Metallgesellschaft Aktiengesellschaft

Paul Rudolph

Hans Kupfer

Paul D Becker

Carl Hafke

Johann Schlauer

Karl Bratzler

Rudolf Kohlen

Georg Kempf

Martin Hirsch

Heinz Jockel

Alexander Doerges

Emil Supp

Rainer Reimert

Gerhard Baron

Herbert Bierbach

Heinz Hiller

Manfred Kuhn

Osman Turna

Paul Lange

Werner Schmidt

Uwe D Marwig

Alexander Dorges

Coarse-grained fuels are gasified in a moving bed under a pressure of 5 to 150 bars with oxygen, water vapor and, if desired, carbon dioxide. The resulting product gas is at temperatures of 250.degree. to 700.degree. C. and is cooled to temperatures in the range from 120.degree. to 220.degree. C. to form an aqueous condensate, which contains distillation products and is known as gas liquor. The gas liquor obtained by the gasification in a moving bed is pressure-relieved to atmospheric or a higher pressure and the flashed-off vapor is supplied to the fluidized bed gasifier. In the fluidized bed gasifier, fine-grained solid fuels are gasified under a pressure which is lower than that in the moving bed. The flashed-off vapor supplied to the fluidized bed supplies at least one-half of the water vapor required for the gasification in the fluidized bed. The water vapor contained in the product gas formed by the gasification in the fluidized bed is cooled and the resulting condensate is treated separately from the gas liquor obtained by the gasification in a moving bed.

Process of gasifying solid fuels in a moving bed and in a fluidized bed

Coarse-grained solid fuels in particle sizes of at least 2 mm are gasified under a pressure of 5 to 150 bars in a fixed bed which is slowly descending and into which the gasifying agents are introduced from below whereas the incombustible mineral constituents are withdrawn as solid ash or liquid slag from the lower end of the bed. Fine-grained solid fuels are gasified in a fluidized bed under a pressure of 1 to 100 bars. Oxygen, steam and/or carbon dioxide are used as gasifying agents for the gasification in the fixed bed and in the fluidized bed. The product gas from the fluidized-bed gasifier has a temperature of 700.degree. to 1200.degree. C. and is indirectly cooled with water. The resulting steam is fed as gasifying agent to the fixed-bed gasifier. The product gas from the fixed-bed gasifier can be indirectly cooled to produce steam and at least part of said steam is fed as gasifying agent to the fluidized-bed gasifier. The steam fed as gasifying agent to the fixed-bed gasifier has a temperature of about 300.degree. to 600.degree. C., preferably of about 400.degree. to 500.degree. C. The steam produced by an indirect heat exchange with the product gas from the fixed-bed gasifier can be superheated by an indirect heat exchange with the product gas from the fluidized-bed gasifier before said steam is fed as gasifying agent to the fluidized-bed gasifier.

Process of gasifying solid fuels

Solid fuels are gasified in a fixed bed with gasifying agents passed through the fixed bed from below. The gasification residues are withdrawn as solid ash or as liquid slag under the fixed bed. The reactor is charged with solid fuels through a lock chamber and with tar through a supply conduit. The tar is delivered to the fuel in numerous individual streams, which are distributed over the cross-section of the fixed bed. In the gasifying reactor, an inclined distributor surface is disposed over the fixed bed and has numerous passage openings for the tar and the solid fuels. The outlet end of the tar supply conduit is directed to the upper portion of the distributor surface. A tar tub having outlet openings is associated with the distributor surface and serves to receive the tar. The distributor surface is rotatable on a vertical axis.

Reactor for gasifying solid fuels

The apparatus serves to continuously charge coarse-grained and fine-grained solid fuels by means of a rotary distributor onto a fixed bed of fuel. The fixed bed is disposed within a reactor for gasifying the fuels. Gasifying agents comprising oxygen, steam and/or carbon dioxide are passed through the fixed bed from below. Residual matter left after the gasification is withdrawn under the fixed bed as solid ash or liquid slag. Fine-grained fuel having a mean particle size up to 5 mm are placed onto the fixed bed as helical layers separately form more coarsely grained fuel having a mean particle size above 5 mm. The more coarsely grained fuel is deposited directly on fine-grained fuel which has just been deposited. The gasifier comprises a rotary distributor that includes at least one passage for the fine-grained fuel and at least one passage for the more coarsely grained fuel. The inlet of the passage for fine-grained fuel is disposed near the center of the rotary distributor. The inlet of the passage for the more coarsely grained fuel is disposed near the periphery of the rotary distributor.

