Other

Bergwerksverband Gmbh

Foster Wheeler Energy Corporation

Uhde Gmbh

Deutsche Babcock Aktiengesellschaft

Bergwerksvergand Gmbh

Grochowski, Horst

Horst Grochowski

Karl K Knoblauch

Jurgen Schwarte

Harald Juntgen

Horst Lichtenberger

Ekkehard Richter

Rolf Noack

Stefan Gramelt

Klaus Goldschmidt

Ludwig Muhlhaus

Manfred Koch

Rolf Lambach

Dieter Zurawsky

A fluid treatment system having bulk beds. The fluid to be treated essentially streams from the bottom up through a bulk bed, while the bulk material migrates through the bulk beds in countercurrent to the fluid essentially from the top down. This is accomplished by removing partial quantities of bulk material at the lower end of the bulk bed, and delivering partial quantities of the bulk material to the bulk bed at the top. At least one charging wagon provided with optionally sealable bulk material outlets is able to traverse a charging channel between a charging position and several partial bulk bed release positions above the bulk beds. Provided below the bulk material outlets and the bulk material valve of the charging wagon are bulk material through pipes, the bulk material outlet mouths of which end on bulk material cones of an underlying bulk bed.

Fluid treatment system with bulk material beds operated in parallel and method for operating such a system

A method for purifying waste gases of an at least partially burnt solid fuel to reduce pollutants such as SOand/or HCl and NO. The waste gas flows into a moving bed reactor from below through a lower and upper layer of an adsorption and/or absorption agent already polluted with NO, SOand/or HCl. SOand/or HCl components are adsorbed from the waste gas into the NOloaded adsorption and/or absorption agent. Thereafter, the waste gas is mixed with an ammonium-containing compound and flows through an upper horizontal gas inflow and bulk material removal tray of the moving bed reactor into the upper layer of the adsorption and/or absorption agent already polluted with NOand small quantities of SOand/or HCl. During the throughflow of the upper layer, NOcomponents are adsorbed from the waste gas onto the adsorption/absorption agent.

Method and device for purifying the flue gases of a sintering process of ores and/or other material-containing materials in metal production

The invention is directed to a method for cleaning exhaust gases of a glass melting process. The raw material for production of the glass is charged to the glass furnace and molten glass is removed from the glass furnace. The exhaust gases of the glass melting process are freed of the pollutant components in a moving bed reactor system on a catalytically active adsorbent and/or absorbent. Catalyst damaging pollutant components are bound by absorption and the particulate components are adhesively removed. Catalytic removal of nitrogen is performed in the layer area adjacent to the immediate oncoming flow area of the catalyst damaging pollutant components. Other pollutant components that do not damage the catalyst, such as dioxins and furans, are removed by absorption in the layer area.

Method for purifying waste gases of a glass melting process, particularly for glasses for LCD display

The invention relates to a process for cleaning exhaust gases produced by a sintering process of metal-containing waste. The sintering exhaust gas includes one or more harmful substances which are eliminated in at least two steps by at least one adsorption and/or absorption agent in a single moving bed in a moving bed reactor system. The moving bed includes a particle layer (stage I) disposed above a flow input area and below an adsorption layer (stage II) of the moving bed. One or more harmful substances in the sintering exhaust gas are absorptively or adsorptively bound to potassium and/or sodium compounds and the harmful substances are trapped by adhesion in the flow input area or the Particle layer (stage I) of the moving bed. The substantial removal of NOand the adsorptive or absorptive removal of dioxins and furans takes place in the adsorption layer (stage II) in the moving bed.

Method for cleaning exhaust gases produced by a sintering process for ores and/or other metal-containing materials in metal production

The fluid treatment installation, in particular for cleaning gases on a bulk material in countercurrent with respect to the movement of the bulk material, is characterized in that adjacent bulk material beds are interconnected by a shared horizontal charging channel and a bulk material delivery container can be moved through the charging channel between a charging position and several bulk material portion delivery positions above the bulk material beds. Several bulk material beds can be interconnected by a shared horizontal discharge channel, where a bulk material reception container can be moved through the discharge channel between the bulk material portion exchange positions (bulk material portion reception positions) and at least one bulk material delivery position below the bulk material beds.

Method for treating fluids on bulk material

To achieve better distribution of the fluid and optimal flow of bulk products, the feed inlet floor of a mobile bed reactor comprises parallel cellular bulk feed hoppers (9A) covering the surfaces or funnel shaped bulk discharge chutes (9B), the side walls (14A and 14B) of which are provided with openings (16A and 16B) for the passage of feed fluid above which roof-shaped feed distribution elements (18A; 18B; 18C) opening downward are arranged on the inner surface of the hoppers or chutes so as to project from the said surface. For flat, parallel flow of the bulk product, it is particularly advantageous that the distribution elements are arranged so that they also lie, in the direction of flow of the product, above the outlet openings (26A and 26B) for the latter in the hoppers or chutes and therefore preferably cover the entire surface region of the opening in the form of a roof. This type of feed inlet floor is advantageously used, amongst others, by adding to the intake fluid in the region of the said floor, another fluid component, for fluid treatment purposes, which then initiates a desired reaction in the region of fluid treatment and/or by extracting the bulk product from the reactor in cycles and in quantities corresponding to the contaminated layer of the product in the region of fluid treatment, and/or by using as intake fluid a gas or gaseous mixture the dew point of which is not attained at least in the lower horizontal region of fluid treatment. This non-attainment of the dew point is judiciously achieved by means of the feed inlet floor and makes it possible to carry out the fluid treatment in two phases, namely a first wet phase and a second dry phase.

