultimate flash stage.
3. A process as claimed in claim 1, wherein the steam-jet ejector is connected downstream of the mechanical vacuum-producing apparatus.
4. A process as claimed in claim 3, wherein the gas taken off at the top of the final flash stage is fed, together with the steam used for operating the steam-jet ejector, into the bottom of the penultimate flash stage.
Drawing.
Drawing.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP3445063.7 | 1984-12-11 | ||
| DE19843445063 DE3445063A1 (en) | 1984-12-11 | 1984-12-11 | METHOD FOR REMOVING CO (DOWN ARROW) 2 (DOWN ARROW) AND / OR H (DOWN ARROW) 2 (DOWN ARROW) S FROM GASES |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1290553C true CA1290553C (en) | 1991-10-15 |
Family
ID=6252419
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000496618A Expired - Lifetime CA1290553C (en) | 1984-12-11 | 1985-12-02 | Removal of co -and/or h s from gases |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0190434A3 (en) |
| JP (1) | JPS61138515A (en) |
| CA (1) | CA1290553C (en) |
| DE (1) | DE3445063A1 (en) |
| NO (1) | NO160178C (en) |
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|---|---|---|---|---|
| US7276153B2 (en) | 2000-06-09 | 2007-10-02 | Basf Aktiengesellschaft | Method for neutralising a stream of hydrocarbon fluid |
| US10207217B2 (en) | 2014-08-25 | 2019-02-19 | Basf Se | Removal of hydrogen sulphide and carbon dioxide from a stream of fluid |
| US10214482B2 (en) | 2014-08-25 | 2019-02-26 | Basf Se | Diamine having tert-alkylamino group and primary amino group for use in gas scrubbing |
| US10279309B2 (en) | 2014-08-25 | 2019-05-07 | Basf Se | Removal of carbon dioxide from a fluid flow |
| US10464013B2 (en) | 2014-08-25 | 2019-11-05 | Basf Se | Absorbent for selective removal of hydrogen sulfide from a fluid stream |
| US10493398B2 (en) | 2015-09-29 | 2019-12-03 | Basf Se | Cyclic amine for selectively removing hydrogen sulphide |
| US10525404B2 (en) | 2016-04-25 | 2020-01-07 | Basf Se | Use of morpholine-based hindered amine compounds for selective removal of hydrogen sulfide |
| US11241652B2 (en) | 2017-05-15 | 2022-02-08 | Basf Se (Reitstötter, Kinzebach & Partner) | Absorbent and process for selectively removing hydrogen sulfide |
| US11458433B2 (en) | 2017-09-04 | 2022-10-04 | Basf Se | Absorbent and process for selectively removing hydrogen sulfide |
Families Citing this family (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3518368A1 (en) * | 1985-05-22 | 1986-11-27 | Basf Ag, 6700 Ludwigshafen | METHOD FOR REMOVING CO (DOWN ARROW) 2 (DOWN ARROW) AND / OR H (DOWN ARROW) 2 (DOWN ARROW) S FROM GASES |
| US4814104A (en) * | 1987-02-05 | 1989-03-21 | Uop | Tertiary alkanolamine absorbent containing an ethyleneamine promoter and its method of use |
| DE3922785C2 (en) * | 1989-07-11 | 1994-03-31 | Metallgesellschaft Ag | Process for regenerating a high-boiling wash solution containing CO¶2¶ and H¶2¶S |
| DE19828977A1 (en) * | 1998-06-29 | 1999-12-30 | Basf Ag | Absorbent for removing acidic components from gases |
| DE10135370A1 (en) | 2001-07-20 | 2003-01-30 | Basf Ag | Process for removing acid gases from a gas stream |
| DE10306254A1 (en) | 2003-02-14 | 2004-08-26 | Basf Ag | Absorbent for removing acid gases from fluids, e.g. carbon dioxide, hydrogen sulfide, carbonyl sulfide and mercaptans from various gases, contains tertiary alkanolamine(s) plus mono- and/or bis-(hydroxyethylpiperazine |
| DE102005033837B4 (en) | 2005-07-20 | 2019-02-28 | Basf Se | Process for removing acidic gases and ammonia from a fluid stream |
| CN102292139B (en) | 2009-01-29 | 2014-09-03 | 巴斯夫欧洲公司 | Absorption medium for removing acid gases which comprises amino acid and acid promoter |
| US8221712B2 (en) | 2009-05-12 | 2012-07-17 | Basf Se | Absorption medium for the selective removal of hydrogen sulfide from fluid streams |