Process and apparatus for charging solid fuels into a fixed-bed gasifier

A process for reducing an ore which comprises:

Process of producing reducing gas from solid fuels

A process of treating aqueous condensate which is formed as a result of the cooling of raw gas produced by the gasification of solid fuels under a pressure of 5 to 150 bars. The condensate formed as a result of the cooling is at a temperature of at least 110.degree. C. and under a pressure of at least 2 bars and at least part of it is pressure-relieved. The flashed-off vapor is removed and the pressure-relieved condensate is fed to a separator, from which a condensate phase consisting mainly of water is withdrawn. The condensate or a portion thereof is used as a coolant for the raw gas. The flashed-off vapor may be burnt.

Process of treating pressurized condensate

In the gasification of granular solid fossil fuel in a reactor wherein the fuel forms a fixed bed moving from top to bottom of the reactor under gravity, oxygen-containing gases and water vapor are fed into the fuel bed through nozzles in the lower portion of the reactor, molten slag at a temperature of about 1350.degree. to 1500.degree. C. is discharged through a conduit which is inclined to the horizontal, and product gas is withdrawn from the reactor above the fuel bed, the improvement which comprises feeding oxygen gas into the reactor adjacent to the inlet of the slag discharge conduit and directed from above onto the molten slag, thereby forming a leakage gas at a temperature of at least about 1500.degree. C. which leakage gas is withdrawn through the slag discharge conduit co-current with the slag. The leakage gas is separated from the slag in a lock chamber and mixed with the product gas. The temperature and/or composition of the leakage gas in the slag discharge conduit may be used to control the rate at which leakage is produced. A corresponding apparatus is described. This simplifies slag discharge and prevents clogging.

Process for removing slag during pressure gasification of solid fuels

An improvement in a known process and apparatus for gasifying coal with water vapor and oxygen under pressure and at elevated temperature wherein coal is dropped onto a grate within a reactor supplied with gasifying agent from below, product gas being withdrawn above. In accordance with the invention an annular wall depends from the reactor top to form an annular gas space through which product gas is withdrawn. The annular space surrounds the top of the coal bed so the coal is preheated thereby. The wall is provided with apertures so that at least 20% of the product gas enters the annular space by traversing that part of the coal bed surrounded by the wall. This results in reduced product gas velocity and entrainment of coal dust.

Process and apparatus for gasifying granular coal under superatmospheric

In a process for producing a fuel gas from a solid fuel by a gasification of solid fuel under a pressure of about 15-100 bars by a treatment with steam and a gas which contains free oxygen, cooling the raw gas to a temperature of about 150.degree.-200.degree. C. and saturating it with water vapor, removing condensate which has formed so that the raw gas contains hydrocarbons having a boiling range from about 20.degree. to 400.degree. C. in an amount of about 10-100 g per standard m.sup.3 of dry gas and has a CO:H.sub.2 O volume ratio of about 0.8-2, and subjecting the raw gas to a shift conversion, the improvement which comprises dividing the raw gas into first and second partial streams in a ratio of about 1:10 to 1:1, feeding the first partial stream with a surplus of water vapor to a first shift conversion stage at an inlet temperature of about 280.degree.-450.degree. C., and passing through a second shift conversion stage a mixture of effluent gas from the first shift conversion stage and at least part of the second partial stream of raw gas at a temperature of about 300.degree.-500.degree. C., while maintaining a pressure of about 15-100 bars in the shift conversion stages. Advantageously water vapor is added to the raw gas entering the first shift conversion stage in at least about 70% of the stoichiometric amount required for shift conversion of all the carbon monoxide contained in the entire raw gas.

