Patent Grant
7189282
This invention relates to a process of cleaning gas, in particular hydrocarbonaceous gas such as e.g. natural gas, which is contaminated with sulfur in the form of H2S and mercaptan as well as CO2.
The document WO 97/26069 describes a process of cleaning carbon dioxide and sulfur-containing gases, in which there are sulfur-contaminated impurities in the form of mercaptans and H2S. In a first absorption, the sulfur-contaminated impurities are removed from the gas, in order to produce a clean gas stream and a sour gas stream, the sour gas being hydrogenated in order to convert a major amount of mercaptans to H2S. The hydrogenated sour gas is introduced into a second absorption/regeneration plant, in which the sour gas is separated into a first gas stream rich in H2S, which is introduced into a Claus plant, and a second gas stream containing little H2S, which is supplied to the postcombustion. The Claus plant is followed by a tail gas aftertreatment, in wich the H2S is reduced further and a gas rich in H2S is withdrawn.
What is disadvantageous in this process is the too small amount of sulfur and mercaptans which can be removed from the gas. In accordance with the prior art, it is only possible with a large effort to remove the sulfur from the crude gas for more than 95 wt-%.
It is the object underlying the invention to create an improved process for cleaning hydrocarbonaceous gas, in which the undesired sulfur-containing substances in the form of H2S and mercaptan are removed.
In accordance with the invention, this object is solved in that crude gas is introduced into an absorption and regeneration column and washed therein, three gas streams being withdrawn from this absorption and regeneration column, a first exhaust gas stream being introduced into a Claus plant, a second sour gas stream with a low H2S concentration of 10–30 vol-% being introduced into another absorption plant, and a third gas stream, the valuable gas with the mercaptans, being cooled and supplied to an adsorption plant, that from this adsorption plant a sweet gas is withdrawn and a gas stream containing mercaptan is subjected to washing. As washing stage, there is preferably used a physical washing stage, e.g. a Purisol plant, with which a small amount of gas with a high concentration of mercaptan is introduced into the Claus plant and part of the coadsorbed valuable gas from the regeneration of the adsorption plant is recovered as fuel gas. In the Claus plant, the mercaptan gas is burnt completely.
Due to the fact that before being introduced into the Claus plant, the second sour gas stream is first fortified in an absorption and the solution is regenerated in a fortification washing stage, the Claus plant can be designed smaller, as the sour gas stream has a higher concentration of H2S. The processing of concentrated H2S-containing gas and the mercaptan stream in the Claus plant as well as the processing of the gas stream from the first absorption and of the Claus exhaust gas in a tail gas washing stage increases the degree of sulfur recovery of the entire plant.
To achieve that the absorption plant for the sour gas to be fortified consumes less lye and only one regeneration column is required, the H2S-containing solution is withdrawn from the absorption plant, which is disposed behind the hydrogenation of the residual Claus gas, and introduced into the absorption plant for fortifying the sour gas.
The degree of sulfur recovery is increased in that the gas from the absorption of the fortification is introduced into the hydrogenation, in order to convert sulfur components into H2S, and subsequently into the absorption of the tail gas aftertreatment.
The drawing depicts a block diagram of the process.
Embodiments of the process will be explained by way of example with reference to the drawing.
Through line (1), crude gas is introduced into a first washing stage comprising an absorption and regeneration column (2) and washed therein. A first exhaust gas stream (5) from the regeneration is directly introduced into a Claus plant (14). This exhaust gas stream (5) chiefly consists of up to 80 vol-% hydrocarbon and up to 20 vol-% CO2 with small amounts of mercaptans (up to 0.3 vol-%) and H2S (up to 5 vol-%).
A second sour gas stream (4) with a low H2S concentration of up to 30 vol-% H2S is introduced into another absorption plant (15) and fortified there with a non-loaded solvent from lines (26) and (27). From the absorption plant (15), the solvent (16) loaded with H2S is introduced into a regeneration plant (17). The gas (up to 97 vol-% CO2 and 0.2 vol-% mercaptan) from the absorption plant (15) is supplied to a hydrogenation (22) via line (18).
From the regeneration (17), sour gas with a high H2S concentration of up to 60 vol-% H2S is introduced into the Claus plant (14) via line (19).
