CA1291321C - Removal of co- and/or h-s from gases - Google Patents
Removal of co- and/or h-s from gasesInfo
- Publication number
- CA1291321C CA1291321C CA000475993A CA475993A CA1291321C CA 1291321 C CA1291321 C CA 1291321C CA 000475993 A CA000475993 A CA 000475993A CA 475993 A CA475993 A CA 475993A CA 1291321 C CA1291321 C CA 1291321C
- Authority
- CA
- Canada
- Prior art keywords
- absorption
- stage
- flash
- gas
- absorption liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—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
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
- C10K1/14—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors organic
- C10K1/143—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors organic containing amino groups
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0415—Purification by absorption in liquids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0495—Composition of the impurity the impurity being water
-
- 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
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Abstract
Abstract of the Disclosure: CO2 and/or H2S are removed from gases containing CO2 and/or H25 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 adsorption 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, to effect further removal of 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 adsorption liquid fed into the first absorption stage, the treated gas is taken off at the top of the second absorption stage, the aqueous absorption liquid obtained at the bottom of the second absorption stage and preladen with CO2 and/or H2S is fed to the top of the first absorption stage, the aqueous absorption liquid obtained in the lower part of the first absorption stage and laden with CO2 and/or H2S is let down in two or more flash stages in order to regenerate it, the final flash stage being operated under reduced pressure, 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 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, the gas obtained at the top of the first absorption stage is fed to a second absorption stage in which, to effect further removal of 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 adsorption liquid fed into the first absorption stage, the treated gas is taken off at the top of the second absorption stage, the aqueous absorption liquid obtained at the bottom of the second absorption stage and preladen with CO2 and/or H2S is fed to the top of the first absorption stage, the aqueous absorption liquid obtained in the lower part of the first absorption stage and laden with CO2 and/or H2S is let down in two or more flash stages in order to regenerate it, the final flash stage being operated under reduced pressure, 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 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
~l~9~;3'~
The present .invention relates to a process for the .removal of CO2 and/or H2S Erom gases by means of an aqueous rnethyldiethanolamine-containing absorpti.on liquid.
It has been disclosecl, for example in German Pa-tent 2,551,717, that CO2 and/or H~S can be removed from gases by means of aqueous sol.utions of alkanolamines.
Although the conventional method is very cost-efficient, it is not satisfactory in every case.
It is an object of the present invention to provide a process for the removal of CO2 and/or H25 from gases, which can be operated with lower energy consumptior and capital costs.
It has now been found tha-t this and other objects and advantages are achieved, in accordance with the invention, by a process for the removal of CO2 and/or H2$
from gases containing CO2 and/or H2S by means of an aqueous alkanolamine-containing absorption liquid, which process comprises the steps of:
(a) treating a gas containing CO2 and/or H2S, in a first absorption stage, at from 40 to 100C, with an aqueous absorpti.on liquid containing from 20 to 70~ by weight of methyldiethanolamine;
(b) feeding the gas obtained at the top of the first absorption stage to a second absorption stage in which, to effect further removal of CO2 and/or H2S, it is treated at - from 30 to 90C with an aqueous absorption liguid which contains from 20 to 70~ by weigh-t oE methyldiethanolamine and has a lowe.r content of CO2 and/or H2S than the absorption liquid fed into the first absorption stage;
(c) taking off the treated gas at the top of -the second absorption stage;
(d) feeding the aqueous absorption liquid obtained at the bottom of the second absorption stage and preladen with C2 and/or H25 to the top of the first absorption stage;
,~.; .
(e) letting down the aqueous absorption liquid obtained in the lower part of the first absorption stage and laden with CO2 and/or ll2S in two or more flash stages in order to regenerate it, the final flash stage being operated under reduced pressure;
(f) recycling a stream of absorption liquid obtained at the bottom of the final flash stage to the first absorption stage;
(g) feedlng a fur-ther stream of absorption liquid obtained at the bot-tom of the final and/or penultimate flash s-tages to a stripping ~one for further regeneration; and (h) recycl.ing the regenerated absorption liquid obtained at the bo-ttom of the stripping zone to the second absorption stage.
In an advantageous embodiment of the process, in order to compensate for water losses due to water present in the gas streams taken off at the top of the second absorption stage and/or from the flash stages and/or from the stripping zone, an amount of steam corresponding to the water loss is fed in at the bottom of the penultimate flash stage.
In another preferred embodiment of the process, the reduced pressure in the final flash stage is produced by means of a steam ejec-tor. It may be advantageous if the gas taken off at the top of the final flash stage is fed, together with the steam used to operate the steam ejector, to the bottom of the penultimate flash stage.
By operating the final flash stage under reduced pressure, a regenerated absorption liquid having a lower CO2 and/or H2S content is obtained, so that it is possible to circulate smaller amounts of absorption liquid. This results in corresponding savings in energy consumption for transporting the absorption li~uid. At the same time, this procedure permits the use of less complicated apparatus, ~L;29~3'~
with the result that capital costs can also be reduced.
Another advantage of the process is that water losses which arise in the gas washers as a result of water being present in the gas s-treams taken off at the top of the second absorption column and from the flash chambers and the stripper can be compensated for by feeding in at the bottom of the penultimate flash stage an amount of steam corresponding to the water 106~. A~ a ~9~3;~1 - 3 - O.Z. 0050/37006 result of this procedure, it is possible not only ~o regu-late the water balance of the gas ~asher but at the same time to contro~ the heat balance of ~he said unit, so that a heat exchanger present in the gas washer for regu-lating the heat balance can be smaller or, if appropria-te, completely ~ispensed with.
Examp~es of gases treated by the novel process are coal gasification gases, coke oven gases, natural gases and synthesis gases.
The gases have a COz content of in general from 1 to 90, preferably from 2 to 9~, and particularly from 5 to 60, mol Y.~ In addition to the C02, the 3ases can contain H2S as a further actdic gas, or can contain HzS
alone, for example in amounts of a few mol ppm, eg. ~rom 1 mol ppm to 50 mol %, preferably frorn 10 mol ppm to 40 mol ~.
