Gas treatment process in ammonia plants with a heat pump system utilizing heat from the lean amine solution

Abstract

The present invention relates to a process for treating a stream comprising CO2 and H2, the process comprising (i) preparing a stream comprising CO2 and H2; (ii) treating the stream prepared in (i) with one or more liquid amine-containing streams, obtaining a gaseous H2-containing stream and a liquid CO2-loaded amine-containing stream; (iii) expanding the liquid CO2-loaded amine-containing stream, obtaining one or more gaseous CO2-containing streams and a liquid CO2-reduced amine-containing stream; (iv) optionally dividing the liquid CO2-reduced amine-containing stream into a first liquid CO2-reduced amine-containing stream and a second liquid CO2-reduced amine-containing stream; (v) stripping CO2 from the liquid CO2-reduced amine-containing stream obtained from (iii) or from the first liquid CO2-reduced amine-containing stream obtained from (iv), obtaining a liquid CO2-depleted amine-containing stream and a gaseous CO2-containing stream; (vi) preparing a liquid H2O-containing stream; (vii) transferring heat from the liquid CO2-depleted amine-containing stream to the liquid H2O-containing stream, obtaining a cooled amine-containing stream and a heated H2O-containing stream; (viii) expanding the heated H2O-containing stream, obtaining a gaseous H2O-containing stream and a liquid H2O-containing stream; (ix) recycling at least a part of the liquid H2O-containing stream into the H2O-containing stream prepared in (vi).

