Production method of liquid hydrocarbons from natural gas
In a so-called GTL process of producing synthesis gas from natural gas, producing Fischer-Tropsch oil by way of Fischer-Tropsch synthesis of the obtained synthesis gas and producing liquid hydrocarbons containing fuel oil by upgrading, the synthesis gas produced from the synthesis gas production step is partly branched off prior to getting to the Fischer-Tropsch oil production step and the synthesis gas entering the branch line is subjected to a water gas shift reaction to raise the hydrogen concentration thereof. Subsequently, high-purity hydrogen is isolated from the synthesis gas and the residual gas left after the isolation is circulated to the synthesis gas production step and used as raw material for synthesis gas production. As a result, a significant improvement can be achieved in terms of raw material consumption per product of the entire process.
1. A production method of liquid hydrocarbons from natural gas, comprising:
a hydrodesulfurization step of removing sulfur compounds in natural gas by hydrodesulfurization;
a synthesis gas production step of producing synthesis gas by way of a reforming reaction of the natural gas after hydrodesulfurization with steam and/or carbon dioxide;
a Fischer-Tropsch oil production step of producing Fischer-Tropsch oil from the synthesis gas by subjecting the synthesis gas produced from the synthesis gas production step to a Fischer-Tropsch reaction;
an upgrading reaction step of hydrogenating the Fischer-Tropsch oil produced from the Fischer-Tropsch oil production step;
an upgrading gas/liquid separation step of subjecting the hydrogenated product obtained by the upgrading reaction step to gas/liquid separation to obtain liquid hydrocarbons;
a shift step of partly branching the synthesis gas produced from the synthesis gas production step to form a branch line at a stage prior to getting to the Fischer-Tropsch oil production step and raising the hydrogen concentration by subjecting the synthesis gas into the branch line to a water gas shift reaction; and
a hydrogen separation step of separating the high-purity hydrogen from the outlet gas of the shift step and also isolating the consequently produced residual gas,
wherein the residual gas separated in the hydrogen separation step is circulated to the synthesis gas production step in order to use it as raw material for synthesis gas production.
2. The method according to claim 1 , wherein the residual gas separated in the hydrogen separation step contains methane and carbon dioxide as main components.
3. The method according to claim 1 , wherein the high-purity hydrogen gas separated in the hydrogen separation step is supplied to the hydrodesulfurization step and the upgrading reaction step.
4. The method according to claim 2 , wherein the high-purity hydrogen gas separated in the hydrogen separation step is supplied to the hydrodesulfurization step and the upgrading reaction step.
5. The method according to claim 1 , wherein steam and/or carbon dioxide are added at a ratio of H 2 O/C=0.0 to 3.0 and/or at a ratio of CO 2 /C=0.0 to 1.0, where H 2 O and CO 2 represent the number of H 2 O molecules and the number of CO 2 molecules respectively and C represents the number of carbon atoms in hydrocarbons originating from the mixture material of natural gas and hydrocarbons being circulated for use.
6. The method according to claim 2 , wherein steam and/or carbon dioxide are added at a ratio of H 2 O/C=0.0 to 3.0 and/or at a ratio of CO 2 /C=0.0 to 1.0, where H 2 O and CO 2 represent the number of H 2 O molecules and the number of CO 2 molecules respectively and C represents the number of carbon atoms in hydrocarbons originating from the mixture material of natural gas and hydrocarbons being circulated for use.
7. The method according to claim 1 , wherein the outlet temperature and the outlet pressure of the catalyst bed are respectively 800 to 950° C. and 1.5 to 3.0 MPaG and the gas hourly space velocity (GHSV) is 500 to 5,000 hr −1 , in the synthesis gas production step.
8. The method according to claim 2 , wherein the outlet temperature and the outlet pressure of the catalyst bed are respectively 800 to 950° C. and 1.5 to 3.0 MPaG and the gas hourly space velocity (GHSV) is 500 to 5,000 hr −1 , in the synthesis gas production step.
9. The method according to claim 1 , wherein the natural gas supplied as raw material contains hydrocarbons having 1 to 6 carbon atoms, which include methane as a main component, in the synthesis gas production step.
10. The method according to claim 2 , wherein the natural gas supplied as raw material contains hydrocarbons having 1 to 6 carbon atoms, which include methane as a main component, in the synthesis gas production step.