The solvent used for the process according to the invention is an aqueous absorption liquid containing from 20 to 70, preferaDly from 30 to 65, and in parlicular from 4û to 60, X by weight of methyldiethanolamine. Advan-tageously, an aqueous methyldiethanolamine solution is employed, for example an aqueous solution of technical grade methyldiethanolamine. In an advantageous embodiment of the process, the aqueous methyl~iethanoLamine solution used additionally contains from û.O5 to 1, in particu~ar from 0.1 to 0~8, and especially from 0.1 ~o 0.6, mole/l of a primary amine or a~kano~amine, such as monoethano~-amine, or preferably a secondary amine or alkanolamine, advantageously methylmonoethano~amine, very part1cu~ar~y adYantageous~y pipera~ine.
The aqueous a~sorption liquid containing from 20 ; to 70Z ~y weight of methyldie~hanolamine can additionally contain a physical solYent. Examples of sui~ar,~e physical solvents are N-methylpyrrolidone, tetramethylene sulfone, methanol, ~ligoethylene glycol dialky~ ethers, SUCh as oligoethylene glycol methyl isopropyl ether (SEPASOLY MPE~
or oligoethylene glycol dimethyl e~her tSELEXOL~. The * trade mar}c ~2~9~321 ~ ~ ~ -Z~ 005~/37006 physical solvent is present ln the a~sorption liquid in general in an amount of from 1 to 60, preferably from 10 to 50, in particular from 20 to 40, % ~y weight.
The novel process is carried out as follows: the gas containing C0z and/or H2S is first treated, in the first absorption stage, with the methyldiethanolamine-containing absorption liquid, the temperature maintained in the first absorption stage ~eing from 40 to 1~0C, preferably from S0 to 90C, in particular from 60 to 90C. Advantageously, the gas being treated is fed into the lower part of th~ first absorption stage, prefera~y into the lower third, countercurrent to the absorption liquid, which is advantageously introduced into the upper part of the first absorption stage, preferably into the upper third. The gas obtained at the top OT the first absorption stage is fed to a second absorption zone in which, for furthe~ removal of C0z and/or H2S, it is treatea, at from 30 to 90C, prefera~ly from 40 to 80C, in particular from 50 to 80C, with the methy~diethanol-amine-containing absorption liquia whish has a lower content of C02 and/or H2S than that of the absorption liquid fed to the first absorption stage. Regarding the s-cond absorption stage, too, the gas oeing treated is advantageously fed into the lower part, preferably into the lower thir~, of the second a~sorption zone, counter-current to the absorption liquid, which is ad~antageously introduced into the upper part, preferably into the upper third, of the second absorotion ~one. The product gas is taken off at the top of the second absorp~ion zone.
3û The aqueous absorption liquid ~hich is ootained at the bottom of the second a~sorption stage and is prela~en ~it~
C2 and/or H2S is fed to the top of the first absorption stage. In general, pressures of from S to 110, preferabl~
from 10 to 100, in particular from 20 to 90, bar are emploYed in the flrst and second aosorp~ion stages, and the pressures in these two stages may differ from one anothe~r. In general, however, the first and second 1~9~321 - 5 - O.Z. 0050/37006 absorption stages~are operatea under the same pressure, or essentially the same pressure, the pressure differences occurring as a result of, for example, the pressure loss resulting in the absorption stages. The absorption stages used are advantageously absorption columns, in general packed coLumns or columns equipped with trays. Tne absorp-tion liquid laden with the acidic gases C02 and/or ~2S
is taken off in the lower part of the first absorption zone, preferably in the lower third, in particular ac the ~ottom of this a~sorption zone.
Thereafter, the laden a~so~ption ltquld obtained from the first absorption st3ge is regenerated by being let down in not ~ess than 2, advantageously from 2 to 5, preferably 2 or 3, flash stages, the final flash stage being operated under reduced pressure, and, if necessary, the water losses of the system as a result of water being present in the gas streams taken off at the ~op of the second absorption stage and from the flash stages and stripping ~one are compensated for at the same time ~y ~0 feeding in at the bottom of the penultimate flash stage an amount of steam corresponding to the water loss. Pre-ferably, the pressure in the final flash stage is maintained at from 0.3 to a~out 1, preferably from 0.5 to aDout 1, in particular from 0.6 to about 0.9, bar. Suitable apparatuses for producing the reducea pressure in the final flash stage are the apparatuses conventionally used for generating redu-ced pressure, for example mechanical apparatuses, such as vacuum pumps or compressors, eg. screw-type compressors or cen-trifugal compressors, or steam ejectors; it may ~e aavantageous to use mechanical apparatuses for generating reduced pressure.
The temperatures used in the flash stages are in gen~ral from 35 to 100C, preferably from 45 to 90c, in particular from 55 to 85C.
To compensate for the water ~osses which arise 3; in the process as a result of ~ater being present in the gas streams taken off at the top of tne seconc a~sorption stage and from the flash stages and the stripping one, 1~9~3~:1 - 6 - O.Z. OOS0/37006 an amount of steam corresponding to the water loss is fea in, advantageously at the bottom of the penultimate flash stage. As a rule~ the water present in the gas streams taken off 1S essentially removea as steam. Low pressure, medium pressure or high pressure steam, ie. steam unaer from 1.5 to 100 bar, can ~e fed into the bot;om of the penultimate flash stage. Preferab~y, low pressure s~eam, eg. under from 1.5 to 10, advantageously from 1.5 to 5, bar, is used, since this low pressure steam is generally cheaply available.
The gas taken off at the top of the final flash stage can be released into the atmosphere, or can be mi~ea with the gas stream removed from the penultimate flash stage, and the mixture fed for further treatment. In an advantageouS em~odiment of the process, the reduced ores-sure in the final flash stage is produced by means of a steam ejector, and, advantageously, the gas taken off at the top of the final flash stage is fed, together with the steam used to operate the steam ejector, to the bottom of the penultimate flash stage.
If ~e steam from the steam ejector is fed in at the bottom of the penultimate flash stage, the steam ejector is advantageously operated with the amount of steam fequired to compensate for the water losses of the process. However, it is also possible for the steam ejector to be operated with less than the amount of steam required to compensate for the water losses~ and for the amount of steam still required for this purpose additionally to be fed in at the bottom of tne penultimate flash sCage.
The steam ejector can be operated using medium pressure or high pressure s~eam, preferably meaium pressure steam, eg. from S to 20 bar, preferably from 5 eo 10 bar.
