Systems and Methods for the Devolatilization of Thermally Produced Liquids

Abstract

Methods and systems for the devolatilization of thermally produced liquids to raise the flash point are disclosed. Various methods and apparatus can be used to effectively reduce the volatile components, such as wiped film evaporator, falling film evaporator, flash column, packed column, devolatilization vessel or tank.

What is claimed is: 
     
         1 . A method of increasing the flash point of a starting liquid by devolatilization of the starting liquid, wherein the starting liquid is produced from thermal conversion, the method comprising:
 i) supplying the starting liquid to a first component;   ii) heating the first component to a temperature in the range of 20° C. to 200° C.;   iii) obtaining a processed liquid product, wherein the processed liquid has an increased flash point and a reduced concentration of volatile components as compared to the starting liquid; and   iv) obtaining a volatile components product.   
     
     
         2 . The method of  claim 1 , wherein the first component is a wiped film evaporator. 
     
     
         3 . The method of  claim 1 , wherein the first component is a falling film evaporator. 
     
     
         4 . The method of  claim 1 , wherein the first component is a packed column. 
     
     
         5 . The method of  claim 1 , wherein the first component is a devolatilization tank. 
     
     
         6 . The method of  claim 1 , wherein the first component comprises an outlet, wherein the outlet includes a carbon filter system. 
     
     
         7 . The method of  claim 1 , wherein the first component comprises an outlet, wherein the outlet includes a scrubber. 
     
     
         8 . The method of  claim 1 , wherein the first component comprises an outlet, wherein the outlet includes a filter system. 
     
     
         9 . The method of  claim 1 , wherein heating comprises heating the first component to a temperature in the range of 20° C. to 150° C. 
     
     
         10 . The method of  claim 1 , wherein heating comprises heating the first component to a temperature in the range of 20° C. to 100° C. 
     
     
         11 . The method of  claim 1 , wherein the volatile components product is directed to a flare. 
     
     
         12 . The method of  claim 1 , further comprising introducing a stripper gas into the first component. 
     
     
         13 . The method of  claim 12 , wherein the stripper gas comprises one or more of nitrogen, air, inert gas, and the product gas obtained during the thermal conversion process. 
     
     
         14 . The method of  claim 1 , wherein the first component comprises an agitator, wherein the agitator is configured to improve the rate of devolatilization. 
     
     
         15 . The method of  claim 1 , wherein the first component comprises a circulation pump, wherein the circulation pump is configured to improve the rate of devolatilization. 
     
     
         16 . The method of  claim 1 , wherein the first component is operated under the influence of a vacuum. 
     
     
         17 . The method of  claim 16 , wherein the first component is adjusted in a range of 10 to 100 mmHg with a product temperature of 10 to 50° C. 
     
     
         18 . The method of  claim 16 , wherein the first component is adjusted in a range of 100 to 350 mmHg with a product temperature of 10 to 100° C. 
     
     
         19 . The method of  claim 16 , wherein the first component is adjusted in a range of 10 to 750 mmHg with a product temperature of 10 to 200° C. 
     
     
         20 . A system for thermal conversion comprising:
 i) a feed system;   ii) a reactor; and   iii) a plurality of condensing chambers, wherein the temperature of the one or more of the plurality of condensing chambers is adjusted to a temperature greater than 30° C.   
     
     
         21 . The system of  claim 20 , wherein the temperature of the one or more of the plurality of condensing chambers is adjusted to a temperature in the range of 30 to 50° C. 
     
     
         22 . The system of  claim 20 , wherein the temperature of the one or more of the plurality of condensing chambers is adjusted to a temperature in the range of 30 to 60° C. 
     
     
         23 . The system of  claim 20 , wherein the temperature of the one or more of the plurality of condensing chambers is adjusted to a temperature in the range of 40 to 75° C. 
     
     
         24 . The method of  claim 1 , wherein the flash point of the devolatilized, processed liquid is elevated in the range of between 1° C. to 50° C., relative to the flash point of the thermally converted starting liquid prior to devolatilization. 
     
     
         25 . The method of  claim 1 , wherein the flash point of the devolatilized, processed liquid is elevated by at least 5° C., relative to the flash point of the thermally converted starting liquid prior to devolatilization. 
     
     
         26 . The method of  claim 1 , wherein the flash point of the thermally converted starting liquid prior to devolatilization comprises a flash point temperature in the range of between 30° C. to 60° C. 
     
     
         27 . The method of  claim 26 , wherein the flash point of the devolatilized, processed liquid comprises a flash point temperature in the range of between 40° C. to 90° C. 
     
     
         28 . The method of  claim 1 , wherein the resulting devolatilized, processed liquid is introduced into at least a second system or apparatus for further processing. 
     
     
         29 . The method of  claim 28 , wherein the at least a second system or apparatus for further processing comprises: a refinery system; a fluidized catalytic cracker (FCC); an FCC refinery system; a coker; a coking unit; a field upgrader unit; a hydrotreater; a hydrotreatment unit; a hydrocracker; a hydrocracking unit; or a desulfurization unit. 
     
     
         30 . The method of  claim 29 , wherein the at least a second system or apparatus for further processing comprises a fluidized catalytic cracker (FCC). 
     
     
         31 . The method of  claim 28 , wherein the introduction of the resulting devolatilized, processed liquid comprises: injecting, feeding, or co-feeding, the devolatilized liquid product into the at least a second system or apparatus via a mixing zone, a nozzle, a retro-fitted port, a retro-fitted nozzle, a velocity steam line, or a live-tap. 
     
     
         32 . The method of  claim 31 , wherein the further processing comprises co-injecting a petroleum fraction feedstock and the devolatilized liquid product into the at least a second system or apparatus;
 wherein the co-injecting comprises co-feeding, independently or separately introducing, injecting, feeding, or co-feeding, the petroleum fraction feedstock and the devolatilized liquid product.   
     
     
         33 . The method of  claim 31 , wherein the further processing comprises co-injecting a renewable fuel oil and the devolatilized liquid product into the at least a second system or apparatus;
 wherein the co-injecting comprises co-feeding, independently or separately introducing, injecting, feeding, or co-feeding, the petroleum fraction feedstock and the devolatilized liquid product.   
     
     
         34 . A method of processing, comprising introducing a devolatilized liquid material into a fluidized catalytic cracker (FCC), wherein the devolatilized liquid material is produced by:
 i) thermally converting biomass, petroleum materials, or both, to form a starting liquid;   ii) supplying the starting liquid to a first component;   iii) heating the first component to a temperature in the range of 20° C. to 200° C.;   iv) obtaining a devolatilized liquid material, wherein the devolatilized liquid material has an elevated flash point temperature and a reduced concentration of volatile components relative to said starting liquid; and   v) obtaining a volatile components product.