Method for utilizing thermal energy of product gases in a btl plant

Abstract

The invention for utilizing thermal energy of gases generated in a BtL plant. A feature of the invention is that the thermal energy of discharge gas streams generated in the BtL plant is used for driving various compressor machineries and/or electricity generation, whereby the plant can operate as a stand-alone facility.

1 . A method for utilizing thermal energy of gases generated in a BtL plant, wherein the thermal energy of gases generated in the production process of the BtL plant is utilized in superheating steam for driving the turbine machineries of the BtL plant. 
     
     
         2 . The method of  claim 1 , wherein the method the compressors and/or electric generators of the plant process stages are driven by steam turbines using the steam streams generated in the BtL plant processes that are superheated by the flue gases of a steam reformer, that is, an SMR reactor integrated with the BtL plant equipment and, additionally, to maximize the yield of end products of the BtL plant, hydrogen is recovered with the help of a PSA unit. 
     
     
         3 . The method of  claim 1 , wherein the method superheating the saturated steam streams generated in the BtL processes substantially increases the self-supported electrical balance of the BtL and facilitates self-contained operation of the BtL plant as a stand-alone facility independent from another industrial plant or power utility, while simultaneously the yield of end product is maximized. 
     
     
         4 . The method of  claim 1 , wherein a BtL plant has integrated thereto a method for utilizing the thermal energy of the flue gases and/or reformed gas of a steam reformer for superheating the steam that is used in the BtL plant for driving a syngas turbocompressor and/or producing electricity as well as improving the hydrogen yield, whereby a WGS process is included having a steam reformer connected to a PSA unit. 
     
     
         5 . The method of  claim 1 , wherein a BtL plant generates in its FT process different FT tail gases, that is, process reject gases, which are passed to a steam reformer, wherein the FT tail gases are reformed in such a way that the hydrocarbons of gases are reformed into hydrogen and substantially into carbon monoxide and therefrom further to carbon dioxide, from which gas stream after cooling in a PSA unit hydrogen is recovered, whereupon the remaining gases are recirculated to a steam reformer for heating the steam reformer to a correct temperature of about 800-1100° C. 
     
     
         6 . The method of  claim 1 , wherein gases reformed in steam reformer and flue gases exiting the steam reformer are passed for cooling to a heat exchanger, whereby the thermal energy of the gas streams is used for superheating the saturated high-pressure steam exiting the gasifier. 
     
     
         7 . The method of  claim 1 , wherein heat exchanger comprises superheaters and, wherein saturated high-pressure steam is superheated for compressor/turbine and that boilers and a superheater are employed for producing steam required in steam reforming. 
     
     
         8 . The method of  claim 1 , wherein to the compressor/turbine combination and operating as a turbocompressor is connected a steam condensation turbine, whereto are passed the low-pressure and middle-high-pressure steam streams generated in the BtL plant and a generator is provided for electricity generation. 
     
     
         9 . Use of thermal energy of gases generated in a BtL plant for superheating steam streams driving the turbine machineries of the BtL plant and postprocessing gas streams for hydrogen recovery therefrom. 
     
     
         10 . The use according to  claim 9  for utilizing saturated steam streams generated in a BtL plant, wherein superheating increases the self-supported electrical balance of the BtL and facilitates self-contained operation of the BtL plant as a stand-alone facility independent from another industrial plant or power utility, while simultaneously the yield of end product is maximized. 
     
     
         11 . The use according to  claim 9  of a steam reformer such as an SMR reactor integrated with the BtL plant equipment for superheating the discharge gas streams generated in the BtL plant to drive the plant's compressors and/or electricity generation units and, additionally, to maximize the yield of end products of the BtL plant, whereby hydrogen is recovered with the help of a PSA unit. 
     
     
         12 . The use according to  claim 9  for utilizing the thermal energy of the flue gases and/or reformed gas for superheating the steam that is used in the BtL plant for driving the syngas turbocompressor and/or producing electricity. 
     
     
         13 . The use according to  claim 9  for improving the yield of the BtL plant, whereby a WGS process is used having a steam reformer and a PSA unit integrated with the BtL plant equipment. 
     
     
         14 . The method of  claim 2 , wherein the method superheating the saturated steam streams generated in the BtL processes substantially increases the self-supported electrical balance of the BtL and facilitates self-contained operation of the BtL plant as a stand-alone facility independent from another industrial plant or power utility, while simultaneously the yield of end product is maximized. 
     
     
         15 . The method of  claim 2 , wherein a BtL plant has integrated thereto a method for utilizing the thermal energy of the flue gases and/or reformed gas of a steam reformer for superheating the steam that is used in the BtL plant for driving a syngas turbocompressor and/or producing electricity as well as improving the hydrogen yield, whereby a WGS process is included having a steam reformer connected to a PSA unit. 
     
     
         16 . The method of  claim 3 , wherein a BtL plant has integrated thereto a method for utilizing the thermal energy of the flue gases and/or reformed gas of a steam reformer for superheating the steam that is used in the BtL plant for driving a syngas turbocompressor and/or producing electricity as well as improving the hydrogen yield, whereby a WGS process is included having a steam reformer connected to a PSA unit. 
     
     
         17 . The method of  claim 2 , wherein a BtL plant generates in its FT process different FT tail gases, that is, process reject gases, which are passed to a steam reformer, wherein the FT tail gases are reformed in such a way that the hydrocarbons of gases are reformed into hydrogen and substantially into carbon monoxide and therefrom further to carbon dioxide, from which gas stream after cooling in a PSA unit hydrogen is recovered, whereupon the remaining gases are recirculated to a steam reformer for heating the steam reformer to a correct temperature of about 800-1100° C. 
     
     
         18 . The method of  claim 3 , wherein a BtL plant generates in its FT process different FT tail gases, that is, process reject gases, which are passed to a steam reformer, wherein the FT tail gases are reformed in such a way that the hydrocarbons of gases are reformed into hydrogen and substantially into carbon monoxide and therefrom further to carbon dioxide, from which gas stream after cooling in a PSA unit hydrogen is recovered, whereupon the remaining gases are recirculated to a steam reformer for heating the steam reformer to a correct temperature of about 800-1100° C. 
     
     
         19 . The method of  claim 4 , wherein a BtL plant generates in its FT process different FT tail gases, that is, process reject gases, which are passed to a steam reformer, wherein the FT tail gases are reformed in such a way that the hydrocarbons of gases are reformed into hydrogen and substantially into carbon monoxide and therefrom further to carbon dioxide, from which gas stream after cooling in a PSA unit hydrogen is recovered, whereupon the remaining gases are recirculated to a steam reformer for heating the steam reformer to a correct temperature of about 800-1100° C. 
     
     
         20 . The method of  claim 2 , wherein gases reformed in steam reformer and flue gases exiting the steam reformer are passed for cooling to a heat exchanger, whereby the thermal energy of the gas streams is used for superheating the saturated high-pressure steam exiting the gasifier.