The penultimate flash stage is advan~ageously operated under a pressure of about 1 - 30, prefera3!y a~out 1 - 25, in particular about 1 - 20, ûar.
F~ashing is advantageously carried out using flash cham~ers which can, for example, also be in t~e - 7 - 0.Z. 0050/~7006 form of columns. These flash cham~ers need not contain special baffles~ However, it is also possible to use columns equ~pped with baffles, eg. packed columns.
A gas stream which essentially contains the acidic gases C02 andtor HzS is obtained at ~he top of tne final flash stage, and is advantag~ously either combined with the gas taken off at the top of the penultimate flash stage, or is fed, together with the steam for operat-ing the steam ejector, to the botto~ of the penultimate flash stage.
A stream of the absorption liquid which is obtainea at the bottom of the final flash stage ana ~which, in the flash stages, has been freed from the acidic gases C02 and/or H2S to a substantial e~tent, advantageously to more than 50%, preferably to more tnan 60%, is then recyc~ea to the first absorption stage as a wash liquid, and is advantageously introduced at the toP of this absorption - stage. Ahother stream of absorption liquid which is oDtained at the bo~tom of the final and/or penultimate flash stages is fed, for further regeneration, to a stripp-ing zone in which the acidic gases C02 ana/or H2S sti~l present in this stream are substantially stripped off.
In a preferrea embodiment of the procedure describea above, the absorption liquid obtained at the bottom of the final fLash stage is completely recycled to tne first absorption stage, and a bleed stream of the absorption l1quid obtained at the ~ottom of the penu~timate flash stage is fed to the stripping zone, for further regenera-tion. In another preferred embodiment, some of the aosorp-tion liquid obtained at the oottom of the final flashstage is recycled to the first aosorption stage as 3 wash liquid, and a further bleea stream of the absorption liquid ootaine~ at the bottom of the final flash stage is fed to the stripping zone, for further regeneration.
However, it is a-so possirJle for a hleed stream of the absorption liquia obtained at the bottom of the fina~
flash stage to ~e recyclea to the first aosorption stage ~l2~3~L3;~:~
- 8 - 0.Z. 0050/37006 as a wash liquid, and another bleed stream of tne a~sorp-tion liquid obtain~d at the bottom of the final flash stage, and a oleed stream of the absorption liquid ootainea at the bottom of the penultimate flash stage, to be re-cycled to the stripping zone, for further rageneration.
The stream recycled to the first absorption stage and that fed to the stripping zone are in a ratio of, in generaL, from 10:1 to 1:2, preferably from 5:1 to 1:1.
The gas stream obtained at the top of the stripping zone, and essentially containing C2 and/or H2S in ad~ition to steam, can be removed from the system. However, it may also be advantageous to recycle this stream into the lower part, preferably into the lower half, in particular into 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.
In general, the stripping column is operated at from B5 to 115c~ prefera~ly from 85 to 110C, in particular 20 from 90 to 110C.
The regenerated a~$orption liquid obtained at the bottom of the stripping zone is recYcled to the second absorption stage, where it is aavantageously introduced at the top.
The two examples which follow illustrate the invention in more detail, the eourse of the process being shown diagrammatically in Figures 1 an~ 2.
In Figure 1, a gas containing C2 and/or H2S, eg. a synthesis gas contalning C0z as an acidic gas, is passed under superatmosPheric pressure, via line 1, into the ~ottom of the first absorption co~umn 2. At the same time, arl absorption liquid comprising from 20 to 70%
strength by weight aqueous methyldiethanol3mine solution is introduced, via line 5, at the top of the first absorp-tion column. The prewashed gas ootained at the top ofthe first absorption column is 1ntroducea via line 3 in~o the DOttOm of the second a~sorption co~umn, for fina~
129~2~
- 9 - O.Z. ~050/37006 purification. An a~sorption liquid comprising from 20 to 70% strength ~y weight aqueous methyldiethanolamine solution, which is o~tained from the stripping column Z2 an~ is virtually free of acidic gases, is simultaneously introduced at the top of the secona a~sorption column, via line 20. The washed gas is taken off from the top of the second a~sorption column 6, via line 7. The aqueous absorption liquid which is obtained at the bottom of the second a~sorption column and is pr~laden with acidic gases is combined with the absorption liquid obtained via lines 12 and 13 from the final flash stage 11, and the combinea liqui~s are then fed via lines 14 and 5 to the top of the first absorption column 2. The aqueous absorption liqu1d which is obtained at the bottom of the first absorption column Z and is laden wi~h C02 and/or H2S is regenerated ~y being let down via line 4 into a first flash chamber 8, for example via a valve or, preferably, an e~pansion turbine. ~In this stage, an intermediate flash gas is liDerated from tne a~sorption liquid and is taken off ~ia line 2~ and combined with the gas removed from the final flash stage 11 via line 30. After they have passed the heat exchanger 27 and the separation vessel Z8, the com-bined 3as streams are taken off via line 25. Liquia which separates out in separation vessel 28 is removed via line 18. If necessaryr steam, eg. low pressure steam under 2.5 bar, is passed via line 29 into the ~ottom of flash chamber 8, in order to compensate for the water losses in the sys~em. At the bo~tom of the flash chamber 8, the absorption liquid which has been partially let down is taken off via line 9 and, in a first version of the pro-cess, with valve 16 closed and valve 17 open, is let do~n ; completely vi3 line 10 into a second flash cham~er 11 in uhich reduced pressure down to, for example, 0.5 Dar is maintainedj for example ~y means of vacuum pump 15. This lioerates a flash gas which is rich in acidic gas, this flash gas being removed at the top of the flash chamber 11 via line 33 and being com~ined with the gas taken off - 10 - O.Z. 0~50/37006 from the first fLash cham~er 8 via line 26. Some of t~e absorption Liquid ~nich has been let aown, and removed at the ~ottom of the flash chamber 11 via line 12, is recycled via lines 13 and 5 to the top of the absorption column 2, whiLe the other par~ is introduced at ~he top of the stripping column ZZ via line 23.
In a second version of the process, with valve 17 closed and valve 16 open, some of the a~sorption liquid which has been partiall~ let down, and removed via line ~, is let down via line 10 into the second flash chamDer 11, ana the other part is introduced, via lines 31 and 23~ at the top of the stripping column 22. In the secon~
yersion, the aosorption liquid which has been let down, and removed at the bottom of the flash cham~er 11 via line 12, is recycle~ completeLy via lines 13 and 5 to the top of the absorption column 2.