Shift conversion of raw gas from gasification of coal

A process for producing lean gases in which solid fuels are gasified under superatmospheric pressure by a treatment with free oxygen-containing gases, water vapor, and other gasifying agents. In the process, fuel and gasifying agent are caused to flow in opposite directions, about 1.5 to 3.5 kg of water vapor are added per standard m.sup.3 of free oxygen in the gasifying agent, about 70% of the lump coal to be gasified has a particle size from above 2 mm to about 30 mm and the remaining coal has a particle size below about 2 mm. The ballast content, consisting of water and ash, amounts to at least about 15% by weight, most of the mineral constituents have a particle size of about 2 to 30 mm and the ash which becomes available in the gasification process is withdrawn from the reactor shaft at temperatures above about 250.degree. C. Raw gas is withdrawn at temperatures above about 350.degree. C, coal is reacted in a water-cooled, double-walled reactor chamber and the resulting jacket steam is used to cool the grate and as a reactant. The rate at which steam consisting of extraneous steam and jacket steam is added to the gasifying agent is so adjusted in the above-mentioned range of about 1.5 to 3.5 kg per standard m.sup.3 of oxygen, that the nitrogen content of the dry raw product gas does not exceed about 50% by volume.

Process for producing a lean gas by the gasification of a fuel mainly in

Gravity separation process for removing tar from water in a condensate formed by the cooling of a raw gas produced by the gasification or dry distillation of solid fuel such as coal. The tar and water condensate formed by cooling the raw gas to about 100.degree. C is enriched in a tar-water separator with ammonium carbonate to a concentration of least 5 grams NH.sub.3 per kg H.sub.2 O. The cooling can be carried out in a plurality of stages with the hotter condensate from at least one of the first cooling stages being mixed at a weight ratio of 10:1 to 1:2 with colder condensate from at least one of the succeeding cooling stages.

Process for breaking emulsions in a tar-containing aqueous condensate

An apparatus for gasifying solid fuels such as coal, in a packed bed by a treatment with a gasifying agent such as free oxygen-containing gas and water vapor under pressure, comprising a water-cooled reactor housing provided in its lower portion with gasifying agent inlet openings, a fuel distributor mounted on a vertical axis, a stirrer on a shaft disposed in the fuel bed in the upper portion of the reactor, and independent first and second drive means for independently rotating the fuel distributor and stirrer. Advantageously the distributor includes a hollow bearing shaft coaxial with the shaft of the stirrer and the stirrer shaft also has a bearing, a common bearing support cooperating with both of the bearings.

Reactor for gasifying solid fuels, particularly coal, under

Process for treating raw gas produced by the gasification of coal under elevated pressures and temperatures by a treatment with oxygen and steam and, if desired, additional gasifying agents such as carbon dioxide. The raw gas leaving the gas producer is cooled in a first condensing stage to a temperature which is in the range of 150.degree.-220.degree. C and 3.degree.-25.degree. C below the dew point temperature of the raw gas. The resulting condensate is withdrawn and the raw gas is conducted through at least one additional condensing stage. The condensate of the first condensing stage is treated independently of the condensate from the further stage or stages.

Process for treating raw gas produced by the pressure gasification of

A reactor for the pressure gasification of coal by treatment with oxygen and steam and, if desired, additional gasifying agents, at elevated temperatures and pressures, includes a water-cooled jacket and a rotary grate for moving the material to be gasified and for distributing the gasifying agents introduced into the reactor. The rotary grate is made of at least two concentric parts each of which rotates independly of the other part.

Reactor for the pressure gasification of coal

Gases produced by reacting fuels with oxygen containing gases and water vapor under pressure are desulfurized by scrubbing with a concentrated solution of one or more alkali salts of weak inorganic acids at a temperature near the atmospheric-pressure boiling point of the solution in a column while maintaining an exchange ratio of from 0.2 to 2.0 cubic meters of the concentrated solution per standard cubic meter hydrogen sulfide in the gas to be purified.

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Bad Homburg, Germany

Paul Rudolph