Texaco Inc.

Warren G Schlinger

William L Slater

Peter L Paull

George N Richter

Edward T Child

William B Crouch

James R Muenger

Everett M Barber

David L Alexander

Everett M Johnson

In the partial oxidation of a sulfur- and metal-containing carbonaceous charge fuel to produce a sulfur-containing synthesis gas and metal-containing molten slag, an integrated method of charge fuel pretreatment and Claus unit tail gas sulfur removal is provided. The process of the instant invention is advantageous over other partial oxidation processes in that: (i) a fluid, molten slag which flows easily is produced, thereby improving reactor performance; and (ii) the overall removal of sulfur compounds from the synthesis gas is made simpler, more efficient, and less costly, as the need for a conventional Claus unit tail gas sulfur removal process is eliminated.

Integrated method of charge fuel pretreatment and tail gas sulfur

A high turndown de-slagging burner is provided for simultaneously introducing one or two mixed pairs of reactant feedstreams into a free-flow noncatalytic partial oxidation gas generator for the production of synthesis gas, fuel gas, or reducing gas by way of the central and/or annular sections of the burner, respectively. Each pair of feedstreams comprises a stream of free-oxygen containing gas with or without a temperature moderator and a pumpable liquid slurry stream of solid carbonaceous fuel, such as a coal-water slurry. Other hydrocarbonaceous fuels may be employed. The burner comprises four coaxial concentric conduits that are radially spaced to provide coaxial concentric annular passages. All of the conduits and annular passages are closed at the upstream ends and open at the downstream ends. Each pair of feedstreams is separately mixed together in a central or annular pre-mix chamber located upstream from the face of the burner. A water-cooled flat face-plate is provided with separate passages for discharging air or soot-blowing or de-slagging media at the face of the burner.

Partial oxidation process

A slag trap structure is for use where synthesis gas is generated having small particulate slag entrained therewith. It has a high pressure shell with a body of water at the bottom for quenching and removing the slag. There is a coaxial inner wall to direct the flow of synthesis gas and slag down from an inlet at the top toward the body of water. And there is an outlet spaced substantially above the level of the water to cause reversal of the gas and slag flow. Also, there is means for recirculating some clean gas in conjunction with the inner wall to direct a swirling flow that confines the downward flow centrally in the vessel.

Apparatus for gasifying coal including a slag trap

A high turndown de-slagging burner is provided for simultaneously introducing one or two mixed pairs of reactant feedstreams into a free-flow noncatalytic partial oxidation gas generator for the production of synthesis gas, fuel gas, or reducing gas by way of the central and/or annular sections of the burner, respectively. Each pair of feedstreams comprises a stream of free-oxygen containing gas with or without a temperature moderator and a pumpable liquid slurry stream of solid carbonaceous fuel, such as a coal-water slurry. Other hydrocarbonaceous fuels may be employed. The burner comprises four coaxial concentric conduits that are radially spaced to provide coaxial concentric annular passages. All of the conduits and annular passages are closed at the upstream ends and open at the downstream ends. Each pair of feedstreams is separately mixed together in a central or annular pre-mix chamber located upstream from the face of the burner. A water-cooled flat face plate is provided with separate passages for discharging air or soot-blowing or de-slagging media at the face of the burner.

Partial oxidation burner

A process for conversion of hydrogen and carbon monoxide into hydrocarbons in the presence of an ebullient bed of catalyst comprising reduced iron oxide promoted with potassium equivalent to 2-10 pounds potassium carbonate per 1000 pounds iron oxide catalyst, and having an average particle size in the range of 100-1000 microns, wherein the catalyst is chlorided for increasing the yield of C.sub.1 -C.sub.4 range hydrocarbons.

Catalysts comprising halogenated, reduced iron oxide-potassium carbonate

A process for conversion of hydrogen and carbon monoxide into hydrocarbons in the presence of an ebullient bed of catalyst comprising reduced iron oxide containing an amount of potassium equivalent to 2 to 10 pounds potassium carbonate per 1000 pounds iron oxide catalyst, and having an average particle size in the range of 100-1000 microns. The catalyst may be sulfided for increasing the yield of C.sub.1 -C.sub.4 range hydrocarbons.

Catalyst for conversion of hydrogen and carbon monoxide into C.sub.1 -C.sub

Conversion of hydrogen and carbon monoxide into C.sub.1 -C.sub.4 range

Solid carbonaceous fuels are converted into gaseous fuels by a process comprising liquefying at least a portion of the solid fuel, subjecting a portion of the high boiling product to gasification with substantially pure oxygen to provide hydrogen for the liquefaction, subjecting the balance of the high boiling product to gasification with air to provide a gaseous product used as the stripping medium to remove lighter boiling materials from the liquefaction product and recovering fuel gas from the stripping zone overhead.