The regenerated aosorption liquid ontainea at the bottom of the stripping column Z2 is recycled, downstream of the heat exchangers 19 and 21, to the top of the secona Z0 absorption column 6, via line 20. The exit ~as stream which contains C02 and/or HzS and is obtained at the top of the stripping column Z2 is fed via line 24, advan-tayeously to the lower part of the fLash chamber 8.
However, it is also possible for the said exit gas stream to ~e removed directLy from the system, without being fed beforehand to the flash chamber 8.
In another embodiment (cf. Fig. 2), the procedure ~essribed for the first embodiment is foLlowed, except that, instead of a vacuum pump, the steam ejector 15 is used for generating the reduced pressure in the secona fLash cham~er 11, the said ejector b~ing supoliea ~itn steam via line 3Z, for example in the amout required to compensate for tne water losses of the system. The gas taken off at the top of the flash chamber 11 is fed, to-gether with the steam use~ for operating tne steam ejector15, ~o the ~ottom of the first flash chamber 8 via line 33.
9~ 3~ 1 ~ O.Z. O0S0/37006 The'Example which follows illustrates the invention.
EXAMPIE
The gas ~asher used is shown in Fig. 2 and com-pr1ses two absorptlon columns connected in series, two flash chambers connected in series, and a stripping column.
In the absorption columns, 9800 kmol/h of a C02 containtng synthesis gas are washed with a 50% strength by weight aqueous methyldieth'anolamine solution as the aosorp~ion liquid. The synthesis gas to be treated is fed under Z8 ~ar to the bottom of the firs~ absorption column. The gas to be.treated originates from a steam reformer and has the following composition:
C2 18.3 vol.%
C0 0.4 vol.X
15 H2 61.0 vol.X
N2 20.0 vol.%
CH4 0.1 vol.%
Ar 0.2 V0~4%
The temperature of the absorption liquid in-th~
feed to the first absorption column is 60C, while that of the absorption liquid fed to the second absorption column is 75C~ The treated synthesis gas ~aken off at the top of the second abso'rption colwmn has the follow-ing composition:
25 C02 0.01 vol.X
CO ~0.5 vol.%
~2 74.~ vol.%
N2 24.5 vol.%
CH2 0.2 vol.%
30 Ar0.3 vol.%
The laden absorption liquid leaving the bottom of the first aDsorption column is let down to S ~ar in the first flash chamber. 1150 kmol~h of a flash gas are removed from the top of the first flash cham~er. Th~ aD-sorption liquid taken off at the bottom of the second flash cham~er is then let down into the secon~ fl3sh cnamber, in which a pressure of 0.7 bar is maintained Dy ~29~L3;;~1 - 12 - O.Z. 0050/37006 means of a steam ejector. About 3/4 of the let-down absorption liquid obtained at lhe ~ottom of the secona flash chamber is recycled to the first absorption column, and the remaining part is regenerated in the stripping column and then recycled to the second absorption column.
Using the novel process, it is possi~le to use absorption columns with substantially smaller diameters and fewer trays, so that the capital costs for tne gas washer can oe substantially reduced.
The present .invention relates to a process for the .removal of CO2 and/or H2S Erom gases by means of an aqueous rnethyldiethanolamine-containing absorpti.on liquid.
It has been disclosecl, for example in German Pa-tent 2,551,717, that CO2 and/or H~S can be removed from gases by means of aqueous sol.utions of alkanolamines.
Although the conventional method is very cost-efficient, it is not satisfactory in every case.
It is an object of the present invention to provide a process for the removal of CO2 and/or H25 from gases, which can be operated with lower energy consumptior and capital costs.
It has now been found tha-t this and other objects and advantages are achieved, in accordance with the invention, by a process for the removal of CO2 and/or H2$
from gases containing CO2 and/or H2S by means of an aqueous alkanolamine-containing absorption liquid, which process comprises the steps of:
(a) treating a gas containing CO2 and/or H2S, in a first absorption stage, at from 40 to 100C, with an aqueous absorpti.on liquid containing from 20 to 70~ by weight of methyldiethanolamine;
(b) feeding the gas obtained at the top of the first absorption stage to a second absorption stage in which, to effect further removal of CO2 and/or H2S, it is treated at - from 30 to 90C with an aqueous absorption liguid which contains from 20 to 70~ by weigh-t oE methyldiethanolamine and has a lowe.r content of CO2 and/or H2S than the absorption liquid fed into the first absorption stage;
(c) taking off the treated gas at the top of -the second absorption stage;
(d) feeding the aqueous absorption liquid obtained at the bottom of the second absorption stage and preladen with C2 and/or H25 to the top of the first absorption stage;
,~.; .
(e) letting down the aqueous absorption liquid obtained in the lower part of the first absorption stage and laden with CO2 and/or ll2S in two or more flash stages in order to regenerate it, the final flash stage being operated under reduced pressure;
(f) recycling a stream of absorption liquid obtained at the bottom of the final flash stage to the first absorption stage;
(g) feedlng a fur-ther stream of absorption liquid obtained at the bot-tom of the final and/or penultimate flash s-tages to a stripping ~one for further regeneration; and (h) recycl.ing the regenerated absorption liquid obtained at the bo-ttom of the stripping zone to the second absorption stage.
In an advantageous embodiment of the process, in order to compensate for water losses due to water present in the gas streams taken off at the top of the second absorption stage and/or from the flash stages and/or from the stripping zone, an amount of steam corresponding to the water loss is fed in at the bottom of the penultimate flash stage.
In another preferred embodiment of the process, the reduced pressure in the final flash stage is produced by means of a steam ejec-tor. It may be advantageous if the gas taken off at the top of the final flash stage is fed, together with the steam used to operate the steam ejector, to the bottom of the penultimate flash stage.
By operating the final flash stage under reduced pressure, a regenerated absorption liquid having a lower CO2 and/or H2S content is obtained, so that it is possible to circulate smaller amounts of absorption liquid. This results in corresponding savings in energy consumption for transporting the absorption li~uid. At the same time, this procedure permits the use of less complicated apparatus, ~L;29~3'~
with the result that capital costs can also be reduced.
