Institute of Gas Technology

Suresh P Babu

Gerald L Anderson

Satyendra P Nandi

Richard A Knight

Wilford G Bair

A method for mild gasification of crushed coal in a single vertical elongated reaction vessel providing a fluidized bed reaction zone, a freeboard reaction zone, and an entrained reaction zone within the single vessel. Feed coal and gas may be fed separately to each of these reaction zones to provide different reaction temperatures and conditions in each reaction zone. The reactor and process of this invention provides for the complete utilization of a coal supply for gasification including utilization of caking and non-caking or agglomerating feeds in the same reactor. The products may be adjusted to provide significantly greater product economic value, especially with respect to desired production of char having high surface area.

Pyrolysis of coal

A process for gasification of cellulosic materials in a single gasification vessel wherein the cellulosic materials are introduced directly into a single back-mixed fluidized bed of high heat capacity inert solids. The fluidized bed is maintained at temperatures of about 1200.degree. to about 1600.degree. F., pressures of up to about 500 psig devolatilizing the cellulosic materials. A substantial portion of the heavier hydrocarbons produced by devolatilization of the cellulosic materials is reformed within the gasification vessel and a substantial portion of the devolatilized cellulosic materials is gasified by reaction with hydrogen and steam within the fluidized bed. Cellulosic materials residue is combusted in an oxygen-rich atmosphere in the lower portion of the fluidized bed to principally form heat and cellulosic materials ash. The highly back-mixed fluidized bed results in temperature variation along the height of the bed, including the combustion zone, of less than 100.degree. F. and preferably less than about 90.degree. F. Introduction of cellulosic materials feed to the fluidized bed is vertically adjustable and maintained at a position where the combustion consumes principally cellulosic materials residue. Formed gases, vapor and biomass ash are removed from the top of the gasification vessel in the gas stream. The process provides high throughput, efficient production of low and medium Btu fuel gas. The medium Btu fuel gas may be readily upgraded to high Btu SNG. At least half of the methane required for SNG is produced in the gasification vessel.

Process for gasification of cellulosic materials

A process for gasification of cellulosic biomass in a single gasification vessel wherein the cellulosic biomass is introduced directly into a single back-mixed fluidized bed of high heat capacity inert solids. The fluidized bed is maintained at temperatures of about 1200.degree. to about 1600.degree. F., pressures of up to about 500 psig devolatilizing the biomass. A substantial portion of the heavier hydrocarbons produced by devolatilization of the biomass is reformed within the gasification vessel and a substantial portion of the devolatilized biomass is gasified by reaction with hydrogen and steam within the fluidized bed. Biomass residue is combusted in an oxygen-rich atmosphere in the lower portion of the fluidized bed to principally form heat and biomass ash. The highly back-mixed fluidized bed results in temperature variation along the height of the bed, including the combustion zone, of less than 100.degree. F. Introduction of cellulosic biomass feed to the fluidized bed is vertically adjustable and maintained at a position where the combustion consumes principally biomass residue. Formed gases, vapor and biomass ash are removed from the top of the gasification vessel in the gas stream. The process provides high throughput, efficient production of low and medium Btu fuel gas. The medium Btu fuel gas may be readily upgraded to high Btu SNG. At least half of the methane required for SNG is produced in the gasification vessel.

Process for gasification of cellulosic biomass

A process for fossil fuel refining by contacting ground solid fossil fuel for about 1/2 to about 3 hours with phenol at a temperature of about 600.degree. to 690.degree. F. and a corresponding saturation pressure of about 250 to 430 psig, the phenol being present in greater amounts by weight than the fossil fuel and dissolving refined product from the fossil fuel leaving a solid fuel residue. The phenol containing the refined product is removed from the fuel residue while heated, followed by cooling and separation of the refined product from the phenol which is recycled to the solvent extraction process. The process provides refined products low in mineral matter and sulfur following a low pressure solvent refining process which does not require a proton donor, acid catalyst or an external source of hydrogen.

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Willow Springs, IL, United States of America

Suresh P Babu