Abstract: The method of performing the Claus process includes the steps of connecting in parallel two combustion furnaces with waste heat boilers, further reacting, after the partial combusting in the combusion furnaces, in a single Claus reactor which is connected to both of the waste heat boilers of the combustion furnaces so as to receive partially combusted gas from the combustion furnaces, and partially combusting the reactant gas in only one of the combustion furnaces, when a hydrogen sulfide mass flow rate of the hydrogen sulfide fed with the reactant gas is below a certain threshold, and partially combusting of the reactant gas in both of the combustion furnaces, when the hydrogen sulfide mass flow rate of the hydrogen sulfide is greater than the threshold value. The production capacity of the single Claus reactor is designed for a maximum expected hydrogen sulfide mass flow rate in the inflowing reactant gas.

Abstract: A method of hot repair heating trains of a coke oven battery includes brick laying of a heating train, warming a finished portion of a respective heating train during the brick laying to a temperature of approximately 250.degree. C., directly after ending the brick laying heating a new heating train to a temperature of approximately 500.degree. C., performing the warming and heating by means of gaseous heat carrier, blowing the heat carrier into the heating trains and heating the heat carrier in a heat exchange with use of heat of hot parts of the coke oven battery.

Abstract: In a method of optimizing the operation of a distillation column with a side heating device for reconditioning of extract which is received during the extraction of hydrocarbon-containing initial products with N-substituted morpholines whose substituents have not more than seven C-atoms as selective solvents a liquid is withdrawn to a side heating device through a chimney plate arranged above a feed plate, so that between 5 and 30 volume percent of the liquid supplied to the chimney plate is not withdrawn to the side heating device but instead supplied directly to a plate located underneath the chimney plate. A vapor-liquid mixture which has escaped through a top from the side heating device is returned back to the distillation column. The returned vapor-liquid mixture is fed either to the feed plate or to the plate located underneath the chimney plate. An arrangement for performing the inventive method is also provided.

Abstract: A gas with a hydrogen content of at least 85 volume percent of partial oxidation crude gas is produced in a method including cooling of the gas after waste heat boiler of a gasifier by adding converted circulating gas in a quenching zone. The resulting gas mixture after corresponding gas treatment is subjected to a CO-conversion and then separated into a circulating gas partial stream and a product gas partial stream. The circulating gas partial stream is supplied back after a corresponding compression to the quenching zone, while the product gas partial stream after a so-called acid gas washing is subjected to a further gas treatment in correspondence with a desired use.

Abstract: The method of reducing a nitrogen oxides content of a flue gas generated on firing of a rich gas or combination coke oven having a plurality of heating walls forming dual heating flues, in which a single stage or multistage combustion takes place, and also having a plurality of regenerators for recovery of flue gas heat and preheating of an underfiring medium, includes the steps of mixing one portion of the flue gas drawn from one flue of the dual heating flues with the underfiring medium, gas and/or air, prior to or on admission to the other flue of the dual heating flues, or a regenerator connected with it, and circulating another portion of the flue gas additionally inside the dual heating flues.

Abstract: A pipe wall for hot reaction chambers comprises a plurality of pipes which together define a side to be heat loaded, and a plurality of holding elements arranged on the heat-loaded side for holding a temperature resistant coating. The pipes on the heat-loaded side together forming a substantially flat surface.

Abstract: A stripping column installation especially for separating starting materials with a high boiling point difference comprises a stripping column having a withdrawal plate and a column sump, and a circulating boiler connected with the stripping column and having a pipe bundle through which a sump product from the stripping column flows. The circulating boiler has an upper plate and a separating wall which separates a space above the upper plate into two chambers. One of the chambers has a connection for receiving the sump product from the stripping column, while the other of the chambers has a connection for discharging the sump product after heating in the boiler.

Abstract: The process for obtaining a p-xylene final product more than 98% pure from a crystalline starting material with a purity of about 98%, includes the steps of intermixing the starting material with precooled water and fed back recovered p-xylene in a mixer at a temperature of 0.degree. to 13.degree. C. to form a p-xylene-crystal-water mixture containing p-xylene crystals and water; continuously transferring the mixture produced as soon as it contains about 30% by weight p-xylene crystals into a purifying centrifuge via a dewatering filter to form a fluid phase and a p-xylene crystal slurry; separating the fluid phase further from the p-xylene crystals in a first stage of a purifying centrifuge, mixing the p-xylene crystal slurry in a second stage with a partial flow of final product, heating at about 13.degree. C.

Abstract: The column for distillation of charge products which form a heavier liquid phase and a lighter liquid phase and connected sump circulating boiler are provided with a liquid impermeable collecting bottom plate located in a lower part of the column. The bottom plate has a discharge passage and the column is provided with a liquid withdrawal outlet arranged closely underneath the collecting bottom plate but above the lower end of the discharge passage so that the heavier phase can be prevented from reaching the liquid withdrawal outlet by gravity. One pipe connects the sump circulating boiler with the liquid withdrawal outlet to provide a free flow of liquid from the column to the sump circulating boiler for heating and another pipe connects the column with the sump circulating boiler above the collecting bottom plate so that the reheated liquid can flow from the sump circulating boiler to the column without a circulating pump.

Abstract: A hydrocarbon material of the starting product is separated in an extractive distillation column in which an N-substituted morpholine whose substituents do not have more than seven carbon atoms is used as a selective solvent. The overhead product comes down as a top product of the extractive distillation and is fed through a coalescer in which the sump product comes down with a solvent content of 20 to 75% by weight at a temperature of 20.degree. to 70.degree. C. and subsequent to that is fed into a separating vessel. There it is separated into a heavier and lighter phase. After that the heavier phase is conducted into an extractive distillation column and the lighter phase into the overhead product distillation column.