Another advantage of the process is that water losses which arise in the gas washers as a result of water being present in the gas s-treams taken off at the top of the second absorption column and from the flash chambers and the stripper can be compensated for by feeding in at the bottom of the penultimate flash stage an amount of steam corresponding to the water 106~. A~ a ~9~3;~1 - 3 - O.Z. 0050/37006 result of this procedure, it is possible not only ~o regu-late the water balance of the gas ~asher but at the same time to contro~ the heat balance of ~he said unit, so that a heat exchanger present in the gas washer for regu-lating the heat balance can be smaller or, if appropria-te, completely ~ispensed with.
Examp~es of gases treated by the novel process are coal gasification gases, coke oven gases, natural gases and synthesis gases.
The gases have a COz content of in general from 1 to 90, preferably from 2 to 9~, and particularly from 5 to 60, mol Y.~ In addition to the C02, the 3ases can contain H2S as a further actdic gas, or can contain HzS
alone, for example in amounts of a few mol ppm, eg. ~rom 1 mol ppm to 50 mol %, preferably frorn 10 mol ppm to 40 mol ~.
The solvent used for the process according to the invention is an aqueous absorption liquid containing from 20 to 70, preferaDly from 30 to 65, and in parlicular from 4û to 60, X by weight of methyldiethanolamine. Advan-tageously, an aqueous methyldiethanolamine solution is employed, for example an aqueous solution of technical grade methyldiethanolamine. In an advantageous embodiment of the process, the aqueous methyl~iethanoLamine solution used additionally contains from û.O5 to 1, in particu~ar from 0.1 to 0~8, and especially from 0.1 ~o 0.6, mole/l of a primary amine or a~kano~amine, such as monoethano~-amine, or preferably a secondary amine or alkanolamine, advantageously methylmonoethano~amine, very part1cu~ar~y adYantageous~y pipera~ine.
The aqueous a~sorption liquid containing from 20 ; to 70Z ~y weight of methyldie~hanolamine can additionally contain a physical solYent. Examples of sui~ar,~e physical solvents are N-methylpyrrolidone, tetramethylene sulfone, methanol, ~ligoethylene glycol dialky~ ethers, SUCh as oligoethylene glycol methyl isopropyl ether (SEPASOLY MPE~
or oligoethylene glycol dimethyl e~her tSELEXOL~. The * trade mar}c ~2~9~321 ~ ~ ~ -Z~ 005~/37006 physical solvent is present ln the a~sorption liquid in general in an amount of from 1 to 60, preferably from 10 to 50, in particular from 20 to 40, % ~y weight.
The novel process is carried out as follows: the gas containing C0z and/or H2S is first treated, in the first absorption stage, with the methyldiethanolamine-containing absorption liquid, the temperature maintained in the first absorption stage ~eing from 40 to 1~0C, preferably from S0 to 90C, in particular from 60 to 90C. Advantageously, the gas being treated is fed into the lower part of th~ first absorption stage, prefera~y into the lower third, countercurrent to the absorption liquid, which is advantageously introduced into the upper part of the first absorption stage, preferably into the upper third. The gas obtained at the top OT the first absorption stage is fed to a second absorption zone in which, for furthe~ removal of C0z and/or H2S, it is treatea, at from 30 to 90C, prefera~ly from 40 to 80C, in particular from 50 to 80C, with the methy~diethanol-amine-containing absorption liquia whish has a lower content of C02 and/or H2S than that of the absorption liquid fed to the first absorption stage. Regarding the s-cond absorption stage, too, the gas oeing treated is advantageously fed into the lower part, preferably into the lower thir~, of the second a~sorption zone, counter-current to the absorption liquid, which is ad~antageously introduced into the upper part, preferably into the upper third, of the second absorotion ~one. The product gas is taken off at the top of the second absorp~ion zone.
3û The aqueous absorption liquid ~hich is ootained at the bottom of the second a~sorption stage and is prela~en ~it~
C2 and/or H2S is fed to the top of the first absorption stage. In general, pressures of from S to 110, preferabl~
from 10 to 100, in particular from 20 to 90, bar are emploYed in the flrst and second aosorp~ion stages, and the pressures in these two stages may differ from one anothe~r. In general, however, the first and second 1~9~321 - 5 - O.Z. 0050/37006 absorption stages~are operatea under the same pressure, or essentially the same pressure, the pressure differences occurring as a result of, for example, the pressure loss resulting in the absorption stages. The absorption stages used are advantageously absorption columns, in general packed coLumns or columns equipped with trays. Tne absorp-tion liquid laden with the acidic gases C02 and/or ~2S
is taken off in the lower part of the first absorption zone, preferably in the lower third, in particular ac the ~ottom of this a~sorption zone.
Thereafter, the laden a~so~ption ltquld obtained from the first absorption st3ge is regenerated by being let down in not ~ess than 2, advantageously from 2 to 5, preferably 2 or 3, flash stages, the final flash stage being operated under reduced pressure, and, if necessary, the water losses of the system as a result of water being present in the gas streams taken off at the ~op of the second absorption stage and from the flash stages and stripping ~one are compensated for at the same time ~y ~0 feeding in at the bottom of the penultimate flash stage an amount of steam corresponding to the water loss. Pre-ferably, the pressure in the final flash stage is maintained at from 0.3 to a~out 1, preferably from 0.5 to aDout 1, in particular from 0.6 to about 0.9, bar. Suitable apparatuses for producing the reducea pressure in the final flash stage are the apparatuses conventionally used for generating redu-ced pressure, for example mechanical apparatuses, such as vacuum pumps or compressors, eg. screw-type compressors or cen-trifugal compressors, or steam ejectors; it may ~e aavantageous to use mechanical apparatuses for generating reduced pressure.
The temperatures used in the flash stages are in gen~ral from 35 to 100C, preferably from 45 to 90c, in particular from 55 to 85C.
To compensate for the water ~osses which arise 3; in the process as a result of ~ater being present in the gas streams taken off at the top of tne seconc a~sorption stage and from the flash stages and the stripping one, 1~9~3~:1 - 6 - O.Z. OOS0/37006 an amount of steam corresponding to the water loss is fea in, advantageously at the bottom of the penultimate flash stage. As a rule~ the water present in the gas streams taken off 1S essentially removea as steam. Low pressure, medium pressure or high pressure steam, ie. steam unaer from 1.5 to 100 bar, can ~e fed into the bot;om of the penultimate flash stage. Preferab~y, low pressure s~eam, eg. under from 1.5 to 10, advantageously from 1.5 to 5, bar, is used, since this low pressure steam is generally cheaply available.