Description

Gas Treatment Process in Ammonia Plants with a Heat Pump System utilizing Heat from the Lean Amine SolutionTECHNICAL FIELDThe present invention relates to a process for treating a stream comprising CO2 and H2, the process particularly including a heat transfer step for heating a ^©-containing stream.INTRODUCTIONCarbon dioxide is one of the most abundant greenhouse gases in the atmosphere. Greenhouse gases are such gases that absorb and emit infrared radiation in the wavelength range emitted by the earth and thus contributing to global warming.Currently, amine gas treating is one of most mature methods for carbon capture. Amine gas treating refers to processes in which acidic gases (sour gas), such as carbon dioxide or hydrogen sulfide are removed from a feed gas stream by absorption in amine solvents. A typical acid gas removal unit (AGRU) comprises an absorber and a regenerator as well an ancillary equipment. In the absorber, the downflowing amine absorbs the acidic components of the feed gas to obtain a sweetened gas or sweet gas stream and an amine solution partially loaden with the acidic components (“rich amine”). The rich amine solution is then fed to a regenerator or stripper where it is heated to strip or flash the desorbed acid gas overhead and to produce a regenerated amine solutions (“lean amine”) which can be recycled to the absorber. Stripped CO2 is then compressed, dried, and optionally refrigerated and transported to its storage destination.Amine gas treating is a relatively energy intensive process. It has been estimated that up to 30 percent of the energy produced by a power station is consumed by carbon capture and sequestration. This energy penalty splits into a value of around 60 % for the amine gas treating process and 30 % for carbon dioxide compression. The energy extensive part of amine gas treating is the stripping of captured carbon dioxide in the stripper. Temperatures in the absorber are usually around 30 to 70 °C, whereas the temperatures necessary to strip carbon dioxide are usually in the range of 100 to 150 °C. The energy required for heating the rich amine is usually supplied by transferring heat from hot process steam to the rich amine in the regenerator. Process steam maybe produced in combined cycle gas power plants. In such cases, steam production from power production may be integrated into the amine gas treating process. However, a steam integration with existing steam sources is not always possible for all AGRUs and the required steam then needs to be provided by a stand-alone process steam production process, such as a steam boiler. Accordingly, numerous activities address the need to reduce the energy consumption of amine gas treating units.One possible strategy to reduce the energy consumption is by trying to improve the cyclic capacity of the amine solvent and reduce the energy required to regenerate the amine solvent. Solvent development is however quite cost and time extensive and often requires the use of specialized, high priced solvent systems leading to higher operational costs.Another strategy employed to reduce the energy consumption of amine gas treating units is to transfer heat from sources within the gas treating unit having a higher temperature to places having a lower temperature. The most prominent example for such a heat-transfer measure is the so-called crossflow heat exchanger (also called “economizer") between the regenerator and the absorber in which the hot lean amine exiting the regenerator is heating up the cold rich amine from the absorber before the rich amine is fed to the regenerator. However, indirect heat exchange by crossflow heat exchangers is usually not sufficient to supply the bulk of the energy required to operate the stripper.US 3823222 A teaches the utilization of the energy contained in hot feed gases which are to be deacidified in an AGRU to produce steam in separate boilers which can be used for steam stripping in the regenerator to heat the reboiler of the regenerator. US 3101996 A also teaches the utilization of hot fluid streams, such as synthesis gas or hydrogen gas obtained in a water shift reaction, to produce steam in separates boilers which can be used to heat the amine stripper. WO 2007 / 12143 A1 discloses two separate cooling stages for cooling hot flue gas from a steam turbine before amine gas treating. In an initial stage, the flue gas is cooled in a heat exchanger by indirect heat exchange with a fluid that is used to heat the stripper. In a second stage, the flue gas is cooled by transferring thermal energy to a heat pump system used to heat the stripper. The heat pump system can be supplemented by heat regenerated in other heat sources, such as the CO2-compression stage.Other heat sources in an amine gas treating process have also been suggested for utilization with a heat pump. WO 2010 / 097047 A1 and WO 2011 / 122525 A1 teach utilizing the heat of absorption in the absorber as a heat source for heat pumps to heat the rich amine solution.JP 2015131735 A uses an intercooler loop in the absorber as a heat source for a heat pump to heat the stripper.WO 2007 / 81214 A1 and ON 114405258 A disclose the use of the condensation energy generated in the condenser of a stripper as a heat source. WO 2012 / 58558 A2 describes the use of the thermal energy of the stripper gas in the overhead condenser as heat source for a heat pump.JP 2010 / 088982 A discloses the use of the heat of compression generated in the compressor(s) used to compress the carbon dioxide to high pressures to heat the rich amine solution.JP 2015 / 131736 A essentially teaches the replacement of the conventional crossflow heat exchanger used to transfer heat from the hot lean amine solution exiting the stripper to the rich amine solution entering the stripper with a heat pump. FR 2968574 A1 discloses the use of multiple heat sources for heat pumps, such as the overhead condenser of the stripper, the lean amine solution exiting the absorber and the overhead condenser of the absorber used to remove water vapor from the sweetened gas.US 4702898 A relates to a process for the removal of acid gases from gas mixtures, such as CO2, wherein ethanolamines could be used as aqueous alkaline scrubbing solution, wherein the process can comprise flashing and stripping of a CO2 and amine-containing solution.CN 103214009 B relates to a process for removing CO2, the process particularly comprising steps of contacting shift gas in a CO2 absorption tower with a lean liquid and a semi-lean liquid; flashing the obtained rich liquid; stripping the liquid phase in a CO2 regeneration, obtaining a lean liquid; stripping the lean liquid in a CO2 absorption tower. A mixture of diethanolamine and a hindered amine, preferably 2-amino-2-methyl-1 -propanol may be used in said process.US 4160810 A relates to a process for treating a stream comprising CO2 and H2, for example gas from reforming of natural gas.US 4591370 A relates to a process for removing acid gases from natural gas or synthesis gases.Thus, there is still a need for a new process for treating a stream comprising CO2 and H2, in particular with respect to its resource- and energy-efficiency.DETAILED DESCRIPTIONThus, it was an object of the present invention to provide a process for treating a stream comprising CO2 and H2, which particularly includes a heat transfer step for recovering energy, in particular for heating a H2O-containing stream, which can be used in other processes. Further, it was an object of the present invention to provide a process enabling production of green steam, in particular when using green power for the components, for example for a compressor.Surprisingly, it has been found that an energy-efficient process for treating CO2 and H2 can be provided, wherein a part of the energy can be recovered by a heat transfer step for heating a H2O-containing stream.Thus, the present invention relates to a process for treating a stream comprising CO2 and H2, the process comprising(i) preparing a stream comprising CO2 and H2;(ii) treating the stream prepared in (i) with one or more liquid amine-containing streams, obtaining one or more gaseous H2-containing streams and one or more liquid CC>2-loaded amine-containing streams; optionally combining the one or more gaseous H2-containing streams if two or more amine-containing streams are applied, obtaining a gaseous H2- containing stream, and optionally combining the one or more liquid CC>2-loaded amine- containing streams if two or more liquid amine-containing streams are applied, obtaining a liquid CC>2-loaded amine-containing stream;(iii) expanding the liquid CC>2-loaded amine-containing stream, obtaining one or more gaseous CC>2-containing streams and a liquid CC>2-reduced amine-containing stream;(iv) optionally dividing the liquid CO2-reduced amine-containing stream into a first liquid CO2- reduced amine-containing stream and a second liquid CO2-reduced amine-containing stream;(v) stripping CO2 from the liquid CO2-reduced amine-containing stream obtained from (iii) or from the first liquid CO2-reduced amine-containing stream obtained from (iv), obtaining a liquid CO2-depleted amine-containing stream and a gaseous CO2-containing stream;(vi) preparing a liquid H2O-containing stream;(vii) transferring heat from the liquid CO2-depleted amine-containing stream to the liquid H2O- containing stream, obtaining a cooled amine-containing stream and a heated H2O-contain- ing stream;(viii) expanding the heated H2O-containing stream, obtaining a gaseous H2O-containing stream and a liquid H2O-containing stream;(ix) recycling at least a part of the liquid H2O-containing stream into the H2O-containing stream prepared in (vi).It is preferred that the H2 comprised in the stream comprising CO2 and H2 prepared in (i) is obtained from a process for converting NH3 to N2 and H2.It is preferred that from 7 to 27 volume-%, more preferably from 12 to 22 volume-%, more preferably from 15 to 19 volume-%, of the stream comprising CO2 and H2 prepared in (i) consist of CO2.It is preferred that from 44 to 64 volume-%, more preferably from 49 to 59 volume-%, more preferably from 52 to 56 volume-%, of the stream comprising CO2 and H2 prepared in (i) consist of H2.It is preferred that the stream comprising CO2 and H2 prepared in (i) further comprises CH4, wherein more preferably from 0.1 to 5 volume-%, more preferably from 0.5 to 3 volume-%, more preferably from 1 to 2 volume-%, of the stream prepared in (i) consist of CH4.It is preferred that the stream comprising CO2 and H2 prepared in (i) further comprises CO, wherein more preferably from 0.1 to 5 volume-%, more preferably from 0.5 to 3 volume-%, more preferably from 1 to 2 volume-%, of the stream prepared in (i) consist of CO.It is preferred that the stream comprising CO2 and H2 prepared in (i) further comprises N2, wherein more preferably from 17 to 37 volume-%, more preferably from 22 to 32 volume-%, more preferably from 25 to 29 volume-%, of the stream comprising CO2 and H2 prepared in (i) consist of N2.It is preferred that from 90 to 100 volume-%, more preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, of the stream comprising CO2 and H2 prepared in (i) consist of CO2, H2, optionally N2, optionally CH4, and optionally CO.It is preferred that the stream comprising CO2 and H2 prepared in (i) has a temperature in the range of from 130 to 180 °C, more preferably from 138 to 169 °C.It is preferred that the stream comprising CO2 and H2 prepared in (i) has a pressure in the range of from 15 to 60 bara, more preferably from 20 to 40 bara, more preferably from 25 to 33 bara.It is preferred that the stream comprising CO2 and H2 prepared in (i) has a volume flow rate in the range of from 10,000 to 500,000 Nm3 / h, more preferably from 150,000 to 300,000 Nm3 / h, more preferably from 170,000 to 239,000 Nm3 / h.The unit Nm3(normal cubic meter) is used to denote a gas volume at a pressure of 1 .01325 bara and a temperature of 0 °C for a molar amount of 0.0446158 kmol.It is preferred that the process further comprises after (i) and prior to (ii)(1.1 ) cooling of the stream comprising CO2 and H2 prepared in (i); wherein the stream comprising CO2 and H2 is more preferably cooled in (i.1 ) to a temperature in the range of from 44 to 64 °C, more preferably from 49 to 60 °C.In the case wherein the process further comprises cooling according to (i.1 ) as defined herein, it is preferred that cooling is conducted with a heat exchanger.It is preferred that the process further comprises after (i) and prior to (ii), preferably after (i.1 ) and prior to (ii)(1.2) expanding the stream comprising CO2 and H2 prepared in (i) or the stream comprising CO2 and H2 cooled in (i.1 ).In the case wherein the process further comprises expanding according to (i.2) as defined herein, it is preferred that the stream comprising CO2 and H2 prepared in (i) or the stream comprising CO2 and H2 cooled in (i.1) is expanded in (i.2) in a vessel.It is preferred that the stream comprising CO2 and H2 obtained from (i), (i.1) or (i.2) is treated in (ii) in one or more columns, more preferably in two columns, wherein the one or more columns are more preferably sequentially arranged.It is preferred that the stream comprising CO2 and H2 obtained from (i), (i.1) or (i.2) is treated in (ii) with two or more liquid amine-containing streams AS(n), wherein n = 1 , 2, 3, 4In the case wherein the stream comprising CO2 and H2 obtained from (i), (i.1 ) or (i.2) is treated in (ii) with two or more liquid amine-containing streams AS(n), wherein n = 1 , 2, 3, 4 it is preferred that the stream comprising CO2 and H2 is treated in (ii) with a first liquid amine-containing stream AS(1 ) and a second liquid amine-containing stream AS(2), wherein treating the stream comprising CO2 and H2 prepared in (i) or obtained from (i.1 ) or (i.2) in (ii) comprises(11.1 ) treating the stream comprising CO2 and H2 prepared in (i) or obtained from (i.1 ) or (i.2) with a first liquid amine-containing stream AS(1), obtaining a (^-containing stream and a first liquid CC>2-loaded amine-containing stream;(11.2) treating the (-^-containing stream obtained from (ii.1 ) with a second liquid amine-containing stream AS(2), obtaining a (-^-containing stream and a second liquid CC>2-loaded amine-containing stream;(11.3) combining the first liquid CC>2-loaded amine-containing stream obtained from (ii.1) and the second liquid CC>2-loaded amine-containing stream obtained from (ii.2), obtaining the liquid CC>2-loaded amine-containing stream.In the case wherein the stream comprising CO2 and H2 is treated in (ii) with a first liquid amine- containing stream AS(1) and a second liquid amine-containing stream AS(2) according to (ii.1),(11.2) and (ii.3) as defined herein, it is preferred that the first liquid amine-containing stream AS(1) has a temperature in the range of from 60 to 95 °C, more preferably from 70 to 90 °C, more preferably from 75 to 86 °C.Further in the case wherein the stream comprising CO2 and H2 is treated in (ii) with a first liquid amine-containing stream AS(1) and a second liquid amine-containing stream AS(2) according to (ii.1 ), (ii.2) and (ii.3) as defined herein, it is preferred that the second liquid amine-containing stream AS(2) has a temperature in the range of from 30 to 80 °C, more preferably from 45 to 65 °C.Further in the case wherein the stream comprising CO2 and H2 is treated in (ii) with a first liquid amine-containing stream AS(1 ) and a second liquid amine-containing stream AS(2) according to (ii.1 ), (ii.2) and (ii.3) as defined herein, it is preferred that the stream comprising CO2 and H2 prepared in (i) or obtained from (i.1 ) or (i.2) is treated in (ii) with the first liquid amine-containing stream AS(1) in counter current flow.Further in the case wherein the stream comprising CO2 and H2 is treated in (ii) with a first liquid amine-containing stream AS(1) and a second liquid amine-containing stream AS(2) according to (ii.1 ), (ii.2) and (ii.3) as defined herein, it is preferred that the stream comprising CO2 and H2 prepared in (i) or obtained from (i.1) or (i.2) is treated in (ii) with the first liquid amine-containing stream AS(1) in a column.In the case wherein the stream comprising CO2 and H2 prepared in (i) or obtained from (i.1) or(1.2) is treated in (ii) with the first liquid amine-containing stream AS(1) in a column, it is preferred that the H2-containing stream obtained in (ii) is removed from the top of the column.Further in the case wherein the stream comprising CO2 and H2 is treated in (ii) with a first liquid amine-containing stream AS(1) and a second liquid amine-containing stream AS(2) according to(11.1 ), (ii.2) and (ii.3) as defined herein, it is preferred that the H2-containing stream obtained in(11.1 ) is treated in (ii.2) with the second liquid amine-containing stream AS(2) in counter current flow.Further in the case wherein the stream comprising CO2 and H2 is treated in (ii) with a first liquid amine-containing stream AS(1 ) and a second liquid amine-containing stream AS(2) according to(11.1 ), (ii-2) and (ii.3) as defined herein, it is preferred that the H2-containing stream obtained in(11.1 ) is treated in (ii.2) with the second liquid amine-containing stream AS(2) in a column.In the case wherein the H2-containing stream obtained in (ii.1) is treated in (ii.2) with the second liquid amine-containing stream AS(2) in a column, it is preferred that the H2-containing stream obtained in (ii.2) is removed from the top of the column.It is preferred that the amine contained in the one or more liquid amine-containing streams independently from one another is a primary amine wherein the amine nitrogen is bonded to a tertiary carbon atom, a secondary amine wherein the amine nitrogen is bonded to at least one secondary carbon atom or at least one tertiary carbon atom, or a tertiary amine.It is preferred that the amine contained in the one or more liquid amine-containing streams independently from one another comprises one or more of an amine having formula I:NR1(R2)2(I), wherein R1is selected from C2-Ce-hydroxyalkyl groups, Ci-C6-alkoxy-C2-Ce-alkyl groups, hy- droxy-Ci-C6-alkoxy-C2-Ce-alkyl groups and 1-piperazinyl-C2-Ce-alkyl groups, and R2is independently from one another selected from H, Ci-Ce-alkyl groups and C2-Ce-hydroxyalkyl groups; an amine having formula II:R3R4N-X-NR5R6(II), wherein R3, R4, R5and R6are independently from one another selected from H, Ci-Ce-alkyl groups, C2-Ce-hydroxyalkyl groups, Ci-C6-alkoxy-C2-Ce-alkyl groups and C2-Ce-aminoalkyl groups, and X is a C2-Ce-alkylene group, -X1-NR7-X2- or -X1-O-X2-, wherein X1and X2are independently from one another C2-Ce-alkylene groups and R7is H, a Ci-Ce-alkyl group, C2-Ce-hy- droxyalkyl group or C2-Ce-aminoalkyl group; and5- to 7-membered saturated heterocycles which have at least one nitrogen atom in the ring and may comprise one or two further heteroatoms selected from nitrogen and oxygen in the ring.It is preferred that the amine contained in the one or more liquid amine-containing streams independently from one another comprises one or more of 2-aminoethanol (monoethanolamine), 2- (methylamino)ethanol, 2-(ethylamino)ethanol, 2-(n-butylamino)ethanol, 2-amino-2-methylpropa- nol, N-(2-aminoethyl)piperazine, methyldiethanolamine, ethyldiethanolamine, dimethylaminopropanol, t-butylaminoethoxyethanol (TBAEE), 2-amino-2-methylpropanol, diisopropanolamine (DIPA), 3-methylaminopropylamine, ethylenediamine, diethylenetriamine, triethylenetetramine,2,2-dimethyl-1 ,3-diaminopropane, hexamethylenediamine, 1 ,4-diaminobutane, 3,3-iminobis- propylamine, tris(2-aminoethyl)amine, bis(3-dimethylaminopropyl)amine, tetramethylhexamethylenediamine, piperazine, 2-methylpiperazine, N-methylpiperazine, 1 -hydroxyethylpiperazine, 1 ,4-bishydroxyethylpiperazine, 4-hydroxyethylpiperidine, homopiperazine, piperidine, 2-hydroxy- ethylpiperidine, triethylenediamine (TEDA), and morpholine.It is preferred that the amine contained in