A method for using waste heat from a cement producing plant, wherein heat of a process gas is used through a heat exchanger, which comprises a sequence of cyclones, for heating raw mix. A cement producing plant having at least one calcinator and at least one heat exchanger, which comprises a series of cyclones for heating raw mix. The process gas is removed at the outlet of the calcinator and/or at the gas-side outlet of the first cyclone in the heat exchanger in the direction of gas flow and, once the heat has been removed in a steam vessel, the cooled process gas is fed back into the second cyclone or third cyclone in the heat exchanger in the direction of gas flow. The heat taken from the process can be used for the further heating of unrecovered heat which can thereby be more efficiently converted into electrical energy.

The present invention provides a fluidized calciner which can perform sufficient calcination by reducing a rate of unburned fuel at an outlet of the fluidized calciner while preventing occlusion in a preheater. In the present invention, plural pulverized coal blowing lines (3), raw material chute (4) of cement raw material, and first to fourth air introduction pipes (5a to 5d) are connected to a bottom side wall of a tubular furnace body (2) whose upper end portion is closed by a top plate (2b); a fluidizing air blowing port (2a) adapted to blow in fluidizing air is disposed at a bottom of the furnace body (2); an exhaust gas duct (6) is connected to a top side wall of the furnace body located above the first and/or second air introduction pipes (5a, 5b) by being spaced away from the top plate (2b); and blowing ports (3a) of the pulverized coal blowing lines are disposed below suction ports of respective air introduction pipes (5a to 5d) but above the fluidizing air blowing port (2a), and at least one of the blowing ports (3a) is placed below the third or fourth air introduction pipe (5c or 5d).

Method and installation for calcining cement raw meal in a calciner whereby fuel and a calciner oxidant having an oxygen content of at least 30% vol are introduced into the calciner so as to generate either an oxidant-lean zone or a fuel-lean zone in the calciner located between the lowermost fuel inlet level and the lowermost oxidant inlet level of the calciner, between 50% and 100% by weight of the raw meal being supplied to the calciner upstream of and/or within the oxidant-lean, respectively the fuel-lean zone.

Apparatus for the production of carbon dioxide from limestone includes a nuclear energy source (32) arranged to generate electricity and a rotary kiln (10). The rotary kiln (10) has an inlet (15) for the introduction of limestone and an outlet (19) for the release of carbon dioxide. An electrical resistance heating element (21) disposed within the kiln (10) is arranged to be supplied with electricity derived from the nuclear energy source (32) to raise the temperature of the element (21) for transfer of heat to the interior of the rotary kiln (10). Limestone in the rotary kiln (10) is thereby heated to a temperature sufficient for the release of carbon dioxide.

Apparatus for the production of carbon dioxide from limestone includes a nuclear energy source (32) arranged to generate electricity and a rotary kiln (10). The rotary kiln (10) has an inlet (15) for the introduction of limestone and an outlet (19) for the release of carbon dioxide. An electrical resistance heating element (21) disposed within the kiln (10) is arranged to be supplied with electricity derived from the nuclear energy source (32) to raise the temperature of the element (21) for transfer of heat to the interior of the rotary kiln (10). Limestone in the rotary kiln (10) is thereby heated to a temperature sufficient for the release of carbon dioxide.

A method for the thermal treatment of dispersible raw material may inovlve introducing raw material into a riser tube that is perfused by hot gases and thermally treating the raw material with the hot gases. Furthermore, the method may inovle feeding a fuel to the riser tube. The fuel may initially dwell in a fuel-conditioning region on a bearing face, where the fuel comes into contact with a part of the hot gas that is mixed with the raw material. Consequently, the fuel is dried and/or at least partially de-gassed and/or at least partially reacted and subsequently transferred into the riser tube.

A method for the thermal treatment of dispersible raw material may inovlve introducing raw material into a riser tube that is perfused by hot gases and thermally treating the raw material with the hot gases. Furthermore, the method may inovle feeding a fuel to the riser tube. The fuel may initially dwell in a fuel-conditioning region on a bearing face, where the fuel comes into contact with a part of the hot gas that is mixed with the raw material. Consequently, the fuel is dried and/or at least partially de-gassed and/or at least partially reacted and subsequently transferred into the riser tube.

A horizontal pyrolysis furnace has a kiln and two barrels. The two barrels are respectively a processing barrel rotatably disposed in the kiln and a takeover barrel detachably connected with the processing barrel. Each one of the two barrels has a gate assembly and at least one spiral guiding plate. The gate assembly of the processing barrel is mounted on an end of the processing barrel, and extends out from the kiln. The two gate assemblies of the two barrels are detachably connected such that the two barrels are able to rotate synchronously. The at least one spiral guiding plate is fixed on an inner surface of one of the two barrels, and the spiral guiding plates of both barrels have an identical helical direction.

A bypass system may be utilized in installations and methods for producing cement clinker. A portion of a kiln offgas produced in a kiln may be branched off as bypass gas via a bypass line connected between the kiln and a calciner. In some cases 3 to 15% of the kiln offgas is branched off as the bypass gas. The bypass gas may be cooled to a temperature in a range from 300 to 550° C. and dedusted in a temperature range from 300 to 550° C. The dedusted bypass gas may then be recirculated to the calciner and/or into a tertiary air line arranged between the cooler and the calciner and/or into a region between the kiln and the calciner.

Provided is a system for continuous processing of heavy fuel oil from recycling waste oil and the processing residues of crude oil into useful products including means for feeding waste oil; at least one hot-gas filter, at least one condenser, at least one rotating kiln including an outer stationary jacket which forms a heating channel, and an inner rotating reactor, and means for removing solid coke from the rotating reactor. The at least one hot gas filter is configured to separate a naphtha/gasoil fraction after the processing of the heavy fuel oil from a soft coke fraction. The rotating reactor is configured to recover a solid coke fraction comprising high contaminant content. The invention further relates to a process for continuous processing of heavy fuel oil from recycling waste oil and the processing residues of crude oil into useful products, preferably with the system of the invention. Moreover, the invention relates to use of the products and waste products produced with the process and system of the invention.