The gas taken off at the top of the final flash stage can be released into the atmosphere, or can be mi~ea with the gas stream removed from the penultimate flash stage, and the mixture fed for further treatment. In an advantageouS em~odiment of the process, the reduced ores-sure in the final flash stage is produced by means of a steam ejector, and, advantageously, the gas taken off at the top of the final flash stage is fed, together with the steam used to operate the steam ejector, to the bottom of the penultimate flash stage.
If ~e steam from the steam ejector is fed in at the bottom of the penultimate flash stage, the steam ejector is advantageously operated with the amount of steam fequired to compensate for the water losses of the process. However, it is also possible for the steam ejector to be operated with less than the amount of steam required to compensate for the water losses~ and for the amount of steam still required for this purpose additionally to be fed in at the bottom of tne penultimate flash sCage.
The steam ejector can be operated using medium pressure or high pressure s~eam, preferably meaium pressure steam, eg. from S to 20 bar, preferably from 5 eo 10 bar.
The penultimate flash stage is advan~ageously operated under a pressure of about 1 - 30, prefera3!y a~out 1 - 25, in particular about 1 - 20, ûar.
F~ashing is advantageously carried out using flash cham~ers which can, for example, also be in t~e - 7 - 0.Z. 0050/~7006 form of columns. These flash cham~ers need not contain special baffles~ However, it is also possible to use columns equ~pped with baffles, eg. packed columns.
A gas stream which essentially contains the acidic gases C02 andtor HzS is obtained at ~he top of tne final flash stage, and is advantag~ously either combined with the gas taken off at the top of the penultimate flash stage, or is fed, together with the steam for operat-ing the steam ejector, to the botto~ of the penultimate flash stage.
A stream of the absorption liquid which is obtainea at the bottom of the final flash stage ana ~which, in the flash stages, has been freed from the acidic gases C02 and/or H2S to a substantial e~tent, advantageously to more than 50%, preferably to more tnan 60%, is then recyc~ea to the first absorption stage as a wash liquid, and is advantageously introduced at the toP of this absorption - stage. Ahother stream of absorption liquid which is oDtained at the bo~tom of the final and/or penultimate flash stages is fed, for further regeneration, to a stripp-ing zone in which the acidic gases C02 ana/or H2S sti~l present in this stream are substantially stripped off.
In a preferrea embodiment of the procedure describea above, the absorption liquid obtained at the bottom of the final fLash stage is completely recycled to tne first absorption stage, and a bleed stream of the absorption l1quid obtained at the ~ottom of the penu~timate flash stage is fed to the stripping zone, for further regenera-tion. In another preferred embodiment, some of the aosorp-tion liquid obtained at the oottom of the final flashstage is recycled to the first aosorption stage as 3 wash liquid, and a further bleea stream of the absorption liquid ootaine~ at the bottom of the final flash stage is fed to the stripping zone, for further regeneration.
However, it is a-so possirJle for a hleed stream of the absorption liquia obtained at the bottom of the fina~
flash stage to ~e recyclea to the first aosorption stage ~l2~3~L3;~:~
- 8 - 0.Z. 0050/37006 as a wash liquid, and another bleed stream of tne a~sorp-tion liquid obtain~d at the bottom of the final flash stage, and a oleed stream of the absorption liquid ootainea at the bottom of the penultimate flash stage, to be re-cycled to the stripping zone, for further rageneration.
The stream recycled to the first absorption stage and that fed to the stripping zone are in a ratio of, in generaL, from 10:1 to 1:2, preferably from 5:1 to 1:1.
The gas stream obtained at the top of the stripping zone, and essentially containing C2 and/or H2S in ad~ition to steam, can be removed from the system. However, it may also be advantageous to recycle this stream into the lower part, preferably into the lower half, in particular into 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.
In general, the stripping column is operated at from B5 to 115c~ prefera~ly from 85 to 110C, in particular 20 from 90 to 110C.
The regenerated a~$orption liquid obtained at the bottom of the stripping zone is recYcled to the second absorption stage, where it is aavantageously introduced at the top.
The two examples which follow illustrate the invention in more detail, the eourse of the process being shown diagrammatically in Figures 1 an~ 2.
In Figure 1, a gas containing C2 and/or H2S, eg. a synthesis gas contalning C0z as an acidic gas, is passed under superatmosPheric pressure, via line 1, into the ~ottom of the first absorption co~umn 2. At the same time, arl absorption liquid comprising from 20 to 70%
strength by weight aqueous methyldiethanol3mine solution is introduced, via line 5, at the top of the first absorp-tion column. The prewashed gas ootained at the top ofthe first absorption column is 1ntroducea via line 3 in~o the DOttOm of the second a~sorption co~umn, for fina~
129~2~
- 9 - O.Z. ~050/37006 purification. An a~sorption liquid comprising from 20 to 70% strength ~y weight aqueous methyldiethanolamine solution, which is o~tained from the stripping column Z2 an~ is virtually free of acidic gases, is simultaneously introduced at the top of the secona a~sorption column, via line 20. The washed gas is taken off from the top of the second a~sorption column 6, via line 7. The aqueous absorption liquid which is obtained at the bottom of the second a~sorption column and is pr~laden with acidic gases is combined with the absorption liquid obtained via lines 12 and 13 from the final flash stage 11, and the combinea liqui~s are then fed via lines 14 and 5 to the top of the first absorption column 2. The aqueous absorption liqu1d which is obtained at the bottom of the first absorption column Z and is laden wi~h C02 and/or H2S is regenerated ~y being let down via line 4 into a first flash chamber 8, for example via a valve or, preferably, an e~pansion turbine. ~In this stage, an intermediate flash gas is liDerated from tne a~sorption liquid and is taken off ~ia line 2~ and combined with the gas removed from the final flash stage 11 via line 30. After they have passed the heat exchanger 27 and the separation vessel Z8, the com-bined 3as streams are taken off via line 25. Liquia which separates out in separation vessel 28 is removed via line 18. If necessaryr steam, eg. low pressure steam under 2.5 bar, is passed via line 29 into the ~ottom of flash chamber 8, in order to compensate for the water losses in the sys~em. At the bo~tom of the flash chamber 8, the absorption liquid which has been partially let down is taken off via line 9 and, in a first version of the pro-cess, with valve 16 closed and valve 17 open, is let do~n ; completely vi3 line 10 into a second flash cham~er 11 in uhich reduced pressure down to, for example, 0.5 Dar is maintainedj for example ~y means of vacuum pump 15. This lioerates a flash gas which is rich in acidic gas, this flash gas being removed at the top of the flash chamber 11 via line 33 and being com~ined with the gas taken off - 10 - O.Z. 0~50/37006 from the first fLash cham~er 8 via line 26. Some of t~e absorption Liquid ~nich has been let aown, and removed at the ~ottom of the flash chamber 11 via line 12, is recycled via lines 13 and 5 to the top of the absorption column 2, whiLe the other par~ is introduced at ~he top of the stripping column ZZ via line 23.