the one or more liquid amine-containing streams independently from one another comprises one or more of monoethanolamine (M EA), methylaminopropylamine (MAPA), piperazine (PIP), diethanolamine (DEA), triethanolamine (TEA), diethylethanolamine (DEEA), diisopropanolamine (DIPA), aminoethoxyethanol (AEE), tert-butyla- minoethoxyethanol (TBAEE), dimethylaminopropanol (DIMAP), methyldiethanolamine (MDEA), triethylenediamine (TEDA), tert-butylaminopropanediol, tert-butylaminoethoxyethylmorpholine, tert-butylaminoethylmorpholine, methoxyethoxyethoxyethyl-tertbutylamine, and tert-butylami- noethylpyrrolidone, more preferably one or more of tert-butylaminoethoxyethanol (TBAEE), methyldiethanolamine (MDEA), and triethylenediamine (TEDA), more preferably triethylenediamine (TEDA).It is preferred that the one or more liquid amine-containing streams independently from one another further comprises one or more alkanolamines, polyamines, 5-, 6- or 7-membered saturated heterocycles having at least one NH group in the ring, which may comprise one or two further heteroatoms selected from nitrogen and oxygen in the ring, wherein the alkanolamines are more preferably selected from the group consisting of monoethanolamine (MEA), diethanolamine (DEA), ethylaminoethanol, 1-amino-2-methyl-propan-2-ol, 2- amino-1 -butanol, 2-(2-aminoethoxy)ethanol, 2-(2-aminoethoxy)ethanamine, and mixtures of two or more thereof, wherein the polyamines are more preferably selected from the group consisting of hexamethylenediamine, 1 ,4-diaminobutane, 1 ,3-diaminopropane, 3-(methylamino)propylamine (MAPA), N-(2-hydroxyethyl)ethylenediamine, 3-(dimethylamino)propylamine (DMAPA), 3-(diethyla- mino)propylamine, N,N'-bis(2-hydroxyethyl)ethylenediamine, and mixtures of two or more thereof, wherein the 5-, 6- or 7-membered saturated heterocycles having at least one NH group in the ring, which may comprise one or two further heteroatoms selected from nitrogen and oxygen in the ring are preferably selected from the group consisting of piperazine, 2-methylpiperazine, N- methylpiperazine, N-ethylpiperazine, N-(2-hydroxyethyl)piperazine, N-(2-aminoethyl)piperazine, homopiperazine, piperidine, morpholine, and mixtures of two or more thereof, more preferably piperazine.It is preferred that treating in one or more of (ii), (ii.1), and (ii.2) is conducted independently from one another at a pressure in the range of from 10 to 60 bara, more preferably 22 to 42 bara, more preferably from 27 to 37 bara, more preferably from 30 to 34 bara.It is preferred that from 0 to 1 .5 volume-%, more preferably from 0.00001 to 1 .1 volume-%, more preferably from 0.0001 to 1.0 volume-%, of the liquid CC>2-loaded amine-containing stream obtained in (ii) consists of CO2.It is preferred that the liquid CC>2-loaded amine-containing stream obtained in (ii) has a temperature in the range of from 70 to 110 °C, more preferably from 80 to 100 °C, more preferably from 85 to 95 °C.It is preferred that the liquid CC>2-loaded amine-containing stream obtained in (ii) has a volume flow rate in the range of from 100 to 5000 m3 / h, more preferably from 2000 to 3000 m3 / h, more preferably from 2300 to 2500 m3 / h.It is preferred that expanding the liquid CC>2-loaded amine-containing stream in (iii) is performed in one or more steps each comprising expanding the liquid CC>2-loaded amine-containing stream, more preferably in two or more steps, more preferably in two or more sequential steps, obtaining one or more gaseous CC>2-containing streams and the liquid CC>2-reduced amine-containing stream.It is preferred that expanding the liquid CC>2-loaded amine-containing stream in (iii) comprises(111.1 ) expanding the liquid CC>2-loaded amine-containing stream, wherein the liquid CC>2-loaded amine-containing stream is more preferably expanded in a first vessel, wherein the liquid CC>2-loaded amine-containing stream is more preferably introduced in the first vessel at the top of the first vessel for expanding, obtaining a gaseous CC>2-containing stream and a liquid CC>2-reduced amine-containing sub-stream;(111.2) expanding the liquid CC>2-reduced amine-containing sub-stream, wherein the liquid CO2- reduced amine-containing sub-stream obtained in (iii.1) is more preferably expanded in a second vessel, obtaining a gaseous CC>2-containing stream and the liquid CC>2-reduced amine-containing stream.It is preferred that the liquid CC>2-reduced amine-containing stream obtained from (iii) has a temperature in the range of from 65 to 90 °C, more preferably from 73 to 83 °C, more preferably from 76 to 80 °C.It is preferred that the liquid CC>2-reduced amine-containing stream obtained in (iii) comprises from 15 to 35 Nm3CO2 per m3of the liquid CC>2-reduced amine-containing stream, more preferably from 20 to 29 Nm3CO2 per m3of the liquid CC>2-reduced amine-containing stream, more preferably from 23 to 26 Nm3CO2 per m3of the liquid CC>2-reduced amine-containing stream.It is preferred that the process further comprises after (iii) and prior to (iv)(iii’) merging the one or more gaseous CC>2-containing streams obtained from (iii), obtaining a gaseous CC>2-containing stream;(iii”) expanding the gaseous CC>2-containing stream obtained from (iii’), wherein the gaseous CC>2-containing stream is preferably expanded in a vessel.It is preferred that the process comprises dividing the liquid CC>2-reduced amine-containing stream into a first liquid CC>2-reduced amine-containing stream and a second liquid CC>2-re- duced amine-containing stream according to (iv).It is preferred that the first liquid CC>2-reduced amine-containing stream comprises from 5 to 25 weight-%, more preferably from 10 to 21 weight-%, more preferably from 13 to 18 weight-%, of the liquid CC>2-reduced amine-containing stream.It is preferred that the second liquid CC>2-reduced amine-containing stream comprises from 75 to 95 weight-%, more preferably from 79 to 90 weight-%, more preferably from 82 to 87 weight- %, of the liquid CC>2-reduced amine-containing stream.It is preferred that the process further comprises after (iv) and prior to (v)(iv’) recycling the second liquid CC>2-reduced amine-containing stream obtained in (iv) into one or more of the one or more liquid amine-containing streams in (ii), preferably into the first liquid amine-containing stream AS(1) according to (ii.1 ).In the case wherein the process further comprises recycling according to (iv’) as defined herein, it is preferred that the second liquid amine-containing stream obtained in (iv) recycled according to (iv’) has a temperature in the range of from 68 to 98 °C, more preferably from 78 to 88 °C, more preferably from 81 to 85 °C.Further in the case wherein the process further comprises recycling according to (iv’) as defined herein, it is preferred that the second liquid amine-containing stream obtained in (iv) recycled according to (iv’) has a volume flow rate in the range of from 100 to 5000 m3 / h, more preferably from 1500 to 2500 m3 / h, more preferably from 1900 to 2100 m3 / h.It is preferred that the process further comprises after (iii) and prior to (v), preferably after (iv) and prior to (v)(iv”) heating the liquid CC>2-reduced amine-containing stream obtained from (iii) or the first liquid CC>2-reduced amine-containing stream obtained from (iv).In the case wherein the process further comprises heating according to (iv”) as defined herein, it is preferred that the liquid CC>2-reduced amine-containing stream obtained from (iii) or the first liquid CC>2-reduced amine-containing stream obtained from (iv) is heated in (iv”) to a temperature in the range of from 85 to 115 °C, more preferably from 95 to 105 °C, more preferably from 98 to 102 °C.Further in the case wherein the process further comprises heating according to (iv”) as defined herein, it is preferred that in (iv”) heating the liquid CC>2-reduced amine-containing stream obtained from (iii) or the first liquid CC>2-reduced amine-containing stream obtained from (iv) is conducted with a heat exchanger, more preferably with a cross heat exchanger.It is preferred that stripping is conducted by heating the liquid CC>2-reduced amine-containing stream obtained from (iii) or the first CC>2-reduced amine-containing stream obtained from (iv) to a temperature in the range of from 85 to 130 °C, more preferably from 95 to 120 °C, more preferably from 100 to 114 °C.It is preferred that stripping is conducted in a column.It is preferred that the liquid CC>2-depleted amine-containing stream obtained from (v) has a temperature in the range of from 97 to 127 °C, more preferably from 107 to 117 °C, more preferably from 110 to 114 °C.It is preferred that the liquid CC>2-depleted amine-containing stream obtained in (v) comprises from 0.01 to 0.40 Nm3CO2 per m3of the liquid CCh-depleted amine-containing stream, more preferably from 0.05 to 0.35 Nm3CO2 per m3of the liquid CC>2-depleted amine-containing stream, more preferably from 0.10 to 0.30 Nm3CO2 per m3of the liquid CC>2-depleted amine- containing stream.It is preferred that the gaseous CC>2-containing stream obtained from (v) has a temperature in the range of from 87 to 117 °C, more preferably from 97 to 107 °C, more preferably from 100 to 104 °C.It is preferred that the gaseous CC>2-containing stream obtained from (v) has a pressure in the range of from 0.10 to 0.60 bara, more preferably 0.20 to 0.50 bara, more preferably from 0.30 to 0.40 bara.It is preferred that the gaseous CC>2-containing stream obtained from (v) is recycled into the one or more columns as defined in any one of the embodiments disclosed herein, wherein the gaseous CC>2-containing stream obtained in (v) is more preferably treated in (ii.2) with the second amine-containing stream AS(2) as defined in any one of the embodiments disclosed herein.It is preferred that the process further comprises after (v) and prior to (vii)(v’) cooling of the liquid CC>2-depleted amine-containing stream obtained from (v); wherein the liquid CC>2-depleted amine-containing stream is preferably cooled in (v’) to a temperature in the range of from 75 to 105 °C, more preferably from 85 to 95 °C, more preferably from 88 to 92 °C.In the case wherein the process further comprises cooling according to (v’), it is preferred that cooling is conducted with a heat exchanger, more preferably with a cross heat exchanger, more preferably with the cross heat exchanger as defined in any one of the embodiments herein.It is preferred that the process further comprises after (v) and prior to (vii), preferably after (v’) and prior to (vii)(v”) compressing the liquid CC>2-depleted amine-containing stream obtained from (v) or (v’).In the case wherein the process further comprises compressing according to (v”), it is preferred that the liquid CC>2-depleted amine-containing stream is compressed in (v”) to a pressure in the range of from 0.20 to 0.60 barg, more preferably from 0.30 to 0.50 barg, more preferably from 0.35 to 0.45 barg.Further in the case wherein the process further comprises compressing according to (v”), it is preferred that the liquid CC>2-depleted amine-containing stream obtained from (v”) has a temperature in the range of from 75 to 105 °C, more preferably from 85 to 95 °C, more preferably from 88 to 92 °C.It is preferred that the liquid l-hO-containing stream prepared in (vi) has a temperature in the range of from 15 to 105 °C, more preferably from 20 to 105 °C.It is preferred that the liquid l-hO-containing stream prepared in (vi) has a pressure in the range of from 0.1 to 1 .5 bara, more preferably from 0.5 to 1 .5 bara, more preferably from 1 .0 to 1 .5 bara.It is preferred that the liquid l-hO-containing stream comprises, more preferably consists of, deionized water.It is preferred that the liquid l-hO-containing stream comprises from 0 to 0.1 Nm3per m3of the liquid CC>2-depleted amine-containing stream, more preferably from 0.01 Nm3per m3of the liquid CC>2-depleted amine-containing stream, more preferably 0 to 0.001 Nm3per m3of the liquid CC>2-depleted amine-containing stream, of one or more of CO2 or N2, preferably of CO2 and N2, wherein the liquid l-hO-containing stream is more preferably substantially free of one or more of CO2 or N2, more preferably of CO2 and N2.It is preferred that heat is transferred in (vii) with a heat exchanger, more preferably a liquid-to- liquid heat exchanger.It is preferred that heat is transferred in (vii) with a heat pump, more preferably a closed-loop heat pump, wherein the heat pump more more preferably comprises a refrigerant selected from groups R717, R1233, preferably R1233ZDE, R1336, preferably R1336MZZE, R600, preferably R600a, and mixtures of two or more thereof.It is preferred that the heated l-hO-containing stream obtained from (vii) comprises a liquid phase, a gaseous phase or a liquid and a gaseous phase, wherein the gaseous phase more preferably comprises steam.It is preferred that the heated l-hO-containing stream obtained from (vii) has a pressure in the range of from 0.02 to 0.71 bara, more preferably from 0.41 to 0.61 bara, more preferably from 0.45 to 0.56 bara.It is preferred that the cooled amine-containing stream obtained from (vii) has a temperature in the range of from 55 to 85 °C, more preferably from 65 to 75 °C, more preferably from 68 to 72 °C.It is preferred that the cooled amine-containing stream obtained from (vii) is recycled into one or more of the one or more liquid amine-containing streams in (ii), more preferably into the second liquid amine-containing stream AS(2) according to (ii.2).It is preferred that the process further comprising after (viii)(viii’) compressing the gaseous l-hO-containing stream obtained from (viii), wherein the gaseous l-hO-containing stream obtained from (viii) is more preferably compressed to a pressure in the range of from 2 to 100 bara, more preferably in the range of from 3 to 50 bara, more preferably in the range of from 3 to 25 bara, more preferably in the range of from 4 to 7 bara, wherein compressing is conducted in one or more compression stages, more preferably in 2 to 4 compression stages, more preferably in 3 compression stages, wherein the one or more compression stages are more preferably conducted sequentially.Further, the present invention relates to a process, preferably according to any one of the embodiments defined herein, comprising the step of converting the gaseous H2-containing stream and / or the gaseous CC>2-containing stream obtainable by or obtained by the process according to any one of the embodiments defined herein to obtain a product Q.In the context of the presently described process, a l-hO-containing stream can be provided, in particular for recycling into the process itself and also for further use in other processes, whereby the l-hO-containing stream can be provided in various pressure and temperature ranges, preferably as steam stream. This relates in particular to the heated l-hO-containing stream obtained from heat transfer according to (vii).With regard to said streams, it is preferable that they are present in gaseous form, i.e. as water vapor. The steam can also be obtained at low pressures, in particular in the vacuum. The steam obtained is preferably compressed further, as also described in the embodiments herein, for example according to process step (viii’) as defined in embodiment 72. Compression of a gaseous l-hO-containing stream can be carried out by means of one or more compressors, preferably a cascade of compressors. The compressors used can be screw compressors, centrifugal blowers and / or axial turbo compressors. Compression preferably involves feeding water to spray off the steam downstream of a compressor with the longest possible inlet section. Preferably, the water is sprayed in order to accelerate evaporation and avoid the formation of droplet streaks, as the function of the blades / vanes of compressors can be impaired by water droplets. Theblades / vanes of axial turbo compressors in particular should not come into contact with water droplets. Alternatively, water can also be sprayed for cooling, for example if screw compressors and / or centrifugal blowers are used.In this way, the steam can be compressed to a pressure in the range from 1 to 120 barg at a temperature in the range from 127 to 450 °C, preferably to a pressure in the range from 1 .5 to 2.0 barg at a temperature in the range from 127 to 200 °C, a pressure in the range from 4.0 to5.8 barg at a temperature in the range from 151 to 200 °C, a pressure in the range from 15.0 to17.8 barg at a temperature in the range from 201 to 250 °C, a pressure in the range from 40 to 49 barg at a temperature in the range from 250 to 300 °C, or a pressure in the range from 100 to 117 barg at a temperature in the range from 310 to 450 °C.Compression to a pressure in the range of 4.0 to 5.8 barg is comparatively more economical than to a pressure in the range of 15.0 to 17.8 barg. Steam at a pressure in the range of 40 to 49 barg or in the range of 100 to 117 barg can be generated by the described compression, but the generation using waste heat from a cracker or similar processes is comparatively more energy-efficient.The compressed steam can be fed into a steam network, preferably in one of the pressure and temperature ranges described herein. Further, the process of the present invention enables production of green steam, in particular if green power is used for the components, for example for a compressor.The compressed steam can be used in the plant used for the treatment of a stream comprising CO2 and H2 or in neighboring plants for the (trace) heating of apparatus and pipelines (e.g. for frost protection in winter), preferably at a pressure in the range of 1 .5 to 2.0 barg. Alternatively, the compressed steam can be used to heat evaporators and reactors in neighboring systems (e.g. to reduce the amount of steam drawn from the grid). It is then often sufficient to compress the steam to 3 barg, for example. In another alternative, the compressed steam can be mixed with green steam, even at different pressure levels. In this case, the “green steam” produced via waste heat and with the help of green electrical energy in compressors can be allocated to other systems or their products in the balance sheet when connected through pipelines or a steam network. This can reduce the product carbon footprint (PCF) of products that are produced in plants that do not generate green steam.According to a further aspect, the present invention relates to a process, preferably to the process as described above, which (further) comprises the step of converting the gaseous Fh-con- taining stream and / or the gaseous CC>2-containing stream obtainable by or obtained by the process described herein or a chemical material obtainable by or obtained by the process described herein to obtain a product Q. Yet further, the present invention relates to a process comprising the step of using the gaseous H2-containing stream and / or the gaseous CC>2-containing stream as described herein; and preferably converting the H2 and / or the CO2 comprised in said streams to obtain a product Q.Preferably, the product Q is selected from: building block or monomer; or polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acry- late hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.Regarding this process from which the product Q, is obtained, it is preferred: that the content of the H stemming from the gaseous H2-containing stream and / or the content of the C stemming from the gaseous CC>2-containing stream in the product Q, is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or that the content of the H stemming from the gaseous H2-containing stream and / or the content of the C stemming from the gaseous CC>2-containing stream in the product Q is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; wherein it is more preferred that the respective content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.The publication Prior Art Disclosure; Issue 684; paragraphs

