Systems and methods for converting gases to liquids
A system and method of converting natural gases to liquids is provided. The system includes a catalytic partial oxidation (CPO) system with natural gas, air and steam input, a Fischer-Tropsch (F-T) system taking syngas from the CPO system, and supplying product gases to a power engine (PE), after separation of the product liquids. An F-T steam output line is in fluid communication with the CPO-steam input line. The energy output from the PE is supplied to the compressors and condensers, to provide self-sustainability in energy, for the gas-to-liquid separation system.
1. A method comprising:
a. providing natural gas, air, and steam to a catalytic partial oxidation (CPO) system as a CPO input;
b. carrying out a CPO reaction to produce a CPO output comprising syngas and nitrogen;
c. feeding at least a portion of the CPO output as a Fischer-Tropch (F-T) reactor input, to an F-T system;
d. feeding water as an input to an outer region of the F-T system;
e. carrying out an F-T reaction in the F-T system to produce an F-T steam product, and an F-T reactor output comprising F-T liquids and F-T gases;
f. feeding the F-T gases as an input to a power engine (PE); and
g. supplying at least a portion of the F-T steam as a feed-input to the CPO system.
2. The method of claim 1 , wherein a temperature of the CPO system during the initial CPO reaction is less than about 400° C.
3. The method of claim 1 , wherein after an initial start-up period, the CPO reaction is carried out in the absence of any external heat input.
4. The method of claim 1 , wherein the CPO input has an oxygen to carbon ratio in a range from about 0.5 to about 1.5.
5. The method of claim 1 , wherein the CPO input has a steam to carbon ratio in the range from about 0.3 to about 1.5.
6. The method of claim 1 , wherein the syngas comprises hydrogen and carbon monoxide, and the ratio of hydrogen to carbon monoxide is in the range of about 1 to about 3.
7. The method of claim 1 , further comprising the step of compressing the F-T input, prior to feeding the F-T input to the F-T reactor.
8. The method of claim 1 , wherein the PE supplies power for the compression of the F-T input.
9. The method of claim 1 , wherein the F-T-reactor input comprises nitrogen in a range from about 20 volume % to about 50 volume %.
10. The method of claim 1 , wherein the CPO reaction is carried out at a temperature in a range from about 700° C. to about 1000° C.
11. The method of claim 1 , wherein the CPO input exchanges heat with the CPO output to produce a cooled CPO output stream.