A system for methanol synthesis from a synthesis gas rich in hydrogen and CO2/CO having a first adiabatic reactor (11) with a structure having an inlet stream (10), a first catalytic bed (12), one Venturi type mixing element (13), a first divergent nozzle (14), a second catalytic bed (27) and one outlet stream (28) all of them connected sequentially to each other; a first heat exchanger (15) connected to the outlet stream (28) downstream the reactor (11); a condenser (16) connected to the heat exchanger (15) downstream of the heat exchanger (15); a separator (18) connected to the condenser (16); a first cold gas stream (19) joining the separator (18) to both the first heat exchanger (15) and the first Venturi type mixing element (13); a first outlet stream (21) joining the heat exchanger (15) to a second adiabatic reactor (24) similar to the first adiabatic reactor (11).

A system for methanol synthesis from a synthesis gas rich in hydrogen and CO2/CO having a first adiabatic reactor (11) with a structure having an inlet stream (10), a first catalytic bed (12), one Venturi type mixing element (13), a first divergent nozzle (14), a second catalytic bed (27) and one outlet stream (28) all of them connected sequentially to each other; a first heat exchanger (15) connected to the outlet stream (28) downstream the reactor (11); a condenser (16) connected to the heat exchanger (15) downstream of the heat exchanger (15); a separator (18) connected to the condenser (16); a first cold gas stream (19) joining the separator (18) to both the first heat exchanger (15) and the first Venturi type mixing element (13); a first outlet stream (21) joining the heat exchanger (15) to a second adiabatic reactor (24) similar to the first adiabatic reactor (11).

A plasma carbon sequestration system and method are disclosed, wherein in the plasma carbon sequestration system, a first channel and a second channel of a plasma reactor are each provided with a flow controller, the plasma reactor is connected to a high voltage via a high voltage electrode and grounded via a ground electrode, water, or hydrogen, or methane is mixed with carbon dioxide respectively, to be introduced into the plasma reactor in a predetermined proportion under the control of the flow controllers, and a condenser is connected to the plasma reactor to condense a conversion product, and reactants which are not completely reacted from the plasma reactor, and is selectively used for circulation in the plasma reactor, thereby realizing environment-friendly treatment without a catalyst by a room temperature plasma technology.

A plasma carbon sequestration system and method are disclosed, wherein in the plasma carbon sequestration system, a first channel and a second channel of a plasma reactor are each provided with a flow controller, the plasma reactor is connected to a high voltage via a high voltage electrode and grounded via a ground electrode, water, or hydrogen, or methane is mixed with carbon dioxide respectively, to be introduced into the plasma reactor in a predetermined proportion under the control of the flow controllers, and a condenser is connected to the plasma reactor to condense a conversion product, and reactants which are not completely reacted from the plasma reactor, and is selectively used for circulation in the plasma reactor, thereby realizing environment-friendly treatment without a catalyst by a room temperature plasma technology.

The disclosure relates to methods of capturing carbon by microbial fermentation of a gaseous substrate comprising CO into one or more first products which, in turn, may be incorporated into an article of manufacture or one or more second products. Further, the disclosure relates to improving carbon capture and/or efficiency.

The disclosure relates to methods of capturing carbon by microbial fermentation of a gaseous substrate comprising CO into one or more first products which, in turn, may be incorporated into an article of manufacture or one or more second products. Further, the disclosure relates to improving carbon capture and/or efficiency.

Catalytic CO.sub.2 hydrogenation to ethanol utilizing radio frequency is very attractive due to higher selectivity (˜99%) to ethanol and yield of 0.000718 g/h or higher. A dielectric barrier discharge (DBD) plasma reactor packed with a catalyst comprising of Cu/Zn/Al.sub.2O.sub.3 can be used for this purpose, which can be operated at approximately 100-200° C., 1-20 atm pressure and gas flow rates above 20 mL/min. The reactor can be made of a simple inert tube. The process is very attractive for a feasible industrial application. To scale up the process to industrial relevance, a multi-tubular reactor configuration is proposed.

Catalytic CO.sub.2 hydrogenation to ethanol utilizing radio frequency is very attractive due to higher selectivity (˜99%) to ethanol and yield of 0.000718 g/h or higher. A dielectric barrier discharge (DBD) plasma reactor packed with a catalyst comprising of Cu/Zn/Al.sub.2O.sub.3 can be used for this purpose, which can be operated at approximately 100-200° C., 1-20 atm pressure and gas flow rates above 20 mL/min. The reactor can be made of a simple inert tube. The process is very attractive for a feasible industrial application. To scale up the process to industrial relevance, a multi-tubular reactor configuration is proposed.

A bifunctional catalyst for example for conversion of oxygenates, the bifunctional catalyst comprising zeolite, alumina binder, Zn and P, wherein Zn is present at least partly as ZnAl.sub.2O.sub.4.

A bifunctional catalyst for example for conversion of oxygenates, the bifunctional catalyst comprising zeolite, alumina binder, Zn and P, wherein Zn is present at least partly as ZnAl.sub.2O.sub.4.