[1000] to

[8005] ; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1 , which is incorporated herein by reference in its entirety. Preferably, the product Q is a product as described in Reference RF1 ; paragraphs

[1000] to

[8005] , Preferably, the process described herein is further a process for the production of a product.The converting step to obtain the product Q preferably comprises one or more step(s) as described below and can be performed by conventional methods well known to a person skilled in the art. The converting step preferably comprises one or more step(s) selected from: recycling, preferably depolymerizing, gasifying, pyrolyzing, and / or steam cracking; and / or purifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, absorbing, adsorbing and / or subjecting to ion exchanger; and / or assembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and / or compounding; and / or forming, preferably foaming, extruding and / or molding; and / or finishing, preferably coating and / or smoothing.In addition, the one or more step(s) are described in detail in Reference RF1 ; paragraphs

[1000] to

[8005] ,The term “building block”, as used in the context of the product Q herein, comprises compounds, which are in a gaseous or liquid state under standard conditions of 0°C and 0.1 MPa. Building blocks are typically used in chemical industry to form secondary products, which provide a higher structural complexity and / or higher molecular weight than the building block on which the secondary product is based. The building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxid, ethylene oxide, ethylene glycols, syngas comprising a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes and aromatic compounds. The alkanes, alkenes, alkynes and aromatic compounds comprise in particular 1 to 12 carbon atoms, respectively.The term “monomer”, as used in the context of the product Q herein, comprises molecules, which can react with each other to form polymer chains by polymerization. The monomer is preferably selected from the group consisting of (meth)acrylic acid, salts of (meth)acrylic acid; in particular sodium, potassium and zinc salts; (meth)acrolein and (meth)acrylates. (Meth)acry- lates comprising 1 to 22 carbon atoms are preferred, in particular comprising 1 to 8 carbon atoms. The terms (meth)acrylic acid, (meth)acrolein or (meth)acrylate relate to acrylic acid, acrolein or acrylate and also to methacrylic acid, methacrolein or methacrylate, where applicable. Further, the monomer can be selected from hexamethylenediamine (HMD) and adipic acid.The building block can further be an intermediate compound. The term “intermediate compound”, as used in the context of the product Q herein, comprises organic reagents, which are applied for formation of compounds with higher molecular complexity. The intermediate compound can be selected for example from the group consisting of phosgene, polyisocyanates and propylene oxide. The polyisocyanates are in particular aromatic di- and polyisocyanates, preferably toluene diisocyanate (TDI) and / or diphenylmethane diisocyanate (MDI).The building block and the monomer and typical converting step(s) to obtain the building block or monomer are described in more detail in paragraphs

[1000] to

[1012] of Reference RF1.The term “polymer A”, as used in the context of the product Q herein, comprises thermoplastic, e.g., polyamide or thermoplastic polyurethane, thermoset, e.g., polyurethane, elastomer, e.g., polybutadiene, or a copolymer or a mixture thereof and is defined in more detail in paragraphs

[2001] to

[2007] of Reference RF1.The term “polymer composition A”, as used in the context of the product Q herein, comprises all compositions comprising a polymer as described above and one or more additive(s), e.g. reinforcement, colorant, modifier and / or flame retardant, and is defined in more detail in paragraph

[2008] of Reference RF1 .The term “polymer product A”, as used in the context of the product Q herein, comprises any product comprising the polymer A and / or polymer composition A as described above and is defined in more detail in paragraphs

[2009] and

[2010] of Reference RF1.The step(s) to obtain the polymer, preferably polymer A, polymer composition, preferably polymer composition A or polymer product, preferably polymer product A is / are described in more detail in paragraph

[2011] of Reference RF1.The term “industrial use polymer”, as used in the context of the product Q herein, comprises rheology, polycarboxylate, alkoxylated polyalkylenamine, alkoxylated polyalkylenimine, poly- ether-based, dye inhibition and soil release cleaning polymers defined in more detail in paragraphs

[3035] to

[3044] of Reference RF1. The term “industrial use surfactant”, as used in the context of the product Q herein, comprises non-ionic, anionic and amphoteric industrial use surfactants defined in more detail in paragraphs

[3008] to

[3034] of Reference RF1. The term “industrial use descaling compound”, as used in the context of the product Q herein, comprises non-phosphate based builders (NPB) and phosphonates (CoP) described in more detail in paragraphs

[3001] to

[3005] of Reference RF1. The term “industrial use biocide”, as used in the context of the product Q herein, refers to a chemical compound that kills microorganisms or inhibits their growth or reproduction defined in more detail in paragraphs

[3006] to

[3007] of Reference RF1 . The term “industrial use solvent”, as used in the context of the product Q herein, comprises alkyl amides, alkyl lactamides, alkyl esters, lactate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic esters defined in more detail in paragraphs

[3045] to

[3055] of Reference RF1 . The term “industrial use dispersant”, as used in the context of the product Q herein, comprises anionic and non-ionic industrial use dispersants defined in more detail in paragraphs

[3056] to

[3058] of Reference RF1. The term “composition and / or formulation thereof’ with reference to the industrial use polymers, industrial use surfactants, descaling compounds and / or industrial use biocides refers to industrial use compositions and / or institutional use products and / or fabric and home care products and / or personal care products defined in more detail in paragraph

[3059] of Reference RF1. The converting step(s) to obtain the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3060] of Reference RF1. The converting steps to obtain the industrial use composition or formulation of the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3061] of Reference RF1.The term “agrochemical composition”, as used in the context of the product Q herein, typically relates to a composition comprising an agrochemically active ingredient and at least one agrochemical formulation auxiliary. Examples of agrochemical compositions, active ingredients and auxiliaries are described in more detail in Reference RF1 , paragraph

