Method for selective removal of hydrogen sulphide and CO
With the help of a method of selective removal of hydrogen sulphides, organic sulphur components and CO 2 from crude gases, by using a first and second absorption stage ( 41 or 49 ) for separating almost pure CO 2 , a solution has to be found, with which, among other things, hydrogen sulphides and organic sulphur compounds can be removed in as selective a manner as possible. This is achieved as follows: the absorption agent coming out of the first absorption stage ( 41 ) and enriched with hydrogen sulphide and CO 2 a.o., is pre-heated to an increased pressure with the hot-regenerated solution ( 12 ) coming from the desorption stage ( 50 ) in a heat exchanger ( 44 ), and then at the selected higher pressure de-stressed in a high pressure flash container ( 47 ), whereby the gas flow released at the increased pressure is cooled in a condenser ( 48 ) and then guided to the second absorption stage ( 49 ), in which the sulphur components are completely removed with the help of a part-flow of the regenerated absorption agent ( 15, 16, 17 ) coming from the desorption stage ( 50 ), whereby the absorption agent is guided back ( 26/27 ) from the second absorption stage ( 49 ) into the desorption stage ( 50 ).
1. Method for selective removal of hydrogen sulphides, organic sulphur components and CO 2 from crude gases, by using a first absorption stage ( 41 ) and a second absorption stage ( 49 ) for separating almost pure CO 2 and using a desorption stage ( 50 ) for extracting a gas rich in hydrogen sulphide, whereby the regenerated absorbing substance from the desorption stage ( 50 ) is again guided back to both the absorption stages ( 41 , 49 ), whereby as absorbing substance one uses a chemically non-active solvent, wherein the absorption agent enriched with hydrogen sulphide, organic sulphur compounds and CO 2 and coming out of the first absorption stage ( 41 ), finds itself at an increased pressure between the pressure of the absorption column ( 41 ) and the pressure of the desorption column ( 50 ), and is pre-heated with the hot-regenerated solution ( 12 ) coming from the desorption stage ( 50 ) in a heat exchanger ( 44 ), and is then de-stressed at a selected pressure greater than the increased pressure in a high pressure flash container ( 47 ), whereby the gas flow released at the increased temperature is cooled in a condenser ( 48 ) and then guided to the second absorption stage ( 40 ), in which the sulphur components are completely removed with the help of (already mentioned) the part-flow the regenerated absorption agent ( 15 , 16 , 17 ) coming from the desorption stage ( 50 ), whereby the absorption agent is guided back ( 26 / 27 ) out of the second absorption stage ( 49 ) into the desorption stage ( 50 );
wherein the enriched absorption solution leaving the high pressure flash container ( 47 ) is de-stressed in a low pressure ( 56 ), whereby the flash gas along with the flash gas coming out of the flash stage ( 55 ) is guided to the second absorption column ( 45 ) with the help of a common compressor ( 58 ), and whereby the absorption solution leaving the low pressure flash ( 56 ) is guided on to the head of the desorption column.
2. Method as per claim 1 , wherein the charged absorption substance ( 18 ) is heated after the second absorption stage ( 49 ) and before entering into the desorption stage, whereby the heating takes place in indirect heat exchange ( 52 ) with the absorption substance flow ( 15 ) coming from the desorption stage.
3. Method as per claim 1 , wherein the absorption takes place at an operating pressure of 10 to 150 bar.
4. Method as per claim 1 , wherein the temperature of the enriched absorption agent coming from the absorber is increased to 50 to 200° C.
5. Method for selective removal of hydrogen sulphides, organic sulphur components and CO 2 from crude gases, by using a first absorption stage ( 41 ) and a second absorption stage ( 49 ) for separating almost pure CO 2 and using a desorption stage ( 50 ) for extracting a gas rich in hydrogen sulphide, whereby the regenerated absorbing substance from the desorption stage ( 50 ) is again guided back to both the absorption stages ( 41 , 49 ), whereby as absorbing substance one uses a chemically non-active solvent, wherein the absorption agent enriched with hydrogen sulphide, organic sulphur compounds and CO 2 and coming out of the first absorption stage ( 41 ), finds itself at an increased pressure between the pressure of the absorption column ( 41 ) and the pressure of the desorption column ( 50 ), and is pre-heated with the hot-regenerated solution ( 12 ) coming from the desorption stage ( 50 ) in a heat exchanger ( 44 ), and is then de-stressed at a selected pressure greater than the increased pressure in a high pressure flash container ( 47 ), whereby the gas flow released at the increased temperature is cooled in a condenser ( 48 ) and then guided to the second absorption stage ( 49 ), in which the sulphur components are completely removed with the help of (already mentioned) the part-flow the regenerated absorption agent ( 15 , 16 , 17 ) coming from the desorption stage ( 50 ), whereby the absorption agent is guided back ( 26 / 27 ) out of the second absorption stage ( 49 ) into the desorption stage ( 50 );
wherein directly downstream of the second absorption stage ( 49 ) a flash stage ( 55 ) is arranged, in which the absorbing substance ( 18 ) coming out from the absorption stage ( 49 ) is de-stressed and the released gas, which mainly contains hydrogen sulphide, H 2 S and carbon dioxide, CO 2 is guided back into the second absorption stage ( 49 ).
6. Method as per claim 1 , wherein after the second absorption stage ( 49 ) a flash stage ( 55 ) is foreseen, in which the charged absorbing substance is released out of the second absorption stage and the thus released flash gas ( 19 ) which primarily contains CO 2 and portions of H 2 S, is led into a pipeline at least indirectly leading to the leading absorption substance stage, and the absorbing substance ( 26 ) is guided into the desorption stage.