In a second version of the process, with valve 17 closed and valve 16 open, some of the a~sorption liquid which has been partiall~ let down, and removed via line ~, is let down via line 10 into the second flash chamDer 11, ana the other part is introduced, via lines 31 and 23~ at the top of the stripping column 22. In the secon~
yersion, the aosorption liquid which has been let down, and removed at the bottom of the flash cham~er 11 via line 12, is recycle~ completeLy via lines 13 and 5 to the top of the absorption column 2.
The regenerated aosorption liquid ontainea at the bottom of the stripping column Z2 is recycled, downstream of the heat exchangers 19 and 21, to the top of the secona Z0 absorption column 6, via line 20. The exit ~as stream which contains C02 and/or HzS and is obtained at the top of the stripping column Z2 is fed via line 24, advan-tayeously to the lower part of the fLash chamber 8.
However, it is also possible for the said exit gas stream to ~e removed directLy from the system, without being fed beforehand to the flash chamber 8.
In another embodiment (cf. Fig. 2), the procedure ~essribed for the first embodiment is foLlowed, except that, instead of a vacuum pump, the steam ejector 15 is used for generating the reduced pressure in the secona fLash cham~er 11, the said ejector b~ing supoliea ~itn steam via line 3Z, for example in the amout required to compensate for tne water losses of the system. The gas taken off at the top of the flash chamber 11 is fed, to-gether with the steam use~ for operating tne steam ejector15, ~o the ~ottom of the first flash chamber 8 via line 33.
9~ 3~ 1 ~ O.Z. O0S0/37006 The'Example which follows illustrates the invention.
EXAMPIE
The gas ~asher used is shown in Fig. 2 and com-pr1ses two absorptlon columns connected in series, two flash chambers connected in series, and a stripping column.
In the absorption columns, 9800 kmol/h of a C02 containtng synthesis gas are washed with a 50% strength by weight aqueous methyldieth'anolamine solution as the aosorp~ion liquid. The synthesis gas to be treated is fed under Z8 ~ar to the bottom of the firs~ absorption column. The gas to be.treated originates from a steam reformer and has the following composition:
C2 18.3 vol.%
C0 0.4 vol.X
15 H2 61.0 vol.X
N2 20.0 vol.%
CH4 0.1 vol.%
Ar 0.2 V0~4%
The temperature of the absorption liquid in-th~
feed to the first absorption column is 60C, while that of the absorption liquid fed to the second absorption column is 75C~ The treated synthesis gas ~aken off at the top of the second abso'rption colwmn has the follow-ing composition:
25 C02 0.01 vol.X
CO ~0.5 vol.%
~2 74.~ vol.%
N2 24.5 vol.%
CH2 0.2 vol.%
30 Ar0.3 vol.%
The laden absorption liquid leaving the bottom of the first aDsorption column is let down to S ~ar in the first flash chamber. 1150 kmol~h of a flash gas are removed from the top of the first flash cham~er. Th~ aD-sorption liquid taken off at the bottom of the second flash cham~er is then let down into the secon~ fl3sh cnamber, in which a pressure of 0.7 bar is maintained Dy ~29~L3;;~1 - 12 - O.Z. 0050/37006 means of a steam ejector. About 3/4 of the let-down absorption liquid obtained at lhe ~ottom of the secona flash chamber is recycled to the first absorption column, and the remaining part is regenerated in the stripping column and then recycled to the second absorption column.
Using the novel process, it is possi~le to use absorption columns with substantially smaller diameters and fewer trays, so that the capital costs for tne gas washer can oe substantially reduced.
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, said process comprising the steps of:
(a) treating a gas containing CO2 and/or H2S, 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;
(b) feeding the gas obtained at the top of the first absorption stage to a second absorption stage in which, to effect further removal of 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 into the firs-t absorption stage;
(c) taking off the treated gas at the top of the second absorption stage;
(d) feeding the aqueous absorption liquid obtained at the bottom of the second absorption stage and preladen with CO2 and/or H2S to the top of the first absorption stage;
(e) letting down the aqueous absorption liquid obtained in the lower part of the first absorption stage and laden with CO2 and/or H2S in two or more flash stages in order to regenerate it, the final flash stage being operated under reduced pressure;
(f) recycling a stream of absorption liquid obtained a-t the bottom of the final flash stage to the first absorption stage (g) feeding a further stream of absorption liquid obtained at the bottom of the final and/or penultimate flash stages to a stripping zone for further regeneration; and (h) recycling the regenerated absorption liquid obtained at the bottom of the stripping zone to the second absorption stage.
(a) treating a gas containing CO2 and/or H2S, 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;
(b) feeding the gas obtained at the top of the first absorption stage to a second absorption stage in which, to effect further removal of 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 into the firs-t absorption stage;
(c) taking off the treated gas at the top of the second absorption stage;
(d) feeding the aqueous absorption liquid obtained at the bottom of the second absorption stage and preladen with CO2 and/or H2S to the top of the first absorption stage;
(e) letting down the aqueous absorption liquid obtained in the lower part of the first absorption stage and laden with CO2 and/or H2S in two or more flash stages in order to regenerate it, the final flash stage being operated under reduced pressure;
(f) recycling a stream of absorption liquid obtained a-t the bottom of the final flash stage to the first absorption stage (g) feeding a further stream of absorption liquid obtained at the bottom of the final and/or penultimate flash stages to a stripping zone for further regeneration; and (h) recycling the regenerated absorption liquid obtained at the bottom of the stripping zone to the second absorption stage.