[4001] ,The agrochemical composition may take the form of any customary formulation. The agrochemical compositions are prepared in a known manner, e.g. described by Mollet and Grubemann, Formulation technology, Wiley VCH, Weinheim, 2001 ; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005. The converting step(s) to obtain the agrochemically active ingredients and auxiliaries may be conducted in analogy to the production step(s) of their analogues that are based on petrochemicals or other precursors that are not gained by recycling processes. In addition, conversion to compounds mentioned in sections “Polymer” and “Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or compositions or formulations thereof’ may be performed as described in these sections as well as the respective paragraphs in Reference RF1.The term active pharmaceutical ingredients and / or intermediates thereof, as used in the context of the product Q herein, comprises substances that provide pharmacological activity or other direct effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect the structure or any function of the body. Intermediates thereof are isolated products that are generated during a multi-step route of synthesis of an active pharmaceutical ingredient. The term pharmaceutical excipients, as used in the context of the product Q herein, comprises compounds or compound mixtures used in compositions for various pharmaceutical applications, which are not substantially pharmaceutically active on itself. Active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients are defined in more detail in paragraph

[5001] of Reference RF1.The converting step(s) to obtain the active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms animal feed additives, human food additives, dietary supplements, as used in the context of the product Q herein, comprises Vitamins, Pro-Vitamins and active metabolites thereof including intermediates and precursors, especially Vitamin A, B, E, D, K and esters thereof, like acetate, propionate, palmitate esters or alcohols thereof like retinol or salts thereof and any combinations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls including their intermediates and precursors as well as mixtures and derivates thereof, especially beta carotene, Canthaxanthin, Citranaxanthin, Astaxanthin, Zeaxanthin, Lutein, Lycopene, Apo-carotenoids, and any combinations thereof; organic acids, especially formic acid, propionic acid and salts thereof, such as sodium, calcium or ammonium salts, and any combinations thereof, such as but not limited to mixtures of formic acid and sodium formiate, propionic acid and ammonium propionate, formic acid and propionic acid, formic acid and sodium formiate and propionic acid, propionic acid and sodium propionate and formic acid and sodiumformiate; glycerides of carboxylic acids and short and medium chain fatty acids, conjugated linoleic acids, such as omega-6 fatty acid (C18:2) methyl ester and 1 ,2-propandiol and beverage stabilizers, such as polyvinylpyrrolidone-polymer or polyvinylimidazole / polyvinylpyrrolidone-co- polymer. Animal feed additives, human food additives and dietary supplements are defined in more detail in paragraph

[5002] of Reference RF1.The converting step(s) to obtain the animal feed additives, human food additives, dietary supplements may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms aroma chemical and aroma composition as used in the context of the product Q herein, comprise a volatile organic substance with a molecular weight between 70-250 g / mol comprising a functional group with a carbon skeleton of C5-C16 carbon atoms comprising linear, branched, cyclic, for example with a ring size of C5-C18, bicyclic or tricyclic aliphatic chains and but not necessarily one or more unsaturated structural elements like double bonds, triple bonds, aromatics or heteroaromatics and preferably the one or more additional functional groups are selected from alcohol, ether, ester, ketone, aldehyde, acetal, carboxylic acid, nitrile, thiol, amine. In one aspect, the aroma chemical is a terpene-based aroma chemical, for example selected from monoterpenes and monoterpenoids, sesquiterpenes and sesquiterpenoids, diterpenes, triterpenes or tetraterpenes. Aroma chemicals can be combined with further aroma chemicals to give an aroma composition. Aroma chemicals and aroma compositions are defined in more detail in paragraph

[5003] of Reference RF1.The converting step(s) to obtain the aroma chemical and aroma composition may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The term “aqueous polymer dispersion”, as used in the context of the product Q herein, comprises aqueous composition(s) comprising dispersed polymer(s) and is defined in more detail in the section

[6001] entitled “aqueous polymer dispersion” of Reference RF1. The dispersed polymers) may be selected from acrylic emulsion polymer(s), styrene acrylic emulsion polymer(s), styrene butadiene dispersion(s), aqueous dispersion(s) comprising composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curable polyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s). The term “emulsion polymer”, as used in the context of the product Q herein, comprises polymer(s) made by free-radical emulsion polymerization. Aqueous polyurethane dispersion(s) are defined in more detail in the section

[6002] entitled “Polyurethane dispersions” of Reference RF1. UV-curable polyurethane(s) is / are defined in more detail in the section

[6017] of Reference RF1. Polyurethane - poly(meth)acrylate hybrid polymer(s) is / are defined in more detail in the section

[6016] of Reference RF1.The term “polymeric dispersant”, as used in the context of the product Q herein, comprises preferably polymer(s) comprising polyether side chain, in particular polycarboxylate ether polymer(s) and polycondensation product(s) defined in more detail in paragraph

[6020] entitled “Polymeric dispersant” of Reference RF1 .The converting (polymerization) step(s) to obtain the aqueous polymer dispersion(s) comprising emulsion polymer(s) is / are defined in more detail in the section

[6003] entitled “Emulsion polymerization” of Reference RF1.The converting (polymerization) step(s) to obtain the aqueous polyurethane dispersion(s) is / are defined in more detail in the section

[6014] entitled “Process for the preparation of aqueous polyurethane dispersions” and section [6017)] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” of Reference RF1 . Composition(s) and uses of aqueous polymer dispersion(s) and of polymeric dispersant(s) are defined in more detail in the following sections of Reference RF1 : section

[6004] entitled “Uses of aqueous polymer dispersions”, section

[6005] entitled “Binders for architectural and construction coatings” section

[6006] entitled “Binders for paper coating” section

[6007] entitled “Binders for fiber bonding” section

[6008] entitled “Adhesive polymers and adhesive compositions” section

[6015] entitled “Aqueous polyurethane dispersions suitable for use in coating compositions” section

[6016] entitled “Aqueous polyurethane - poly(meth)acrylate hybride polymer dispersions suitable for use in coating compositions” section

[6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” section

[6018] entitled “Inorganic binder compositions comprising polymeric dispersants and their use”

[6019] 100% curable coating compositionsUV-crosslinkable poly(meth)acrylate(s) and its / their uses are defined in more detail in section

[6009] entitled “UV-crosslinkable poly(meth)acrylates for use in UV-curable solvent-free hotmelt adhesives and their use for making pressure-sensitive self-adhesive articles” of Reference RF1 .Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section

[6010] entitled “Polyisocyanates” of Reference RF1 .Hyperbranched polyester polyol(s) and its / their uses are defined in more detail in section

[6011] entitled “Organic solvent based hyperbranched polyester polyols suitable for use in coating compositions” of Reference RF1. The converting step(s) to obtain the hyperbranched polyester polyols is / are defined in more detail in the section

[6012] entitled “Preparation of organic solvent based hyperbranched polyester polyols” of Reference RF1. Coating composition(s) comprising hyperbranched polyester polyol(s), polyisocyanate(s) and additive(s) and substrate(s) coated therewith are defined in more detail in section

[6013] entitled “Organic solvent based two component coating compositions comprising hyperbranched polyester polyols and polyisocyanates” of Reference RF1.Unsaturated polyester polyol(s), solvent-based coating composition(s) comprising said unsaturated polyester polyol(s) and substrate(s) for coating with said coating composition(s) are defined in more detail in section

[6018] entitled “Organic solvent based coating composition comprising unsaturated polyester polyols” of Reference RF1 . 100% curable coating composition(s) is / are defined in more detail in section

[6019] of Reference RF1.Polymeric dispersant(s) for inorganic binder compositions is / are defined in more detail in section

[6020] of Reference RF1 . The inorganic binder composition(s) comprising the polymeric dispersants and their use are defined in more detail in section

[6021] of Reference RF1 . The converting step(s) to obtain the polymeric dispersant(s) are defined in more detail in section

[6020] of Reference RF1 . The term “inorganic binder composition” comprising the polymeric dispersants), as used in the context of the product Q herein, comprises preferably in particular hydraulically setting compositions and compositions comprising calcium sulfate and is defined in more detail in section

[6021] of Reference RF1 entitled “Inorganic binder compositions comprising the polymeric dispersant and their use”. Specific building material formulation(s) comprising polymeric dispersant(s) or building product(s) produced by a building material formulation comprising a polymeric dispersant are disclosed in more detail in section

[6021] of Reference RF1 .The term “cosmetic surfactant”, as used in the context of the product Q herein, comprises nonionic, anionic, cationic and amphoteric surfactants and is defined in more detail in paragraph

[7002] of Reference RF1. The term “emollient”, as used in the context of the product Q herein, refers to a chemical compound used for protecting, moisturizing, and / or lubricating the skin and is defined in more detail in paragraph

[7003] of Reference RF1 . The term “wax”, as used in the context of the product Q herein, comprises pearlizers and opacifiers and is defined in more detail in paragraph

[7004] of Reference RF1 . The term “cosmetic polymer”, as used in the context of the product Q herein, comprises any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph

[7005] of Reference RF1 . The term “UV filter”, as used in the context of the product Q herein, refers to a chemical compound that blocks or absorbs ultraviolet light and is defined in more detail in paragraph

[7006] of Reference RF1. The term “further cosmetic ingredient”, as used in the context of the product Q herein, comprises any ingredient suitable for making a cosmetic formulation. Several sources disclose cosmetically acceptable ingredients. E. g. the database Cosing on the internet pages of the European Commission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC), discloses cosmetic ingredients. The term “composition and / or formulation thereof’ with reference to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and / or further cosmetic ingredient refers to personal care and / or cosmetic compositions or formulations defined in more detail in paragraph

[7007] of Reference RF1 . The converting step(s) to obtain the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter or further cosmetic ingredient is / are defined in more detail in paragraph

[7008] of Reference RF1.The terms “polymer B”, “polymer composition B”, “coating composition”, “other functional composition”, “foil”, “molded body”, “coating” and “coated substrate” are well known to the personskilled in the art and are defined in more detail from paragraph

