Method for producing synthesis gas

Patent metadata

Field	Value
Publication number	US-2018273380-A1
Application number	US-201615779596-A
Country	US
Kind code	A1
Filing date	Nov 28, 2016
Priority date	Dec 1, 2015
Publication date	Sep 27, 2018
Grant date	—

Abstract

A method for producing synthesis gas may involve introducing a hydrocarbon-containing coke-oven gas and a carbon dioxide-containing converter gas into a first reaction zone where hydrogen present in the hydrocarbon-containing coke-oven gas reacts at least partly with carbon dioxide to form water, which reacts thermally with hydrocarbon to form synthesis gas containing carbon monoxide and hydrogen. The method may further involve introducing an oxygen-containing gas in a second reaction zone, and using the oxygen-containing gas and some hydrogen from the first reaction zone to produce thermal energy. Still further, the method may involve supplying the thermal energy produced in the second reaction zone to the first reaction zone.

First claim

1 - 10 . (canceled)

11 . A method for producing synthesis gas, the method comprising:
introducing a hydrocarbon-containing coke-oven gas and a carbon dioxide-containing converter gas into a first reaction zone where hydrogen in the hydrocarbon-containing coke-oven gas reacts at least partly with carbon dioxide to form water, which reacts thermally with hydrocarbon to form synthesis gas containing carbon monoxide and hydrogen; introducing an oxygen-containing gas in a second reaction zone; producing thermal energy from the oxygen-containing gas and some of the hydrogen from the first reaction zone; and supplying the thermal energy produced in the second reaction zone to the first reaction zone.

12 . The method of claim 11 comprising executing a fixed bed comprising a granular solid as a moving bed that is moved from the second reaction zone to the first reaction zone.

13 . The method of claim 12 comprising recycling the granular solid.

14 . The method of claim 12 comprising:
running a gas emerging from the second reaction zone counter-current to the moving bed and thus cooling the gas emerging from the second reaction zone with the moving bed in direct heat exchange; and
running the hydrocarbon-containing coke oven gas and the carbon dioxide-containing converter gas counter-current to the moving bed into the first reaction zone and thus heating the hydrocarbon-containing coke oven gas and the carbon dioxide-containing converter gas with the moving bed in direct heat exchange.

15 . The method of claim 12 comprising separating carbon deposited on the granular solid downstream of the first reaction zone or a first heat-exchange zone and removing the carbon from the moving bed.

16 . The method of claim 12 comprising using corundum (Al 2 O 3 ), quartz glass (SiO 2 ), mullite (Al 2 O 3 .SiO 2 ), cordierite ((Mg,Fe) 2 (Al 2 Si)[Al 2 Si 4 O 18 ]), steatite (SiO 2 .MgO. Al 2 O 3 ), coal, coke, or hydrocarbon produced in the method by thermal hydrocarbon decomposition as the granular solid.

17 . The method of claim 11 comprising supplying water or steam to the first reaction zone.

18 . The method of claim 11 wherein the hydrocarbon-containing coke-oven gas is a methane-rich gas.

19 . The method of claim 18 wherein the carbon dioxide-containing converter gas is a converter gas produced from operation of a steelworks.

20 . The method of claim 11 wherein the carbon dioxide-containing converter gas is a converter gas produced from operation of a steelworks.

21 . The method of claim 11 wherein a ratio of a gas quantity of the hydrocarbon-containing coke-oven gas to the carbon dioxide-containing converter gas is set between 0.5 and 3 to set a hydrogen to carbon monoxide ratio in the synthesis gas at an output of a reactor between 0.8 and 2.5.

22 . The method of claim 11 comprising adding hydrocarbons to the first reaction zone to set a hydrogen to carbon monoxide ratio in the synthesis gas at an output of a reactor between 0.8 and 2.5.

23 . The method of claim 11 comprising adding methane to the first reaction zone to set a hydrogen to carbon monoxide ratio in the synthesis gas at an output of a reactor between 0.8 and 2.5.

24 . The method of claim 11 comprising adding natural gas to the first reaction zone to set a hydrogen to carbon monoxide ratio in the synthesis gas at an output of a reactor between 0.8 and 2.5.

25 . The method of claim 11 comprising adding carbon dioxide to the first reaction zone to set a hydrogen to carbon monoxide ratio in the synthesis gas at an output of a reactor between 0.8 and 2.5.

26 . The method of claim 11 wherein the thermal energy in the second reaction zone is produced at least partially by electric current.

27 . The method of claim 11 comprising using corundum (Al 2 O 3 ), quartz glass (SiO 2 ), mullite (Al 2 O 3 .SiO 2 ), cordierite ((Mg,Fe) 2 (Al 2 Si)[Al 2 Si 4 O 18 ]), steatite (SiO 2 .MgO. Al 2 O 3 ), coal, coke, or hydrocarbon produced in the method by thermal hydrocarbon decomposition as a granular solid.

Assignees

• Thyssenkrupp Ind Solutions Ag
• Thyssenkrupp Ag

Inventors

• Maass Hans-Jürgen
• Göke Volker
• Machhammer Otto
• Bode Andreas
• Kolios Grigorios
• Büker Karsten

Classifications

• C01B3/28

  using moving solid particles, e.g. fluidised bed technique · CPC title

• C01B3/344 Primary

  using non-catalytic solid particles · CPC title

• C01B2203/0216

  containing a non-catalytic steam reforming step · CPC title

• C01B2203/085

  by electric heating · CPC title

• C01B2203/1241

  Natural gas or methane · CPC title