Metallgesellschaft Aktiengesellschaft

Ruhrgas Aktiengesellschaft

Carl Hafke

Gerhard Baron

Herbert Bierbach

Rudolf Kohlen

Paul Rudolph

Rainer Reimert

Hans Kupfer

Gunter Pockrandt

Eberhard Blaum

Martin Hirsch

Lothar Reh

Michael Karl Eichelsbacher

Wolfgang Schafer

Karlheinz Zolzer

Dietrich Engler

Roland Weber

Rudolph Kohlen

The fuel constitutes a fixed bed in the reactor, which is provided in its lower portion with a rotating grate, which is adapted to be speed-controlled. The gasifying agents consisting of oxygen, steam and/or carbon dioxide are introduced through the rotating grate into the fixed bed. Under the action of the rotating grate the incombustible mineral constituents are delivered as solid ash to a lock chamber container. The speed of the rotating grate is controlled in dependence on the temperature in the lock chamber container. The speed will be decreased when the temperature in the lock chamber container exceeds a desired value, and increased when the temperature is too low. The desired temperature in the lock chamber container is taken into account as a range, which varies with time. The speed can be controlled by hand or can be automatically controlled with the aid of a computer. The rate at which oxygen as a gasifying agent is supplied to the reactor is also taken into account in the speed control.

Method of operating a reactor for gasifying solid fuels

A process for the gasification of carbonaceous agglomerates in a reactor at a pressure of the range of 5 to 150 bar. The agglomerates are fed into said reactor from a storage zone located above the reactor and form a fixed bed in the reactor, in which they slowly descend when gasified. At least two gasification agents selected from the group consisting of oxygen, air, steam and carbon dioxide are introduced into said reactor through the bottom and rise through said fixed bed. Solid ash or liquid slag is discharged below said fixed bed and a steam-containing product gas is tapped from the reactor above said fixed bed. In order to minimize or prevent the condensation of steam on the agglomerates in the storage zone, the invention provides for a controlled atmosphere almost entirely free of oxygen and steam which is introduced into the storage zone at a pressure approximately equal to the pressure of the product gas.

Process for the gasification of carbonaceous agglomerates in a fixed bed

A process of gasifying fine-grained solid fuels for the production of a product gas that contains hydrogen, carbon oxides and methane comprises a treatment with steam, oxygen and/or carbon dioxide in two interconnected gasifying stages under a pressure in the range from 2 to 150 bars and at temperatures of 500.degree. to 1500.degree. C. In the first gasifying stage, the fuel is gasified in a circulating fluidized bed by a treatment with gasifying stage. The residual solids which become available in the first gasifying stage are fed to the second gasifying stage and are virtually completely gasified therein, except for residual ash, by a treatment with a gasifying agent which includes oxygen. At least one-half of the product gas from the second gasifying stage is fed to the first gasifying stage and used as fluidizing fluid therein.

Process of gasifying fine-grained solid fuels

A process of producing a gas of high calorific value and low dust content comprising contacting coal with water vapor and free oxygen at a pressure of about 5 to 150 bars and a temperature sufficient to produce a gas containing hydrogen and carbon monoxide, containing at least about 10 grams of dust per standard cubic meter and having a temperature of about 350.degree. to 800.degree. C., subjecting the gas to a coarse purification to reduce the solids content thereof, then scrubbing the gas at about 200.degree. to 300.degree. C. with a liquid predominantly comprising hydrocarbons and including less than about 5% of water by weight, and withdrawing a purified gas substantially free of solids and having an enhanced calorific value. In accordance with preferred features, the coarse purification stage includes at least one cyclone separator, the gas leaves the coarse purification stage at a temperature above about 350.degree. C. and is cooled by spraying with water to below 350.degree. C. before entering the intense scrubbing stage.

Producing pure gas of high calorific value from gasification of solid

In the production of gas from a solid fuel comprising effecting gasification by contacting the solid fuel with oxygen and water under pressure to form raw gas containing tar, solids and water, cooling the raw gas to effect condensation of the tar and water, the condensate containing the solids, separating from the solids-containing condensate a fraction enriched in solids, and disposing of said fraction, the improvement which comprises effecting said disposition by feeding at least part of said fraction to a solids disintegrator wherein the solids are reduced in size, and recycling at least part of the condensate containing disintegrated solids to the gasification step. Disintegration serves to reduce substantially all the particles to below about 2 mm with the predominant part below about 0.5 mm. Part of the condensate may also be recycled to the separation stage and all the recycled condensate is kept above 50.degree. C. to prevent solidification of tars. The process permits continuous operation of a gasification plant without clogging of pipes and pumps such as otherwise necessitate equipment shutdown for cleaning.

Treating condensate 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

A process and apparatus for the continuous gasification of fuels, which are mainly in lump form. The fuels are subjected to a superatmospheric pressure in a fixed bed treatment with a gasifying agent consisting of gases which contain free oxygen and water vapor and/or carbon dioxide in a water-cooled reactor housing. The housing contains a substantially conical rotary grate, which is rotatably mounted in the lower portion of the reactor housing and serves to discharge the gasifying agent into the reactor shaft and permits the removal of gasification residue from the shaft. The gasifying agent is positively distributed in correspondence with the quantity of fuel, which increases in the radial direction of the shaft resulting in an approximately uniform time of contact between the gas and fuel across the entire shaft area.