Feed inlet floor for mobile bed reactors

A process and device for the treatment of fluid, such as flue gas. A moving bed reactor has several reaction chambers. The reaction chambers are located in parallel flow locations. A solid bulk material is located in the reaction chambers. The fluid flows through the reaction chambers in parallel, from bottom to top of each reaction chamber. As the fluid flows through the reaction chambers, the fluid interacts with the bulk material to alter the fluid. Specifically, the bulk material absorbs and/or acts as a catalyst to remove impurities from the fluid. Flow through each of the reaction chambers can be interrupted without interruption of flow through the other reaction chambers. Some of the bulk material in each reaction chamber can be removed, as a layer, from the bottom and a replacement amount can be added, as a layer to the top.

Process and device for treating fluids by means of a pourable solid by

Fluidized bed reactor arrangement

Sulphur is manufactured out of sulphur dioxide containing gases by dividing the feed gas in two flows of gas having a volume ratio of 2 to 1 and reducing the greater flow of gas on a carbon containing substance like anthracite, thereby obtaining hydrogen sulfide which is mixed with the smaller flow of gas, the mixture being converted in a Claus process to sulphur.

Method of manufacturing sulphur from SO.sub.2 containing gases

This invention relates to a process for the desorption of spent solid adsorbent through heating the latter to desorption temperature by means of a hot granular heat carrier medium; particularly of activated coal or activated coke used for flue gas purification by adsorption in power plants, for example.

Process for the desorption of spent solid absorbent

SO.sub.2 -containing gas is made to contact a carbon-containing material to reduce the gas to a gas mixture containing sulfur and also containing H.sub.2 S and SO.sub.2 in a volume ratio of 2:1. The sulfur is then removed by condensation and the remaining gas mixture subjected to a Claus-process treatment to obtain additional sulfur from it.

Method of producing sulfur from SO.sub.2 -containing gases

Sulfur oxides and nitrogen oxides are removed from exhaust gases containing additionally oxygen and steam, by the addition of gaseous ammonia at temperatures between about 110.degree. and 180.degree. C. The exhaust gases travel in the interior of a reactor across a travelling bed which goes from above to below, composed of granulated, carbon-containing adsorbent with or without catalysts. In the first travelling bed initially a large portion of the sulfur oxides is adsorptively removed. In the second travelling bed after dosed addition of gaseous ammonia the nitrogen oxides are catalytically reduced to nitrogen as well as further sulfur oxides being separated. The improvement involves extending the path of the exhaust gases between the first and the second travelling beds and introducing into the volume of the exhaust gas stream between the travelling beds a forced mixture of dosed added ammonia with the exhaust gas departing from the first travelling bed.

Method for the removal of sulfur oxides and nitrogen oxides from exhaust

A reaction vessel for regenerating particulate adsorbents has a bottom outlet and top inlets for admission of the adsorbent to be regenerated by being heated to a regeneration temperature, and for a particulate regenerating material at a temperature above the regeneration temperature. The mixture of the adsorbent with the regenerating material forms a bed in the reaction vessel and is continuously withdrawn through the outlet so that the bed descends toward the latter and is replenished from above under the formation of a cone at the upper region of the bed. A plurality of tubular baffles coaxially surrounds the inlets which are also coaxial with one another, each of the tubular baffles penetrating into the bed in the region of the cone and retards the flow of the particles of the mixture down the slope of the cone in that the particles must pass underneath the baffle to flow to the next baffle. The bed may be confined between a plurality of axially overlapping spaced tubular guide baffles located in the interior of the reaction vessel with a spacing therefrom. At least one partition may be provided between one of the guide baffles and the vessel, subdividing the chamber between the vessel and the guide baffles into two compartments from which gases which develop during the regeneration of the adsorbent are separately exhausted.

Arrangement for regenerating particulate adsorbents

A charged adsorbent is accommodated in a desorbing vessel and in an intermediate container which communicates with the desorbing vessel. The charged adsorbent is desorbed in the desorbing vessel by contacting the same with a heat carrier, such as with hot sand, and a desorption gas which develops during the desorption of the charged adsorbent in the desorbing vessel is passed through the charged adsorbent accommodated in the intermediate container to capture at least one component of the desorption gas in the charged adsorbent present in the intermediate container. The purified desorption gas is withdrawn from the intermediate container, and the regenerated adsorbent is gradually discharged from the desorbing vessel and the supply of the adsorbent in the desorbing vessel is replenished by charged adsorbent from the intermediate container. The desorption gas is cooled during the passage thereof through the charged adsorbent present in the intermediate container. The magnitude of the temperature reduction of the desorption gas may be controlled by controlling the rate at which the desorption gas is discharged from the intermediate container, such as by resorting to the use of an adjustable vane. The adsorbent in the intermediate container may be confined by gas-permeable walls through which the desorption gas enters and leaves the adsorbent present in the intermediate container.

Method of regenerating adsorbents

A method and apparatus for separating undesirable components from a waste gas by adsorption of the components onto a granular adsorbent. The gas is caused to flow serially through two distinct side-by-side layers of adsorbent both moving parallel to one another in a direction perpendicular to the direction of gas flow. The adsorbent material is so controlled that the particles of the second layer to be contacted by the gas are less loaded with impurities than the particles of the first layer. In one embodiment, this result is achieved by moving the second layer faster than the first layer.

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Oberhausen, Germany

Horst Grochowski