| US20130244312A1 (en) * | 2011-10-26 | 2013-09-19 | Phillips 66 Company | Systems and methods for carbon dioxide absorption |
| MX2018004012A (en) | 2015-09-29 | 2018-05-23 | Basf Se | Method for the selective removal of hydrogen sulfide. |
| US10617993B2 (en) | 2015-09-29 | 2020-04-14 | Basf Se | Absorbent for the selective removal of hydrogen sulfide |
| ITUB20154126A1 (en) * | 2015-10-06 | 2017-04-06 | Giammarco Vetrocoke S R L | PROCESS OF PERFECTED REMOVAL OF GASES FROM GASOUS MIXTURES THAT CONTAIN THEM THROUGH THE USE OF WASHING SOLUTIONS WORKING WITH A CHEMICAL-PHYSICAL ABSORPTION AND REGENERATION CYCLE AND PLANT TO IMPLEMENT THE PROCEDURE |
| JP2019520201A (en) | 2016-06-10 | 2019-07-18 | ビーエーエスエフ ソシエタス・ヨーロピアＢａｓｆ Ｓｅ | Cyclohexanediamine for gas scrubbing |
| CN109562320B (en) | 2016-08-01 | 2021-10-12 | 巴斯夫欧洲公司 | Removal of CO from syngas2Two-step Process of |
| EP3579946B1 (en) | 2017-02-10 | 2021-04-07 | Basf Se | Process for removal of acid gases from a fluid stream and corresponding uses |
| CN113453784A (en) | 2019-02-18 | 2021-09-28 | 巴斯夫欧洲公司 | Process for removing acid gases from fluid streams |
| US20240042375A1 (en) | 2019-09-10 | 2024-02-08 | Basf Se | Process for removal of acid gases from a fluid stream |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2551717C3 (en) * | 1975-11-18 | 1980-11-13 | Basf Ag, 6700 Ludwigshafen | and possibly COS from gases |
-
1984
- 1984-12-11 DE DE19843445063 patent/DE3445063A1/en not_active Withdrawn
-
1985
- 1985-11-25 NO NO854706A patent/NO160178C/en not_active IP Right Cessation
- 1985-12-02 CA CA000496618A patent/CA1290553C/en not_active Expired - Lifetime
- 1985-12-06 EP EP85115549A patent/EP0190434A3/en not_active Withdrawn
- 1985-12-09 JP JP60275239A patent/JPS61138515A/en active Granted
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7276153B2 (en) | 2000-06-09 | 2007-10-02 | Basf Aktiengesellschaft | Method for neutralising a stream of hydrocarbon fluid |
| US10207217B2 (en) | 2014-08-25 | 2019-02-19 | Basf Se | Removal of hydrogen sulphide and carbon dioxide from a stream of fluid |
| US10214482B2 (en) | 2014-08-25 | 2019-02-26 | Basf Se | Diamine having tert-alkylamino group and primary amino group for use in gas scrubbing |
| US10279309B2 (en) | 2014-08-25 | 2019-05-07 | Basf Se | Removal of carbon dioxide from a fluid flow |
| US10464013B2 (en) | 2014-08-25 | 2019-11-05 | Basf Se | Absorbent for selective removal of hydrogen sulfide from a fluid stream |
| US11278841B2 (en) | 2014-08-25 | 2022-03-22 | Basf Se | Removal of hydrogen sulphide and carbon dioxide from a stream of fluid |
| US11369919B2 (en) | 2014-08-25 | 2022-06-28 | Basf Se | Absorbent for selective removal of hydrogen sulfide from a fluid stream |
| US10493398B2 (en) | 2015-09-29 | 2019-12-03 | Basf Se | Cyclic amine for selectively removing hydrogen sulphide |
| US11130094B2 (en) | 2015-09-29 | 2021-09-28 | Basf Se | Cyclic amine for selectively removing hydrogen sulphide |
| US10525404B2 (en) | 2016-04-25 | 2020-01-07 | Basf Se | Use of morpholine-based hindered amine compounds for selective removal of hydrogen sulfide |
| US11241652B2 (en) | 2017-05-15 | 2022-02-08 | Basf Se (Reitstötter, Kinzebach & Partner) | Absorbent and process for selectively removing hydrogen sulfide |
| US11458433B2 (en) | 2017-09-04 | 2022-10-04 | Basf Se | Absorbent and process for selectively removing hydrogen sulfide |
Also Published As
| Publication number | Publication date |
|---|---|
| NO854706L (en) | 1986-06-12 |
| NO160178C (en) | 1989-03-22 |
| DE3445063A1 (en) | 1986-06-12 |
| JPH0576326B2 (en) | 1993-10-22 |
| EP0190434A3 (en) | 1987-09-30 |
| JPS61138515A (en) | 1986-06-26 |
| NO160178B (en) | 1988-12-12 |
| EP0190434A2 (en) | 1986-08-13 |
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