초록 ▼

An economical, efficient process is provided employing coal, particularly subbituminous coal, as a fuel source for the production of distillate fuels, methanol, and methane. A hydroliquefier is operated under severe conditions to provide a high net yield of light distillates which are separated by d

An economical, efficient process is provided employing coal, particularly subbituminous coal, as a fuel source for the production of distillate fuels, methanol, and methane. A hydroliquefier is operated under severe conditions to provide a high net yield of light distillates which are separated by distillation. The vacuum residue, which is produced above, is transferred as a slurry to a partial oxidation gasifier where synthesis gas is produced as feedstock for methanol or methane synthesis. Gaseous hydrocarbon contaminants are separated and used to generate additional synthesis gas, or to supply other fuel requirements. No net heavy distillates are taken as a product, being used as a fuel or converted to other products.

대표청구항 ▼

A highly efficient method of producing from coal liquid volatile products having fuel values which comprises: (a) in a hydroliquefaction zone liquefying coal by contacting comminuted coal with hydrogen and a hydrogen donor recycle solvent boiling in the range of about 400°-975°F. under severe condit

A highly efficient method of producing from coal liquid volatile products having fuel values which comprises: (a) in a hydroliquefaction zone liquefying coal by contacting comminuted coal with hydrogen and a hydrogen donor recycle solvent boiling in the range of about 400°-975°F. under severe conditions comprising temperatures in the range of 800°to 900°F. and pressures in the range of 1,000 to 3,000 psig and a solvent to coal weight ratio of 1.5-3:1 to produce a high yield of light distillates boiling below about 650°F. said yield of light distillates comprising from about 15 to 45 weight percent of the coal (dry ash free basis), whereby a substantially gaseous effluent and a substantially liquid effluent are obtained; (b) transferring said liquid effluent to a vacuum distillation separation zone and distilling said liquid effluent into a light distillate fraction, boiling below about 400°F., a middle distillate solvent fraction boiling between about 400°to 650°F., a heavy distillate fraction boiling between about 650°to 975°F., and vacuum bottoms slurry boiling above about 975°F., the quantity of which, when gasified, will supply substantially more gas than is required for producing hydrogen for the hydroliquefier; (c) pumping said vacuum bottoms slurry into a partial oxidation gasifier and transforming said bottoms to synthesis gas consisting essentially of carbon monoxide and hydrogen; (d) shifting the hydrogen to carbon monoxide ratio of the said synthesis gas to produce a hydrogen enriched gas and removing the acid gases therefrom; (e) recycling a portion of said hydrogen enriched gas from said synthesis gas from step (d) to the hydroliquefier; (f) reacting the remainder of said synthesis gas to produce methanol or methane; (g) recycling at least a portion of said 400°-650°F. and said 650°-975°F. fractions in admixture as said recycle hydrogen donor solvent to said hydroliquefaction zone. (h) utilizing excess of said 650°-975°F. as fuel for the plant. (i) withdrawing the remainder of product boiling below about 650°F. not recycled in step (g).