From the absorption and regeneration column (2) a third gas stream (3), the valuable gas with the largest content of mercaptans, is withdrawn, cooled (6) and supplied to an adsorption (8) via line (7). From this adsorption (8), the valuable gas is supplied to further processes, e.g. a liquefaction, via line (9). The mercaptan-containing gas stream (10) is subjected to a physical washing stage, from which the coadsorbed valuable gas is recovered as fuel gas via line (12), and the highly concentrated mercaptan gas is supplied to the Claus plant (14) via line (13). The mercaptan stream is recovered in the regeneration of the Purisol solvent. The amount is small, but with a very high mercaptan concentration of 10 vol-% to 60 vol-%. As an alternative to the Purisol plant (11), another physical or physical-chemical washing stage is possible. However, the same have the disadvantage that too much CH4 is absorbed. In the Claus plant (14), the mercaptan is burnt completely. The SO2 obtained therefrom is reacted with the H2S from the sour gas of line (19) to form sulfur. The liquid sulfur obtained is withdrawn via line (21) and supplied to a further use. Thus, a high degree of sulfur recovery is achieved. The Claus plant (14) is a plant known per se, which consists of a combustion furnace as well as a plurality of catalytic reactors for performing the reaction. In the Claus plant (14), there is always obtained a so-called residual Claus gas, which apart from non-condensed elementary sulfur contains unreacted sulfur dioxide and H2S. This residual gas is withdrawn via line (20) and subjected to an aftertreatment, in order to increase the degree of sulfur recovery. Via line (20), the residual Claus gas is supplied to a hydrogenation plant (22), which is also supplied with the gas from the absorption plant (15) via line (18). In the hydrogenation, SO2 is converted to H2S and supplied to an absorption plant (24) via line (23). From the absorption plant (24), a solution is introduced into the fortification absorption (15) via line (26) for the further absorption of H2S. The remaining H2S-containing gas is withdrawn from the absorption plant (24) via line (25) and supplied to a combustion.
The following Table shows an analysis of the gas streams in the individual lines. The liquid process streams in lines (16), (26), (27) and (28) are not shown.
Corresponding to the values represented in the Table, crude gas is introduced into an absorption and regeneration column (2) via line (1) and washed therein. The first exhaust gas stream (5) from the regeneration, which consists of about 76 vol-% hydrocarbon and about 13 vol-% CO2 with small amounts of mercaptans and H2S, is directly introduced into a Claus plant (14).
A second sour gas stream (4) with a low H2S concentration (20.5 vol-%) is introduced into an absorption plant (15), where it is fortified with a non-loaded or hardly loaded solvent from lines (26) and (27). From the absorption plant (15), the solvent (16) loaded with H2S is introduced into a regeneration plant (17). The gas with about 96 vol-% CO2 and 0.2 vol-% mercaptan from the absorption plant (15) is supplied to a hydrogenation (22) via line (18). From the regeneration (17), sour gas with a high H2S concentration (43.8 vol-%) is introduced into the Claus plant (14) via line (19).
From the absorption and regeneration column (2), a third gas stream (3) with a mercaptan content of about 0.01 vol-% is withdrawn, cooled (6) and supplied to an adsorption (8) via line (7). From this adsorption (8), the valuable gas is supplied to further processes, e.g. a liquefaction, via line (9). The mercaptan-containing gas stream is subjected to a physical washing stage, from which part of the valuable gas is recovered as fuel gas via line (12), and via line (13) the highly concentrated mercaptan gas is supplied to the Claus plant (14). The mercaptan stream is recovered in the regeneration of the Purisol solvent. The amount is small, but with a very high mercaptan concentration of about 54 vol-%. In the Claus plant (14), the mercaptan is burnt completely. The resulting SO2 is reacted with the H2S from the sour gas of line (19) to obtain sulfur. The liquid sulfur obtained is withdrawn via line (21) and supplied to a further use. The residual gas of the Claus plant chiefly consists of the components CO2, N2 and H2O and is withdrawn via line (20).
| Number | Date | Country | Kind |
|---|---|---|---|
| 102 08 253 | Feb 2002 | DE | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/EP03/00582 | 1/22/2003 | WO | 00 | 8/23/2004 |
| Publishing Document | Publishing Date | Country | Kind |
|---|---|---|---|
| WO03/072225 | 9/4/2003 | WO | A |
| Number | Name | Date | Kind |
|---|---|---|---|
| 3989811 | Hill | Nov 1976 | A |
| 4372925 | Cornelisse | Feb 1983 | A |
| 4552572 | Galstaun | Nov 1985 | A |
| 4957715 | Grover et al. | Sep 1990 | A |
| 6740230 | Hugo et al. | May 2004 | B1 |
| Number | Date | Country |
|---|---|---|
| WO 9726069 | Jul 1997 | WO |
| WO 9726070 | Jul 1997 | WO |
| Number | Date | Country | |
|---|---|---|---|
| 20050103194 A1 | May 2005 | US |