Process and apparatus for a pressure gasification of fuels mainly in

A process is disclosed for purifying raw gas produced by the gasification of solid fuels under superatmospheric pressure by treatment with gasifying agents containing water vapor and free oxygen. The raw gas contains dust and hydrocarbons and is at a temperature of 400.degree.-700.degree. C as it leaves the gas producer. The raw gas is purified by spraying in at least two scrubbing stages with virtually dustfree, highly dispersed scrubbing water at temperatures of 160.degree.-300.degree. C. In this manner, the gas is cooled to a temperature that is 0.degree.-20 C above the scrubbing water temperature and is saturated with water vapor in the scrubbing stages. Thereafter, the gas is subjected to centrifugal force to increase the relative velocity between gas and water droplets. The scrubbing water which contains dust and tar is withdrawn from each scrubbing stage. For the first scrubbing stage a cyclone-type scrubber can be used and for the second scrubbing stage a radial flow-type scrubber or a Venturi-type scrubber can be used.

Process for purifying raw gas from the gasification of solid fuels

In the production of a gas having a high calorific value and containing more than about 50% methane by volume by a process comprising gasifying a solid fuel under a pressure of about 5 - 150 bars by a treatment with oxygen and water vapor to produce a water vapor-containing raw gas at a temperature of about 350.degree.- 700.degree. C, the improvement which comprises further reacting the water vapor-containing raw gas under a pressure of about 5 - 150 bars with oxygen in a succeeding reactor to produce an intermediate product gas which contains mainly hydrogen, carbon dioxides, and methane and which leaves the reactor at a temperature between about 600.degree. and 950.degree. C, cooling the intermediate product gas and freeing the intermediate product gas from sulfur compounds. A dust fuel and/or liquid hydrocarbon can be added to the raw gas as such or after prereaction with oxygen, the addition advantageously taking place in the succeeding reactor. The reactor may contain a granular bed of a catalyst such as nickel, cobalt or chromium oxide and/or sulfide, and/or a contact material or catalyst support such as an oxide, spinel or silicate of aluminum and/or magnesium. The bed can be fluidized or otherwise mechanically moved.

Process of producing gases having a high calorific value

In a process of gasifying solid fuel such as coal comprising the steps of contacting the solid fuel under a pressure of at least about 5 bars in a reaction chamber surrounded by a water-cooled zone, the reaction heat evaporating water in said zone, transferring the water vapor from said zone to the reaction chamber, removing product gas from the reaction chamber, scrubbing and cooling said product gas in a scrubber-cooler, and periodically interrupting normal gasification, the improvement which comprises discontinuing the transfer of water vapor to the reaction chamber during such periods of other than normal gasification and instead transferring the water vapor to said scrubber-cooler, whereby generation of product gas will be discontinued during such periods. Hot steam may be supplied to the water-cooled zone during said periods of interruption to delay a drop in the temperature of the fuel in the reactor chamber so that upon resumption of normal operation the initially produced gas wll be of substantially normal composition.

Process of gasifying solid fuels, particularly coal

In the production of a synthesis gas comprising carbon monoxide and hydrogen, by a process comprising gasifying a solid fuel under a pressure of about 5-150 bars by a treatment with oxygen and water vapor to produce a water vapor-containing raw gas at a temperature of about 350.degree.-700.degree. C, the improvement which comprises further reacting the water vapor-containing raw gas under a pressure of about 5-150 bars with oxygen in a succeeding reactor to produce an intermediate product gas which leaves the reactor at a temperature between about 800.degree. C and 1400.degree. C, cooling the intermediate product gas, and freeing the intermediate product gas from sulfur compounds. A dust fuel and/or liquid hydrocarbon can be added to the raw gas as such or after prereaction with oxygen, the addition advantageously taking place in the succeeding reactor. The reactor may contain a granular bed of a catalyst such as nickel, cobalt or chromium oxide and/or sulfide, and/or a contact material or catalyst support such as an oxide, spinel or silicate of aluminum and/or magnesium. The bed can be fluidized or otherwise mechanically moved. The resulting gas is suited for use as a starting material in a methanol, ammonia, oxo or Fischer-Tropsch synthesis.

Process for producing synthesis gases

A device for feeding granular and dust coal to a coal-gasifying reactor which operates under a pressure of 5 to 150 bars. A stationary housing is connected to the coal inlet of the reactor and a lock chamber member is rotatedly mounted therein. The lock chamber member is movable between coal-receiving position and a coal-discharging position. The lock chamber member has at least one chamber which is open only at one end and contains a displacing device which extends approximately to the entrance of the chamber. The displacing device substantially prevents an ingress of product gas into the chamber when in the discharge position.

Feeder for coal-gasification reactor

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

Particulate solids are fed into a pressure reactor operated under a pressure of 5-150 bars by means of a guide cylinder which is secured to the reactor and surrounds the reactor inlet. The guide cylinder is adapted to be closed and a stationary feed conduit is directed towards the guide cylinder. A cylinder container, which is gastightly guided in the guide cylinder and has a bottom which is adapted to be closed, is moved up and down in the guide cylinder and when the bottom of the cylinder is open and the reactor inlet is closed the material flows out of the container into the guide cylinder whereas the bottom of the container is closed and the same is moved toward the open reactor inlet to displace gases into the reactor. The device for carrying out the process includes a guide cylinder secured to the reactor and surrounding the reactor inlet. The guide cylinder is adapted to be closed. A stationary feed conduit is directed towards the guide cylinder and a container is gastightly guided in the guide cylinder and is movable up and down therein and has a bottom that is adapted to be closed.

Growing community of inventors

Frankfurt-am-Main, Germany

Carl Hafke