[8000] to

[8005] of Reference RF1.The unit bara relates to an absolute pressure and the unit barg relates to a relative pressure, wherein 1 bar equals 105Pa.The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The process of any one of embodiments 1 to 4", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The process of any one of embodiments 1 , 2, 3 and 4". Further, it is explicitly noted that the following set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and, thus, suitably supports, but does not represent the claims of the present invention.1 . A process for treating a stream comprising CO2 and H2, the process comprising(i) preparing a stream comprising CO2 and H2;(ii) treating the stream prepared in (i) with one or more liquid amine-containing streams, obtaining one or more gaseous H2-containing streams and one or more liquid CO2- loaded amine-containing streams; optionally combining the one or more gaseous H2-containing streams if two or more amine-containing streams are applied, obtaining a gaseous H2-containing stream, and optionally combining the one or more liquid CC>2-loaded amine-containing streams if two or more liquid amine-containing streams are applied, obtaining a liquid CC>2-loaded amine-containing stream;(iii) expanding the liquid CC>2-loaded amine-containing stream, obtaining one or more gaseous CC>2-containing streams and a liquid CC>2-reduced amine-containing stream;(iv) optionally dividing the liquid CC>2-reduced amine-containing stream into a first liquid CC>2-reduced amine-containing stream and a second liquid CC>2-reduced amine-containing stream;(v) stripping CO2 from the liquid CC>2-reduced amine-containing stream obtained from (iii) or from the first liquid CC>2-reduced amine-containing stream obtained from (iv), obtaining a liquid CC>2-depleted amine-containing stream and a gaseous CC>2-con- taining stream;(vi) preparing a liquid FhO-containing stream;(vii) transferring heat from the liquid CC>2-depleted amine-containing stream to the liquid FhO-containing stream, obtaining a cooled amine-containing stream and a heated FhO-containing stream;(viii) expanding the heated FhO-containing stream, obtaining a gaseous FhO-containing stream and a liquid FhO-containing stream;(ix) recycling at least a part of the liquid l-hO-containing stream into the l-hO-containing stream prepared in (vi).2. The process of embodiment 1 , wherein the H2 comprised in the stream comprising CO2 and H2 prepared in (i) is obtained from a process for converting NH3 to N2 and H2.3. The process of embodiment 1 or 2, wherein from 7 to 27 volume-%, preferably from 12 to 22 volume-%, more preferably from 15 to 19 volume-%, of the stream comprising CO2 and H2 prepared in (i) consist of CO2.4. The process of any one of embodiments 1 to 3, wherein from 44 to 64 volume-%, preferably from 49 to 59 volume-%, more preferably from 52 to 56 volume-%, of the stream comprising CO2 and H2 prepared in (i) consist of H2.5. The process of any one of embodiments 1 to 4, wherein the stream comprising CO2 and H2 prepared in (i) further comprises CH4, wherein preferably from 0.1 to 5 volume-%, more preferably from 0.5 to 3 volume-%, more preferably from 1 to 2 volume-%, of the stream prepared in (i) consist of CH4.6. The process of any one of embodiments 1 to 5, wherein the stream comprising CO2 and H2 prepared in (i) further comprises CO, wherein preferably from 0.1 to 5 volume-%, more preferably from 0.5 to 3 volume-%, more preferably from 1 to 2 volume-%, of the stream prepared in (i) consist of CO.7. The process of any one of embodiments 1 to 6, wherein the stream comprising CO2 and H2 prepared in (i) further comprises N2, wherein preferably from 17 to 37 volume-%, more preferably from 22 to 32 volume-%, more preferably from 25 to 29 volume-%, of the stream comprising CO2 and H2 prepared in (i) consist of N2.8. The process of any one of embodiments 1 to 7, wherein from 90 to 100 volume-%, preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, of the stream comprising CO2 and H2 prepared in (i) consist of CO2, H2, optionally N2, optionally CH4, and optionally CO.9. The process of any one of embodiments 1 to 8, wherein the stream comprising CO2 and H2 prepared in (i) has a temperature in the range of from 130 to 180 °C, preferably from 138 to 169 °C.10. The process of any one of embodiments 1 to 9, wherein the stream comprising CO2 and H2 prepared in (i) has a pressure in the range of from 15 to 60 bara, preferably from 20 to 40 bara, more preferably from 25 to 33 bara.11 . The process of any one of embodiments 1 to 10, wherein the stream comprising CO2 and H2 prepared in (i) has a volume flow rate in the range of from 10,000 to 500,000 Nm3 / h, preferably from 150,000 to 300,000 Nm3 / h, more preferably from 170,000 to 239,000 Nm3 / h.12. The process of any one of embodiments 1 to 11 , further comprising after (i) and prior to (ii)(1.1 ) cooling of the stream comprising CO2 and H2 prepared in (i); wherein the stream comprising CO2 and H2 is preferably cooled in (i.1 ) to a temperature in the range of from 44 to 64 °C, preferably from 49 to 60 °C.13. The process of embodiment 12, wherein cooling is conducted with a heat exchanger.14. The process of any one of embodiments 1 to 13, further comprising after (i) and prior to (ii), preferably after (i.1 ) and prior to (ii)(1.2) expanding the stream comprising CO2 and H2 prepared in (i) or the stream comprising CO2 and H2 cooled in (i.1 ).15. The process of embodiment 14, wherein the stream comprising CO2 and H2 prepared in (i) or the stream comprising CO2 and H2 cooled in (i.1 ) is expanded in (i.2) in a vessel.16. The process of any one of embodiments 1 to 15, wherein the stream comprising CO2 and H2 obtained from (i), (i.1) or (i.2) is treated in (ii) in one or more columns, preferably in two columns, wherein the one or more columns are more preferably sequentially arranged.17. The process of any one of embodiments 1 to 16, wherein the stream comprising CO2 and H2 obtained from (i), (i.1 ) or (i.2) is treated in (ii) with two or more liquid amine-containing streams AS(n), wherein n = 1 , 2, 3, 418. The process of embodiment 17, wherein the stream comprising CO2 and H2 is treated in (ii) with a first liquid amine-containing stream AS(1) and a second liquid amine-containing stream AS(2), wherein treating the stream comprising CO2 and H2 prepared in (i) or obtained from (i.1 ) or (i.2) in (ii) comprises(11.1 ) treating the stream comprising CO2 and H2 prepared in (i) or obtained from (i.1) or (i.2) with a first liquid amine-containing stream AS(1), obtaining a H2-containing stream and a first liquid CC>2-loaded amine-containing stream;(11.2) treating the H2-containing stream obtained from (ii.1 ) with a second liquid amine- containing stream AS(2), obtaining a H2-containing stream and a second liquid CO2- loaded amine-containing stream;(11.3) combining the first liquid CC>2-loaded amine-containing stream obtained from (ii.1 ) and the second liquid CC>2-loaded amine-containing stream obtained from (ii.2), obtaining the liquid CC>2-loaded amine-containing stream.19. The process of embodiment 18, wherein the first liquid amine-containing stream AS(1 ) has a temperature in the range of from 60 to 95 °C, preferably from 70 to 90 °C, more preferably from 75 to 86 °C.20. The process of embodiment 18 or 19, wherein the second liquid amine-containing stream AS(2) has a temperature in the range of from 30 to 80 °C, preferably from 45 to 65 °C.21 . The process of any one of embodiments 18 to 20, wherein the stream comprising CO2and H2prepared in (i) or obtained from (i.1) or (i.2) is treated in (ii) with the first liquid amine-containing stream AS(1) in counter current flow.22. The process of any one of embodiments 18 to 21 , wherein the stream comprising CO2and H2prepared in (i) or obtained from (i.1) or (i.2) is treated in (ii) with the first liquid amine-containing stream AS(1) in a column.23. The process of embodiment 22, wherein the H2-containing stream obtained in (ii) is removed from the top of the column.24. The process of any one of embodiments 18 to 23, wherein the H2-containing stream obtained in (ii.1) is treated in (ii.2) with the second liquid amine-containing stream AS(2) in counter current flow.25. The process of any one of embodiments 18 to 24, wherein the H2-containing stream obtained in (ii.1) is treated in (ii.2) with the second liquid amine-containing stream AS(2) in a column.26. The process of embodiment 25, wherein the H2-containing stream obtained in (ii.2) is removed from the top of the column.27. The process of any one of embodiments 1 to 26, wherein the amine contained in the one or more liquid amine-containing streams independently from one another is a primary amine wherein the amine nitrogen is bonded to a tertiary carbon atom, a secondary amine wherein the amine nitrogen is bonded to at least one secondary carbon atom or at least one tertiary carbon atom, or a tertiary amine.28. The process of any one of embodiments 1 to 27, wherein the amine contained in the one or more liquid amine-containing streams independently from one another comprises one or more of an amine having formula I:NR1(R2)2(I),wherein R1is selected from C2-C6-hydroxyalkyl groups, Ci-C6-alkoxy-C2-C6-alkyl groups, hydroxy-Ci-C6-alkoxy-C2-C6-alkyl groups and 1-piperazinyl-C2-C6-alkyl groups, and R2is independently from one another selected from H, Ci-Ce-alkyl groups and C2-Ce-hydroxy- alkyl groups; an amine having formula II:R3R4N-X-NR5R6(II), wherein R3, R4, R5and R6are independently from one another selected from H, Ci-Ce-al- kyl groups, C2-Ce-hydroxyalkyl groups, Ci-C6-alkoxy-C2-Ce-alkyl groups and C2-Ce-amino- alkyl groups, and X is a C2-Ce-alkylene group, -X1-NR7-X2- or -X1-O-X2-, wherein X1and X2are independently from one another C2-Ce-alkylene groups and R7is H, a Ci-Ce-alkyl group, C2-Ce-hydroxyalkyl group or C2-Ce-aminoalkyl group; and5- to 7-membered saturated heterocycles which have at least one nitrogen atom in the ring and may comprise one or two further heteroatoms selected from nitrogen and oxygen in the ring. The process of any one of embodiments 1 to 28, wherein the amine contained in the one or more liquid amine-containing streams independently from one another comprises one or more of 2-aminoethanol (monoethanolamine), 2-(methylamino)ethanol, 2-(ethyla- mino)ethanol, 2-(n-butylamino)ethanol, 2-amino-2-methylpropanol, N-(2-aminoethyl)piper- azine, methyldiethanolamine, ethyldiethanolamine, dimethylaminopropanol, t-butylami- noethoxyethanol (TBAEE), 2-amino-2-methylpropanol, diisopropanolamine (DIPA), 3-me- thylaminopropylamine, ethylenediamine, diethylenetriamine, triethylenetetramine, 2,2-di- methyl-1 ,3-diaminopropane, hexamethylenediamine, 1 ,4-diaminobutane, 3,3-iminobis- propylamine, tris(2-aminoethyl)amine, bis(3-dimethylaminopropyl)amine, tetramethylhexamethylenediamine, piperazine, 2-methylpiperazine, N-methylpiperazine, 1-hydroxyethylpi- perazine, 1 ,4-bishydroxyethylpiperazine, 4-hydroxyethylpiperidine, homopiperazine, piperidine, 2-hydroxyethylpiperidine, triethylenediamine (TEDA), and morpholine. The process of any one of embodiments 1 to 29, wherein the amine contained in the one or more liquid amine-containing streams independently from one another comprises one or more of monoethanolamine (MEA), methylaminopropylamine (MAPA), piperazine (PIP), diethanolamine (DEA), triethanolamine (TEA), diethylethanolamine (DEEA), diisopropanolamine (DIPA), aminoethoxyethanol (AEE), tert-butylaminoethoxyethanol (TBAEE), dimethylaminopropanol (DIMAP), methyldiethanolamine (MDEA), triethylenediamine (TEDA), tert-butylaminopropanediol, tert-butylaminoethoxyethylmorpholine, tert-butylaminoethyl- morpholine, methoxyethoxyethoxyethyl-tertbutylamine, and tert-butylaminoethylpyrroli- done, preferably one or more of tert-butylaminoethoxyethanol (TBAEE), methyldiethanolamine (MDEA), and triethylenediamine (TEDA), more preferably triethylenediamine (TEDA).31 . The process of any one of embodiments 1 to 30, wherein the one or more liquid amine- containing streams independently from one another further comprises one or more alkanolamines, polyamines, 5-, 6- or 7-membered saturated heterocycles having at least one NH group in the ring, which may comprise one or two further heteroatoms selected from nitrogen and oxygen in the ring, wherein the alkanolamines are preferably selected from the group consisting of monoethanolamine (MEA), diethanolamine (DEA), ethylaminoethanol, 1-amino-2-methyl-propan-2- ol, 2-amino-1 -butanol, 2-(2-aminoethoxy)ethanol, 2-(2-aminoethoxy)ethanamine, and mixtures of two or more thereof, wherein the polyamines are preferably selected from the group consisting of hexamethylenediamine, 1 ,4-diaminobutane, 1 ,3-diaminopropane, 3-(methylamino)propylamine (MAPA), N-(2-hydroxyethyl)ethylenediamine, 3-(dimethylamino)propylamine (DMAPA), 3- (diethylamino)propylamine, N,N'-bis(2-hydroxyethyl)ethylenediamine, and mixtures of two or more thereof, wherein the 5-, 6- or 7-membered saturated heterocycles having at least one NH group in the ring, which may comprise one or two further heteroatoms selected from nitrogen and oxygen in the ring are preferably selected from the group consisting of piperazine, 2- methylpiperazine, N-methylpiperazine, N-ethylpiperazine, N-(2-hydroxyethyl)piperazine, N-(2-aminoethyl)piperazine, homopiperazine, piperidine, morpholine, and mixtures of two or more thereof, more preferably piperazine.32. The process of any one of embodiments 1 to 31 , wherein treating in one or more of (ii), (ii.1 ), and (ii.2) is conducted independently from one another at a pressure in the range of from 10 to 60 bara, preferably 22 to 42 bara, more preferably from 27 to 37 bara, more preferably from 30 to 34 bara.33. The process of any one of embodiments 1 to 32, wherein from 0 to 1 .5 volume-%, preferably from 0.00001 to 1.1 volume-%, more preferably from 0.0001 to 1.0 volume-%, of the liquid CC>2-loaded amine-containing stream obtained in (ii) consists of CO2.34. The process of any one of embodiments 1 to 33, wherein the liquid CC>2-loaded amine- containing stream obtained in (ii) has a temperature in the range of from 70 to 110 °C, preferably from 80 to 100 °C, more preferably from 85 to 95 °C.35. The process of any one of embodiments 1 to 34, wherein the liquid CC>2-loaded amine- containing stream obtained in (ii) has