Conversion of solid fuels into fluid fuels

Power is developed by an expansion turbine in which the working fluid is a gaseous mixture comprising all of the hot raw gas stream leaving an unpacked partial oxidation gas generator, after removing if present a portion of the entrained solids, in admixture with a temperature moderating stream. A molal increase is associated with the partial oxidation process. Power is obtained from this molal increase in addition to the power obtained from the elevated pressure and sensible heat in the hot raw partial oxidation product gas. The temperature moderating stream may comprise a recycle portion of the turbine exhaust gas stream after being cooled, cleaned, optionally water-gas shifted or purified, or both, and recompressed. Alternatively, the recycle gas stream may be mixed with water, steam, or both. In one embodiment the temperature moderating stream comprises liquid water or condensate produced in the process. Auxiliary gas compressors for recompressing said recycle gas, and optionally for compressing a free-oxygen containing gas for use in the gas generation zone may be driven by said expansion turbine. Similarly, an electric generator may be coupled to the turbine shaft.

Partial oxidation process with production of power

A raw synthesis gas feed stream, e.g., gaseous mixtures comprising H.sub.2 and CO and containing gaseous impurities including CO.sub.2, H.sub.2 S, COS, and mixtures thereof (acid gas) and CH.sub.4, optionally in admixture with a CO-rich gas stream produced subsequently in the process, is introduced into a water-gas shift reactor to produce H.sub.2 and CO.sub.2. Acid gases are then removed to produce a stream of purified synthesis gas by contacting the process gas stream with a first liquid solvent absorbent such as methanol, N-methyl-pyrrolidone, or dimethyl ether of polyethylene glycol. An H.sub.2 -rich gas stream may be obtained by removing CO from the purified synthesis gas stream. This may be done by physical absorption in a second liquid solvent absorbent comprising an aqueous solution of cuprous ammonium acetate. By regenerating the second liquid solvent, the aforesaid CO-rich stream may be produced. The first liquid solvent absorbent may be desorbed of said acid gas and regenerated for reuse by such techniques as flashing plus reboiling or stripping. Advantageously, the gas used for stripping the first liquid solvent absorbent may be a portion of the synthesis gas feed either before or after removal of said acid-gas, or a portion of said H.sub.2 -rich product gas. The CO.sub.2 -rich gas optionally in admixture with stripping gas which is produced during the regeneration of said first liquid solvent absorbent may be injected into a subterranean oil reservoir to effect secondary or tertiary recovery of oil. Optionally, H.sub.2 S may be in admixture with said CO.sub.2 -rich gas mixture.

Production of purified synthesis gas H.sub.2 -rich gas, and by-product

The subject process pertains to the secondary recovery of oil by the steam stimulation of an underground oil reservoir. As an added benefit, mechanical power and/or electrical energy may be simultaneously produced. In the subject process, raw fuel gas is first produced by the partial oxidation in a free-flow gas generator of a hydrocarbonaceous feed, such as preferably a portion of the oil recovered. The raw fuel gas is cleaned, purified, and burned in a gas turbine which drives a compressor or electric generator. The sensible heat in the raw fuel gas leaving the gas generator and in the flue gas discharged from the gas turbine is recovered by the production of high quality steam. This steam is injected into subterranean formations and reservoirs to accelerate production and to provide additional oil recovery.

Secondary recovery of oil by steam stimulation plus the production of

Production of a gas suitable for use as a fuel or for conversion into a fuel and simultaneous production of a gas saturated with steam suitable for use as feed to a shift conversion zone.

Synthesis gas generation

This is an improved continuous partial oxidation process for producing synthesis gas or fuel gas from gaseous CO.sub.2 -solid carbonaceous fuel feeds. A solid carbonaceous fuel such as finely ground coal from a pressurized lock hopper is passed directly into a high pressure high velocity CO.sub.2 -rich gas stream which carries the particles of coal into a free-flow noncatalytic gas generator where by the partial oxidation reaction with a free-oxygen containing gas, preferably in the absence of supplemental H.sub.2 O other than that normally present in the reactants, gaseous mixtures principally comprising H.sub.2, CO, CO.sub.2, and H.sub.2 O are produced. A CO.sub.2 -rich gas stream is recovered downstream in the process and recycled to the pressurized feed system. The CO.sub.2 -rich stream serves as a carrier for the carbonaceous fuel and as a reactant in the reaction zone.

Synthesis gas from gaseous CO.sub.2 -solid carbonaceous fuel feeds

This is an improved continuous partial oxidation process for producing synthesis gas or fuel gas from a solid carbonaceous fuel. Liquid CO.sub.2 and a ground solid carbonaceous fuel such as coal are mixed together to produce a pumpable slurry feed. The CO.sub.2 serves as a carrier for the carbonaceous fuel and as a temperature moderator, and is preferably obtained by purifying the product gas.

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Pasadena, CA, United States of America

Warren G Schlinger