2. A process as claimed in claim 1, comprising the additional step of:
(i) feeding an amount of steam corresponding to the water loss to the bottom of the penultimate flash stage in order to compensate for the water losses as a result of water being present in the gas streams taken off at the top of the second absorption stage and/or from the flash stages and/or from the stripping zone.
(i) feeding an amount of steam corresponding to the water loss to the bottom of the penultimate flash stage in order to compensate for the water losses as a result of water being present in the gas streams taken off at the top of the second absorption stage and/or from the flash stages and/or from the stripping zone.
3. A process as claimed in claim 1, wherein the reduced pressure in the final flash stage is produced by means of a steam ejector.
4. A process as claimed in claim 3, comprising the additional step of:
(j) feeding the gas taken off at the top of the final flash stage, together with the steam used for operating the steam ejector, to the bottom of the penultimate flash stage.
(j) feeding the gas taken off at the top of the final flash stage, together with the steam used for operating the steam ejector, to the bottom of the penultimate flash stage.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP3408851.2 | 1984-03-10 | ||
| DE19843408851 DE3408851A1 (en) | 1984-03-10 | 1984-03-10 | 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 |
|---|---|
| CA1291321C true CA1291321C (en) | 1991-10-29 |
Family
ID=6230131
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000475993A Expired - Lifetime CA1291321C (en) | 1984-03-10 | 1985-03-07 | Removal of co- and/or h-s from gases |
Country Status (7)
| Country | Link |
|---|---|
| US (1) | US4997630A (en) |
| EP (1) | EP0159495B1 (en) |
| JP (1) | JPS618112A (en) |
| AT (1) | ATE54060T1 (en) |
| CA (1) | CA1291321C (en) |
| DE (2) | DE3408851A1 (en) |
| NO (1) | NO163172C (en) |
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| US7276153B2 (en) | 2000-06-09 | 2007-10-02 | Basf Aktiengesellschaft | Method for neutralising a stream of hydrocarbon fluid |
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| WO1989011327A1 (en) * | 1988-05-24 | 1989-11-30 | Societe Nationale Elf Aquitaine (Production) | Liquid absorbing acid gases |
| FR2631949B1 (en) * | 1988-05-27 | 1990-09-14 | Inst Francais Du Petrole | PROCESS FOR PRODUCING HIGH PURITY HYDROGEN BY CATALYTIC REFORMING OF METHANOL |
| US5190640A (en) * | 1991-09-18 | 1993-03-02 | Baker Hughes Incorporated | Treatment of oils using aminocarbinols |
| US5603908A (en) * | 1992-09-16 | 1997-02-18 | The Kansai Electric Power Co., Inc. | Process for removing carbon dioxide from combustion gases |
| JP2882950B2 (en) * | 1992-09-16 | 1999-04-19 | 関西電力株式会社 | Method for removing carbon dioxide in flue gas |
| US5556606A (en) * | 1994-10-07 | 1996-09-17 | Khanmamedov; Tofik K. | Method and apparatus for controlling the hydrogen sulfide concentration in the acid gas feedstock of a sulfur recovery unit |
| US5861051A (en) * | 1996-03-06 | 1999-01-19 | Huntsman Petrochemical Corporation | Process for removing carbon dioxide from gas mixture |
| CA2177449C (en) * | 1996-05-20 | 2003-04-29 | Barry Steve Marjanovich | Process for treating a gas stream to selectively separate acid gases therefrom |
| DE19828977A1 (en) * | 1998-06-29 | 1999-12-30 | Basf Ag | Absorbent for removing acidic components from gases |
| US6165432A (en) * | 1998-09-30 | 2000-12-26 | The Dow Chemical Company | Composition and process for removal of acid gases |
| US6337059B1 (en) | 1999-05-03 | 2002-01-08 | Union Carbide Chemicals & Plastics Technology Corporation | Absorbent compositions for the removal of acid gases from gas streams |
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| US2477314A (en) * | 1945-11-27 | 1949-07-26 | Standard Oil Dev Co | Process for purifying gases |
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| DE3030435C2 (en) * | 1980-08-12 | 1982-12-30 | Didier Engineering Gmbh, 4300 Essen | Process for in particular multi-stage washing out of acidic constituents such as CO 2, HCN and in particular H 2 S from gases, in particular coke oven gas, by means of an ammoniacal cycle scrubbing |
| DE3236600A1 (en) * | 1982-10-02 | 1984-04-05 | Basf Ag, 6700 Ludwigshafen | METHOD FOR REMOVING CO (DOWN ARROW) 2 (DOWN ARROW) AND, IF NECESSARY, H (DOWN ARROW) 2 (DOWN ARROW) S FROM NATURAL GAS |
-
1984
- 1984-03-10 DE DE19843408851 patent/DE3408851A1/en not_active Withdrawn
-
1985
- 1985-03-01 EP EP85102325A patent/EP0159495B1/en not_active Expired - Lifetime
- 1985-03-01 AT AT85102325T patent/ATE54060T1/en not_active IP Right Cessation
- 1985-03-01 DE DE8585102325T patent/DE3578379D1/en not_active Expired - Lifetime
- 1985-03-07 CA CA000475993A patent/CA1291321C/en not_active Expired - Lifetime
- 1985-03-08 JP JP60044991A patent/JPS618112A/en active Granted
- 1985-03-08 NO NO850923A patent/NO163172C/en unknown
-
1989
- 1989-03-24 US US07/328,722 patent/US4997630A/en not_active Expired - Fee Related
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| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0159495B1 (en) | 1990-06-27 |
| JPH0421521B2 (en) | 1992-04-10 |
| ATE54060T1 (en) | 1990-07-15 |
| EP0159495A2 (en) | 1985-10-30 |
| US4997630A (en) | 1991-03-05 |
| EP0159495A3 (en) | 1987-09-30 |
| DE3578379D1 (en) | 1990-08-02 |
| NO163172C (en) | 1990-04-18 |
| NO850923L (en) | 1985-09-11 |
| JPS618112A (en) | 1986-01-14 |
| DE3408851A1 (en) | 1985-09-12 |
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