a volume flow rate in the range of from 100 to 5000 m3 / h, preferably from 2000 to 3000 m3 / h, more preferably from 2300 to 2500 m3 / h.36. The process of any one of embodiments 1 to 35, wherein expanding the liquid CC>2-loaded amine-containing stream in (iii) is performed in one or more steps each comprising expanding the liquid CC>2-loaded amine-containing stream, preferably in two or more steps,more preferably in two or more sequential steps, obtaining one or more gaseous CC>2-con- taining streams and the liquid CC>2-reduced amine-containing stream.37. The process of any one of embodiments 1 to 36, wherein expanding the liquid CC>2-loaded amine-containing stream in (iii) comprises(111.1 ) expanding the liquid CC>2-loaded amine-containing stream, wherein the liquid CO2- loaded amine-containing stream is preferably expanded in a first vessel, wherein the liquid CC>2-loaded amine-containing stream is preferably introduced in the first vessel at the top of the first vessel for expanding, obtaining a gaseous CC>2-containing stream and a liquid CC>2-reduced amine-containing sub-stream;(111.2) expanding the liquid CC>2-reduced amine-containing sub-stream, wherein the liquid CC>2-reduced amine-containing sub-stream obtained in (iii.1 ) is preferably expanded in a second vessel, obtaining a gaseous CC>2-containing stream and the liquid CO2- reduced amine-containing stream.38. The process of any one of embodiments 1 to 37, wherein the liquid CC>2-reduced amine- containing stream obtained from (iii) has a temperature in the range of from 65 to 90 °C, preferably from 73 to 83 °C, more preferably from 76 to 80 °C.39. The process of any one of embodiments 1 to 38, wherein the liquid CC>2-reduced amine- containing stream obtained in (iii) comprises from 15 to 35 Nm3CO2 per m3of the liquid CC>2-reduced amine-containing stream, preferably from 20 to 29 Nm3CO2 per m3of the liquid CC>2-reduced amine-containing stream, more preferably from 23 to 26 Nm3CO2 per m3of the liquid CC>2-reduced amine-containing stream.40. The process of any one of embodiments 1 to 39, further comprising after (iii) and prior to (iv)(iii’) merging the one or more gaseous CC>2-containing streams obtained from (iii), obtaining a gaseous CC>2-containing stream;(iii”) expanding the gaseous CC>2-containing stream obtained from (iii’), wherein the gaseous CC>2-containing stream is preferably expanded in a vessel.41 . The process of any one of embodiments 1 to 40, comprising dividing the liquid CC>2-re- duced amine-containing stream into a first liquid CC>2-reduced amine-containing stream and a second liquid CC>2-reduced amine-containing stream according to (iv).42. The process of any one of embodiments 1 to 41 , wherein the first liquid CC>2-reduced amine-containing stream comprises from 5 to 25 weight-%, preferably from 10 to 21 weight-%, more preferably from 13 to 18 weight-%, of the liquid CC>2-reduced amine-containing stream.43. The process of any one of embodiments 1 to 42, wherein the second liquid CC>2-reduced amine-containing stream comprises from 75 to 95 weight-%, preferably from 79 to 90weight-%, more preferably from 82 to 87 weight-%, of the liquid CC>2-reduced amine-con- taining stream.44. The process of any one of embodiments 1 to 43, further comprising after (iv) and prior to (v)(iv’) recycling the second liquid CC>2-reduced amine-containing stream obtained in (iv) into one or more of the one or more liquid amine-containing streams in (ii), preferably into the first liquid amine-containing stream AS(1) according to (ii.1 ).45. The process of embodiment 44, wherein the second liquid amine-containing stream obtained in (iv) recycled according to (iv’) has a temperature in the range of from 68 to 98 °C, preferably from 78 to 88 °C, more preferably from 81 to 85 °C.46. The process of embodiment 44 or 45, wherein the second liquid amine-containing stream obtained in (iv) recycled according to (iv’) has a volume flow rate in the range of from 100 to 5000 m3 / h, preferably from 1500 to 2500 m3 / h, more preferably from 1900 to 2100 m3 / h.47. The process of any one of embodiments 1 to 46, further comprising after (iii) and prior to (v), preferably after (iv) and prior to (v)(iv”) heating the liquid CC>2-reduced amine-containing stream obtained from (iii) or the first liquid CC>2-reduced amine-containing stream obtained from (iv).48. The process of embodiment 47, wherein the liquid CC>2-reduced amine-containing stream obtained from (iii) or the first liquid CC>2-reduced amine-containing stream obtained from (iv) is heated in (iv”) to a temperature in the range of from 85 to 115 °C, preferably from 95 to 105 °C, more preferably from 98 to 102 °C.49. The process of embodiment 47 or 48, wherein in (iv”) heating the liquid CC>2-reduced amine-containing stream obtained from (iii) or the first liquid CC>2-reduced amine-containing stream obtained from (iv) is conducted with a heat exchanger, preferably with a cross heat exchanger.50. The process of any one of embodiments 1 to 49, wherein stripping is conducted by heating the liquid CC>2-reduced amine-containing stream obtained from (iii) or the first CC>2-re- duced amine-containing stream obtained from (iv) to a temperature in the range of from 85 to 130 °C, preferably from 95 to 120 °C, more preferably from 100 to 114 °C.51 . The process of any one of embodiments 1 to 50, wherein stripping is conducted in a column.52. The process of any one of embodiments 1 to 51 , wherein the liquid CC>2-depleted amine- containing stream obtained from (v) has a temperature in the range of from 97 to 127 °C, preferably from 107 to 117 °C, more preferably from 110 to 114 °C.The process of any one of embodiments 1 to 52, wherein the liquid CC>2-depleted amine- containing stream obtained in (v) comprises from 0.01 to 0.40 Nm3CO2 per m3of the liquid CC>2-depleted amine-containing stream, preferably from 0.05 to 0.35 Nm3CO2 per m3of the liquid CC>2-depleted amine-containing stream, more preferably from 0.10 to 0.30 Nm3CO2 per m3of the liquid CC>2-depleted amine-containing stream. The process of any one of embodiments 1 to 53, wherein the gaseous CC>2-containing stream obtained from (v) has a temperature in the range of from 87 to 117 °C, preferably from 97 to 107 °C, more preferably from 100 to 104 °C. The process of any one of embodiments 1 to 54, wherein the gaseous CC>2-containing stream obtained from (v) has a pressure in the range of from 0.10 to 0.60 bara, preferably 0.20 to 0.50 bara, more preferably from 0.30 to 0.40 bara. The process of any one of embodiments 1 to 55, wherein the gaseous CC>2-containing stream obtained from (v) is recycled into the one or more columns according to embodiment 16, wherein the gaseous CC>2-containing stream obtained in (v) is preferably treated in (ii.2) with the second amine-containing stream AS(2) as defined in embodiment 18. The process of any one of embodiments 1 to 56, further comprising after (v) and prior to (vii)(v’) cooling of the liquid CC>2-depleted amine-containing stream obtained from (v); wherein the liquid CC>2-depleted amine-containing stream is preferably cooled in (v’) to a temperature in the range of from 75 to 105 °C, preferably from 85 to 95 °C, more preferably from 88 to 92 °C. The process of embodiment 57, wherein cooling is conducted with a heat exchanger, preferably with a cross heat exchanger, more preferably with the cross heat exchanger as defined in embodiment 49. The process of any one of embodiments 1 to 58, further comprising after (v) and prior to (vii), preferably after (v’) and prior to (vii)(v”) compressing the liquid CC>2-depleted amine-containing stream obtained from (v) or (v’). The process of embodiment 59, wherein the liquid CC>2-depleted amine-containing stream is compressed in (v”) to a pressure in the range of from 0.20 to 0.60 barg, preferably from 0.30 to 0.50 barg, more preferably from 0.35 to 0.45 barg. The process of embodiment 59 or 60, wherein the liquid CC>2-depleted amine-containing stream obtained from (v”) has a temperature in the range of from 75 to 105 °C, preferably from 85 to 95 °C, more preferably from 88 to 92 °C.62. The process of any one of embodiments 1 to 61 , wherein the liquid l-hO-containing stream prepared in (vi) has a temperature in the range of from 15 to 105 °C, preferably from 20 to 105 °C.63. The process of any one of embodiments 1 to 62, wherein the liquid l-hO-containing stream prepared in (vi) has a pressure in the range of from 0.1 to 1.5 bara, preferably from 0.5 to1 .5 bara, more preferably from 1 .0 to 1 .5 bara.64. The process of any one of embodiments 1 to 63, wherein the liquid l-hO-containing stream comprises, preferably consists of, de-ionized water.65. The process of any one of embodiments 1 to 64, wherein the liquid l-hO-containing stream comprises from 0 to 0.1 Nm3per m3of the liquid CC>2-depleted amine-containing stream, preferably from 0.01 Nm3per m3of the liquid CC>2-depleted amine-containing stream, more preferably 0 to 0.001 Nm3per m3of the liquid CC>2-depleted amine-containing stream, of one or more of CO2 or N2, preferably of CO2 and N2, wherein the liquid H2O- containing stream is preferably substantially free of one or more of CO2 or N2, more preferably of CO2 and N2.66. The process of any one of embodiments 1 to 65, wherein heat is transferred in (vii) with a heat exchanger, preferably a liquid-to-liquid heat exchanger.67. The process of any one of embodiments 1 to 65, wherein heat is transferred in (vii) with a heat pump, preferably a closed-loop heat pump, wherein the heat pump more preferably comprises a refrigerant selected from groups R717, R1233, preferably R1233ZDE, R1336, preferably R1336MZZE, R600, preferably R600a, and mixtures of two or more thereof.68. The process of any one of embodiments 1 to 67, wherein the heated l-hO-containing stream obtained from (vii) comprises a liquid phase, a gaseous phase or a liquid and a gaseous phase, wherein the gaseous phase more preferably comprises steam.69. The process of any one of embodiments 1 to 68, wherein the heated l-hO-containing stream obtained from (vii) has a pressure in the range of from 0.02 to 0.71 bara, preferably from 0.41 to 0.61 bara, more preferably from 0.45 to 0.56 bara.70. The process of any one of embodiments 1 to 69, wherein the cooled amine-containing stream obtained from (vii) has a temperature in the range of from 55 to 85 °C, preferably from 65 to 75 °C, more preferably from 68 to 72 °C.71 . The process of any one of embodiments 1 to 70, wherein the cooled amine-containing stream obtained from (vii) is recycled into one or more of the one or more liquid amine-containing streams in (ii), preferably into the second liquid amine-containing stream AS(2) according to (ii.2).72. The process of any one of embodiments 1 to 71 , the process further comprising after (viii) (viii’) compressing the gaseous ^©-containing stream obtained from (viii), wherein the gaseous ^©-containing stream obtained from (viii) is preferably compressed to a pressure in the range of from 2 to 100 bara, preferably in the range of from 3 to 50 bara, more preferably in the range of from 3 to 25 bara, more preferably in the range of from 4 to 7 bara, wherein compressing is conducted in one or more compression stages, preferably in 2 to 4 compression stages, more preferably in 3 compression stages, wherein the one or more compression stages are preferably conducted sequentially.73. A process, preferably according to any one of embodiments 1 to 72, comprising the step of converting the gaseous H2-containing stream and / or the gaseous C©2-containing stream obtainable by or obtained by the process according to any one of embodiments 1 to 72 to obtain a product Q.The present invention is further illustrated by the following examples, comparative examples and reference examples.EXPERIMENTAL SECTIONExample 1 and Comparative Example 2: Process for treating a stream comprising CO2 and H2A gas stream containing about 17 mol-% CO2, about 54 mol-% H2 and about 27 mol-% N2 obtained from an ammonia conversion process was cooled to approximately 54 °C. Then, the stream was flashed in a pre-vessel and then given to the bottom of an absorption column. Here the gas was treated with a semi-lean amine solution at ca. 32 bara in counter current flow. Gas left the pre-treatment column and entered the fine treatment column at the bottom, wherein the fine treatment column was directly on top of the pre-treatment column. In the fine treatment column, the gas was treated with lean amine solution in order to reduce CO2 content to about 1 ppmmol up to 1 mol-%. After passing a further flash vessel the treated CO2-free gas was given to downstream processes. The loaded amine solution leaving the pre-treatment column at the bottom was given to a high pressure flash vessel at the top. From the bottom of the high pressure flash vessel the resulting solution was given to the top of a low pressure flash vessel (pressure about 1 .3 bara). Released CO2 left the low pressure flash vessel at the top, was cooled down to roughly 39 °C and then given to the CO2 product stream.The semi-lean amine solution was partly sent to the top of the pre-treatment column and partly to a stripping column where the remaining CO2 was stripped out using an evaporator at the bottom of the stripping column. Before the semi-lean solution enters the stripping column, it is prewarmed in a cross heat exchanger using the heat of the lean amine solution obtained from the stripper bottom.In Comparative Example 2, the lean amine solution was then pressurized and cooled down in an air cooler from about 90 °C to 54°C before it entered the fine treatment column at the top.In Example 1 , heat was transferred from the lean amine solution to a l-hO-containing stream using a heat exchanger. Thereby, a heated l-hO-containing stream was obtained. The cooled lean amine solution was recycled to the fine treatment column, where it entered at the top of said column.In comparison with Comparative Example 2, it was possible with the process of Example 1 to generate about 13.8 t / h of steam.Cited literature:- US 3823222 A- US 3101996 A- WO 2007 / 12143 A1- WO 2010 / 097047 A1- WO 2011 / 122525 A1- JP 2015131735 A- WO 2007 / 81214 A1- CN 114405258 A- WO 2012 / 58558 A2- J P 2010 / 088982 A- J P 2015 / 131736 A- FR 2968574 A1- US 4702898 A- CN 103214009 B- US 4160810 A- US 4591370 A

