초록 ▼

A cost-effective solution for the disposal of solvent deasphalting process bottoms that include spent solid adsorbent material containing ash-producing constituents, asphalt and process reject materials is provided by introducing them in the form of a flowable slurry into a membrane wall gasificatio

A cost-effective solution for the disposal of solvent deasphalting process bottoms that include spent solid adsorbent material containing ash-producing constituents, asphalt and process reject materials is provided by introducing them in the form of a flowable slurry into a membrane wall gasification reactor to produce a synthesis gas and, optionally, subjecting the synthesis gas to a water-gas shift reaction to produce a more hydrogen-rich product stream; process steam and electricity are produced by recovering the sensible heat values from the hot synthesis gas.

대표청구항 ▼

1. A process for the gasification of solvent deasphalting process bottoms containing a spent solid adsorbent material recovered from a solvent deasphalting process to produce synthesis gas, the bottoms containing ash-forming constitutes, the process comprising: a. preparing a flowable slurry of the

1. A process for the gasification of solvent deasphalting process bottoms containing a spent solid adsorbent material recovered from a solvent deasphalting process to produce synthesis gas, the bottoms containing ash-forming constitutes, the process comprising: a. preparing a flowable slurry of the solvent deasphalting process bottoms consisting of the spent solid adsorbent material, asphalt and process reject materials;b. introducing the slurry of solvent deasphalting process bottoms as a pressurized feedstock into a membrane wall gasification reactor with a predetermined amount of oxygen and steam based on the carbon content of the feedstock;c. operating the gasification reactor at a temperature in the range of 900° C. to 1700° C. and a pressure of from 20 bars to 100 bars;d. subjecting the solvent deasphalting process bottoms to partial oxidation to produce hydrogen, carbon monoxide and slag derived from the spent solid adsorbent material;e. recovering the hydrogen and carbon monoxide from the reactor in the form of a hot raw synthesis gas;f. passing the hot raw synthesis gas to a steam generating heat exchanger to cool the hot raw synthesis gas and produce steam;g. recovering steam from the heat exchanger and introducing the steam into a turbine to produce electricity; andh. recovering the cooled synthesis gas. 2. The process of claim 1 in which the solid adsorbent material has at least 50% of its original pore volume blocked by deposited carbonaceous material. 3. The process of claim 1 in which the solid adsorbent material is selected from the group consisting of attapulgus clay, alumina, silica, activated carbon, spent zeolites, spent catalysts composed of alumina and silica alumina, and mixtures thereof. 4. The process of claim 1 in which the solid adsorbent material includes adsorbed heavy polynuclear aromatic molecules, compounds containing sulfur, compounds containing nitrogen, compounds containing metals and/or metals. 5. The process of claim 1 in which the solid adsorbent material is in the form of pellets, spheres, extrudates and/or natural shapes. 6. The process of claim 1 in which the particle size of solid adsorbent material is in the range of from 4 mesh to 60 mesh. 7. The process of claim 1 in which the solid adsorbent material has a surface area in the range of from 10 m2/g to 1000 m2/g. 8. The process of claim 1 in which the solid adsorbent material has a pore size in the range of from 10 angstroms (0.001 micron) to 5000 angstroms (0.5 micron). 9. The process of claim 1 in which the solid adsorbent material has a pore volume in the range of from 0.1 cc/g to 0.5 cc/g. 10. The process of claim 1, wherein the solvent deasphalting process bottoms comprise in the range of from 2% to 50% by weight of solid adsorbent material. 11. The process of claim 1, wherein the solvent deasphalting process bottoms comprise in the range of from 2% to 20% by weight of solid adsorbent material. 12. The process of claim 1, wherein the solvent deasphalting process bottoms comprise in the range of from 2% to 10% by weight of solid adsorbent material. 13. The process of claim 1, wherein the solvent deasphalting process bottoms comprise spent solid adsorbent material in the range of from 0.5% to about 50% by volume. 14. The process of claim 1, wherein the solvent deasphalting process bottoms comprise spent solid adsorbent material in the range of from 2% to 10% by volume. 15. The process of claim 1, wherein the asphalt is derived from naturally occurring hydrocarbons comprising crude oil, bitumen, heavy oil, shale oil, atmospheric and vacuum residues, fluid catalytic cracking slurry oil, coking unit fractionator bottoms, visbreaking process bottoms, or coal liquefaction products. 16. The process of claim 1 in which the asphalt is separated from a hydrocarbon feedstock containing asphaltenes with a paraffinic solvent having from 3 to 8 carbon atoms. 17. The process of claim 1, wherein the process reject materials comprise heavy hydrocarbon molecules containing sulfur, nitrogen and/or heavy aromatic molecules. 18. The process of claim 1, wherein the flowable slurry of solvent deasphalting process bottoms includes a viscosity-adjusting hydrocarbon solvent. 19. The process of claim 1, wherein the flowable slurry of solvent deasphalting process bottoms are dry and includes fluidizing nitrogen gas. 20. The process of claim 1, wherein the ratio of oxygen-to-carbon in the gasification reactor is in the range of from 0.3:1 to 10:1 by weight. 21. The process of claim 1, wherein the ratio of steam-to-carbon in the gasification reactor is in the range of from 0.1:1 to 10:1 by weight. 22. The process of claim 1, further comprising subjecting the cooled synthesis gas from step (f) to a water-gas shift reaction with a predetermined amount of steam, and recovering a stream comprising hydrogen and carbon dioxide. 23. The process of claim 22, wherein the temperature of the synthesis gas subjected to the water-gas shift reaction is in the range of from 150° C. to 400° C. 24. The process of claim 22, wherein the pressure of the synthesis gas subjected to the water-gas shift reaction is in the range of from 1 bar to 60 bars. 25. The process of claim 24, wherein the mole ratio of water-to-carbon monoxide in the water-gas shift reaction vessel is in the range of from 5:1 to 3:1.