Abstract: NO.sub.x -content in a flue gas during heating of coking oven with heating trains cooperating in pairs, high and low lying combustion stages, and flue gas return at a height of a heating train sole in a circulating stream, is reduced by adjusting a circulating stream rate defined by a volume stream of a returned flue gas divided by a flue gas volume stream without returned flue gas to between 20% and 50%, maintaining a stage ratio for a stage number greater than or equal to 2 defined as an air volume stream of a lower stage divided by a total air volume stream, at between 80/I% and 140/I% wherein I is a number of stages, arranging an upper combustion stage at a height of (45.+-.10%).times.(I-1) of the heating train height.

Abstract: In the method for the production of an aromate concentrate suitable for use as blending component for gasifier fuel, feed hydrocarbon mixtures having boiling ranges substantially between 40.degree. and 170.degree. C., are subjected, without any previous separation into individual fractions, to an extractive distillation employing N-substituted morpholine, substituents of which display no more than seven C-atoms, as selective solvent. Herewith, the lower boiling non-aromates with a boiling range up to about 105.degree. C., practically completely, and most of the higher boiling non-aromates with a boiling range between about 105.degree. and 160.degree. C., are recovered as raffinate, whereas the aromates, which are to be employed in whole or in part as blending component, come down in the extract of the extractive distillation.

Abstract: In accordance with a method of producing of methanol synthesis gas from a partial oxidation crude gas, the gas is cooled after a waste heat boiler of a gasifier by adding a converted circulating gas in a quenching zone. The resulting gas mixture is dedusted and then separated into a product gas partial stream and a circulating gas partial stream. The product gas partial stream is supplied after corresponding gas treatment to the synthesis reactor while the circulating gas partial stream is subjected to a CO-conversion and supplied back to the quenching zone.

Abstract: The cooling of a stream of hot product gas exiting from an outlet opening of a gasification reactor is made by way of two separate partial streams of cooling fluid such as a cooling gas, vapor or liquid. The first partial stream of the cooling fluid is fed from the outside substantially in a radial direction against an outer layer of the product gas stream. The second partial stream of cooling liquid is fed axially in a counter direction to the product gas stream to impinge against a central portion thereof. In this manner the path of mixing of the product gas with the cooling fluid is substantially shortened.

Abstract: A method of removing hydrosulfide from a crude gas produced by partial oxidation of carbon-containing material comprises the steps of treating a gas at a temperature between 10.degree. and 60.degree. C. with a suitable absorption solution, regenerating the absorption solution loaded durhg the treating, and cooling the crude gas which has been precleaned and pre-cooled to a temperature of 110.degree.-150.degree. C. before entering the absorption column, in a stepped manner in indirect heat exchange, the cooling including supplying the gas first through a reboiler of a desorption column and then through a heat exchanger which serves for preheating of the loaded absorption solution.

Abstract: The arrangement for cooling a hot product gas containing adhesive or fusible particles which lose their adhesiveness during cooling, has a reactor for producing the hot product gas, a cooling duct connected with the reactor for the hot product gas, a nozzle ring subdivided into a plurality of chambers mounted adjacent to and communicating with the cooling duct, each of the chambers being structured to introduce a different ring-shaped jet of cooling fluid into the hot product gas in the cooling duct. The different ring-shaped jets are producible with mass and penetration depths according to the mass of a product gas stream flowing in a cooling zone of the cooling duct with injection speeds selected to obtain a predetermined penetration depth. Using different penetration depths for the different ring-shaped jets allows avoidance of baked deposits on the walls of the reactor and cooling duct.

Abstract: The process removes acid components including sulfur oxides and nitrogen oxides from the exhaust gases of industrial furnaces and includes oxidizing the nitrogen oxide contained in the exhaust gases with the oxygen contained in the exhaust gases at a exhaust gases temperature between 300.degree. and 900.degree. C. before entry of the gases into a first absorption stage, with an addition to the exhaust gases of an organic compound, preferably methanol, as a radical former. After oxidation of nitrogen oxides the exhaust gases undergo a two-stage absorption using aqueous ammonium salt solutions as absorption liquid, whose pH-value is continuously adjusted to less than 5 by addition of aqueous ammonia solution. The mol ratio of NO.sub.2 to SO.sub.2 in the exhaust gases introduced to the second absorption stage is maintained between 0.01 and 0.5 by diverting a portion of the exhaust gases prior to the first absorption stage to the second absorption stage.

Abstract: An arrangement for gasification of fuels within the range from fine grain fuel to dust shaped fuels, in a dust cloud with gas comprises a gasification reactor provided with at least two burners, a supply container for accommodating a fuel, a distributor connected to the supply container for receiving the fuel from the supply container, and a plurality of conduits connected with the distributor and supplying the fuel from the latter to the burners, the conduits having a different geometrical parameter including at least one of a length and a direction.

Abstract: A method for cooling a hot product gas containing adhesive or fusible particles include injecting a ring-shaped jet of a cooling fluid into a gas to be cooled in a cooling zone in a flow direction of the gas, with separation of the jet into a plurality of individual cooling fluid jets with mass and penetration depths corresponding to the mass of product gas streams flowing through individual ring-shaped parts of the cooling zone. The injection speed of the cooling fluid jets are selected so as to obtain a desired penetration depth.

Abstract: This process is an improvement of a process described in German Open Patent Application No. 3703646 for obtaining a p-xylene product with a purity of at least 99.5%. The inert fluid used as a cold carrier is mixed with a crude product starting material, which has a high p-xylene content, in a mixing vessel under rotation to form a resultant mixture. Subsequently the resultant mixture is concentrated to a crystal content of from 30% to 70% and after that the p-xylene crystals are separated in a separator. The purity of the product p-xylene can be increased by heating these crystals in the separator.