Process and plant for producing a synthesis gas product stream having an adjustable H
Proposed are a process and a plant for producing a synthesis gas product stream having an adjustable H 2 /CO ratio and a pure hydrogen stream, wherein it is provided according to the invention that a substream of a deacidified synthesis gas stream is supplied to a membrane separation plant fitted with a hydrogen-selective membrane and the remaining substream is supplied to a pressure swing adsorption plant, wherein the latter affords a pure hydrogen stream and a fuel gas stream. The hydrogen-enriched permeate stream obtained from the membrane separation is likewise supplied to the pressure swing adsorption plant, thus enhancing the yield of pure hydrogen. The hydrogen-depleted retentate stream obtained from the membrane separation is discharged as a synthesis gas product stream and if of a suitable composition may be utilized as oxo gas.
1. A process for producing a synthesis gas product stream having an adjustable hydrogen-carbon monoxide ratio (H 2 /CO ratio) and a pure hydrogen stream from an input stream containing hydrocarbons, comprising:
(a) providing the input stream containing hydrocarbons;
(b) supplying the input stream containing hydrocarbons to a synthesis gas production plant comprising:
(b1) a steam reforming stage, or
(b2) an autothermal reforming stage (ATR), or
(b3) a partial oxidation stage (PDX), or
(b4) a combination of at least two of the stages (b1) to (b3);
(c) at least partial conversion of the input stream containing hydrocarbons in the synthesis gas production plant under synthesis gas production conditions to afford a raw synthesis gas stream containing hydrogen (H 2 ) and carbon monoxide (CO);
(d) discharging a raw synthesis gas stream from the synthesis gas production plant;
(e) introducing at least a first proportion of the raw synthesis gas stream into a CO conversion plant comprising at least one CO conversion stage, converting the proportion of the raw synthesis gas stream introduced into the CO conversion plant under CO conversion conditions to afford a verted synthesis gas stream, discharging the converted synthesis gas stream;
(f) introducing the raw synthesis gas stream and/or the converted synthesis gas stream into a sorption apparatus for removal of acidic gas constituents using a physical or chemical sorption process, discharging a deacidified synthesis gas stream from the sorption apparatus;
(g) introducing at least a second proportion of the deacidified synthesis gas stream into a first hydrogen enrichment stage containing a hydrogen selective membrane as the separating means, separating the deacidified synthesis gas stream into a hydrogen-enriched permeate stream and into a hydrogen-depleted retentate stream;
(h) introducing the hydrogen-enriched permeate stream and the proportion of the deacidified synthesis gas stream not passed to the first hydrogen enrichment stage into a second hydrogen enrichment stage operating according to the principle of pressure swing adsorption (PSA);
(i) discharging a pure hydrogen stream and a carbon monoxide-containing residual gas stream from the second hydrogen enrichment stage; and
(j) discharging the hydrogen-depleted retentate stream from the first hydrogen enrichment stage as a synthesis gas product stream,
wherein the first proportion and/or the second proportion are chosen such that the molar H 2 /CO ratio required for the synthesis gas product stream is obtained.
2. The process according to claim 1 , wherein the first proportion is between 0% and 100% of the raw synthesis gas stream and/or the second proportion is between 0% and 100% of the deacidified synthesis gas stream.
3. The process according to claim 1 , wherein a third proportion of the carbon monoxide-containing residual gas stream is passed into the synthesis gas product stream and the first proportion and/or the second proportion and/or the third proportion are chosen such that the H 2 /CO ratio required for the synthesis gas product stream is obtained.
4. The process according to claim 3 , wherein the first proportion is between 0% and 100% of the raw synthesis gas stream and/or the second proportion is between 0% and 100% of the deacidified synthesis gas stream and/or the third proportion is between 0% and 100% of the carbon monoxide-containing residual gas stream.
5. The process according to claim 1 , wherein the molar H 2 /CO ratio of the synthesis gas product stream is between 10 and 0.1 mol/mol.
6. The process according to claim 1 , wherein the raw synthesis gas stream less the first proportion is directly supplied to the sorption apparatus.
7. The process according to claim 1 , wherein the deacidified synthesis gas stream less the second proportion is directly supplied to the second hydrogen enrichment stage.
8. The process according to claim 3 , wherein the residual gas stream less the third proportion is discharged from the process as fuel gas.
9. The process according to claim 1 , wherein the carbon monoxide-containing residual gas stream is compressed before supplying to the synthesis gas product stream.
10. The process according to claim 1 , wherein the carbon monoxide-containing residual gas stream is supplied to a fine purification stage before supplying to the synthesis gas product stream or is supplied to a joint fine purification stage after supplying to the synthesis gas product stream.
11. The process according to claim 1 , wherein the hydrogen-enriched permeate stream is compressed before supplying to the second hydrogen enrichment stage.