Claims

Claims1 . A process for treating a stream comprising CO2 and H2, the process comprising(i) preparing a stream comprising CO2 and H2;(ii) treating the stream prepared in (i) with one or more liquid amine-containing streams, obtaining one or more gaseous H2-containing streams and one or more liquid CO2- loaded amine-containing streams; optionally combining the one or more gaseous H2-containing streams if two or more amine-containing streams are applied, obtaining a gaseous H2-containing stream, and combining the one or more liquid CO2- loaded amine-containing streams if two or more liquid amine-containing streams are applied, obtaining a liquid CC>2-loaded amine-containing stream;(iii) expanding the liquid CC>2-loaded amine-containing stream, obtaining one or more gaseous CC>2-containing streams and a liquid CC>2-reduced amine-containing stream;(iv) optionally dividing the liquid CC>2-reduced amine-containing stream into a first liquid CC>2-reduced amine-containing stream and a second liquid CC>2-reduced amine-containing stream;(v) stripping CO2 from the liquid CC>2-reduced amine-containing stream obtained from (iii) or from the first liquid CC>2-reduced amine-containing stream obtained from (iv), obtaining a liquid CC>2-depleted amine-containing stream and a gaseous CC>2-con- taining stream;(vi) preparing a liquid l-hO-containing stream;(vii) transferring heat from the liquid CC>2-depleted amine-containing stream to the liquid l-hO-containing stream, obtaining a cooled amine-containing stream and a heated l-hO-containing stream;(viii) expanding the heated l-hO-containing stream, obtaining a gaseous l-hO-containing stream and a liquid l-hO-containing stream;(ix) recycling at least a part of the liquid l-hO-containing stream into the l-hO-containing stream prepared in (vi).

2. The process of claim 1 , wherein the stream comprising CO2 and H2 prepared in (i) has a pressure in the range of from 15 to 60 bara.

3. The process of claim 1 or 2, wherein the stream comprising CO2 and H2 obtained from (i) is treated in (ii) in one or more columns.

4. The process of any one of claims 1 to 3, wherein the stream comprising CO2 and H2 obtained from (i) is treated in (ii) with two or more liquid amine-containing streams AS(n), wherein n = 1 , 2, 3, 45. The process of claim 4, wherein the stream comprising CO2 and H2 is treated in (ii) with a first liquid amine-containing stream AS(1) and a second liquid amine-containing stream AS(2), wherein treating the stream comprising CO2 and H2 prepared in (i) in (ii) comprises(11.1 ) treating the stream comprising CO2 and H2 prepared in (i) with a first liquid amine- containing stream AS(1 ), obtaining a H2-containing stream and a first liquid CO2- loaded amine-containing stream;(11.2) treating the H2-containing stream obtained from (ii.1 ) with a second liquid amine- containing stream AS(2), obtaining a H2-containing stream and a second liquid CO2- loaded amine-containing stream;(11.3) combining the first liquid CC>2-loaded amine-containing stream obtained from (ii.1 ) and the second liquid CC>2-loaded amine-containing stream obtained from (ii.2), obtaining the liquid CC>2-loaded amine-containing stream.

6. The process of any one of claims 1 to 5, wherein the amine contained in the one or more liquid amine-containing streams independently from one another is a primary amine wherein the amine nitrogen is bonded to a tertiary carbon atom, a secondary amine wherein the amine nitrogen is bonded to at least one secondary carbon atom or at least one tertiary carbon atom, or a tertiary amine.

7. The process of any one of claims 1 to 6, further comprising after (iv) and prior to (v) (iv’) recycling the second liquid CC>2-reduced amine-containing stream obtained in (iv) into one or more of the one or more liquid amine-containing streams in (ii).

8. The process of any one of claims 1 to 7, wherein stripping is conducted by heating the liquid CC>2-reduced amine-containing stream obtained from (iii) or the first CC>2-reduced amine-containing stream obtained from (iv) to a temperature in the range of from 85 to 130 °C.

9. The process of any one of claims 1 to 8, wherein the liquid CC>2-depleted amine-containing stream obtained from (v) has a temperature in the range of from 97 to 127 °C.

10. The process of any one of claims 1 to 9, further comprising after (v) and prior to (vii) (v”) compressing the liquid CC>2-depleted amine-containing stream obtained from (v) or(v’).11 . The process of claim 10, wherein the liquid CC>2-depleted amine-containing stream is compressed in (v”) to a pressure in the range of from 0.20 to 0.60 barg.

12. The process of any one of claims 1 to 11 , wherein the heated l-hO-containing stream obtained from (vii) has a pressure in the range of from 0.02 to 0.71 bara.

13. The process of any one of claims 1 to 12, wherein the cooled amine-containing stream obtained from (vii) has a temperature in the range of from 55 to 85 °C.

14. The process of any one of claims 1 to 13, wherein the cooled amine-containing stream obtained from (vii) is recycled into one or more of the one or more liquid amine-containing streams in (ii).

15. A process comprising the step of converting the gaseous H2-containing stream and / or the gaseous CC>2-containing stream obtainable by or obtained by the process according to any one of claims 1 to 14 to obtain a product Q.