US3884620A - Process and apparatus for continuously heating fine-grained coal - Google Patents

Process and apparatus for continuously heating fine-grained coal Download PDF

Info

Publication number
US3884620A
US3884620A US405233A US40523373A US3884620A US 3884620 A US3884620 A US 3884620A US 405233 A US405233 A US 405233A US 40523373 A US40523373 A US 40523373A US 3884620 A US3884620 A US 3884620A
Authority
US
United States
Prior art keywords
coal
heat exchange
fluidized
bed
zone
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US405233A
Other languages
English (en)
Inventor
Roland Rammler
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
GEA Group AG
Original Assignee
Metallgesellschaft AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Metallgesellschaft AG filed Critical Metallgesellschaft AG
Application granted granted Critical
Publication of US3884620A publication Critical patent/US3884620A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
    • F26B17/10—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers
    • F26B17/101—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers the drying enclosure having the shape of one or a plurality of shafts or ducts, e.g. with substantially straight and vertical axis
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • C10B57/10—Drying

Definitions

  • Apparatus for carrying out the process of the invention includes a plurality of heat exchange [56] References Cited cyclones for preheating the coal positioned on UNITED STATES PATENTS different levels, a fluidized bed heater positioned below the heat exchange cyclones and means to gz gj Ga transfer exhaust gas from the fluidized bed heater to 3 790 334 2/1974 Cohen ::::::::::::::::III:I: 432/58 the heat exchange cyclones- A dust collector is also included for collecting fine dust from the
  • coal is heated in a pneumatic elevator tube, in which heat is supplied to the coal as it is pneumatically conveyed. That concept has proved highly satisfactory for a treatment at relatively low temperatures and has been embodied in numerous forms of suspended-particle dryers for coal and many other materials. It has also been proposed to degasify coal by a blow-coking process, which involves an internal combustion in the presence of the coal.
  • German Pat. No. 1,l60,823 describes a process of degasifying non-caking coal, in which the coal is predried and in a suspended-particle dryer is heated in a plurality of series-connected cyclones. The coal and the heat-carrying conveying gas are moved in mutually opposite directions in each stage.
  • This process has also the disadvantage that the treating temperature is subjected to substantial fluctuations and the resulting fin ished product is not uniformly degasified.
  • a process in which the disadvantage is alleviated has been described in DOS 1,671,320.
  • the alteration compared to the prior process resides mainly in that the preceding suspendedparticle dryer is replaced by a separate system of cyclones, which will be referred to hereinafter as heat exchange cyclones.
  • the SUMMARY first heat exchange cyclone and flows from the same to one or more heat exchange cyclones which are disposed on a lower level or on successively lower levels, the temperature of the material being raised in said cyclones, the material is then heated to the end temperature in a fluidized-bed heater, and the exhaust gas from the fluidized-bed heater is supplied as a hot conveying gas into the heat exchange cyclones.
  • the residence times of the material being heated in the fluidized bed amount to a few minutes (e.g. 2 or 3 minutes) to about half an hour (30 minutes) and in most cases to between 5 minutes and 20 minutes.
  • the advantages of the heat exchange cyclones are utilized for the initial heating. Because these heat exchangers are operated in a counterflow mode in stages, the exhaust gas therefrom is at low temperatures so that the heat is utilized to a high degree. Besides, the material is rapidly heated in these heat exchangers so that the residence times are short and a small structural expenditure is sufficient.
  • the advantages residing in the extremely rapid temperature equalization taking place within a fluidized-bed heater are utilized according to the invention. This ensures a uniform heating of the material being treated without an occurrence of local temperature differences. At the same time,- higher gas inlet temperatures than in other processes are permissible even if a heat-sensitive feed such as caking coal is to be heated. Because the residence time of the material to be heated amounts to between a few minutes and about half an hour, it is ensured that the coarser particle size fractions which may not have been fully heated through in the heat exchange cyclones are heated to the same temperature as the finer fractions.
  • the relatively long residence times in the fluidized bed have the result that the fluidized-bed heater contains a considerable amount of material to be heated so that the overall system has a certain desired thermal inertia as far its response to inevitable fluctuations of the operating conditions is concerned. For this reason, the uniformity as regards locus and particle size function is accompanied by a stability of the heating as regards time.
  • the heating system according to the invention comprising a fluidized-bed heater as a final stage affords at the same time the advantage that the fluidized-bed heater has such a high storage capacity that there is no need in many cases for an intermediate bin for receiving the heated material because the same can be directly supplied from the fluidized-bed heater to the consuming station, e. g., the mixing station of a plant for making shaped coke bodies.
  • Fine coal is usually wet. Other materials too are free of moisture only in exceptional cases. For this reason it will be desirable in most cases to provide a dryer which precedes the heating system according to the invention unless drying can be accomplished in a desirable manner in the uppermost heat exchange cyclone. This will be particularly useful if a feed which is free of tar or oil is to be heated to temperature above 500 600 C.
  • a suspendedparticle dryer is preferable to other kinds of dryers.
  • the suspended-particle dryer may have a dryer tube which is longer than could be required for drying and combines drying and conveying functions so that it can be combined with the heating system according to the invention in a very simple manner and without an interposition of mechanical conveyors.
  • the exhaust gases from the fluidized-bed heater are approximately at the end temperature of the treatment in the fluidized bed in a development of the invention these exhaust gases are used as a conveying gas and heat carrier in the heat exchange cyclones. If the feed has a low resistance to abrasion, the gases may entrain a relatively large amount of dust from the fluidized bed. In that case it will be desirable to provide a cyclone which is associated with the fluidized-bed heater and collects dust from the exhaust gases leaving the fluidized-bed heater before they flow through the more elevated heat exchange cyclones. Depending on requirements, the solids collected in this dust-collecting cyclone may be supplied to the fluidized-bed heateror may be admixed to the fine-grained product withdrawn from the fluidized-bed heater, or may be separately withdrawn.
  • This example demonstrates the heating of moist, fine-grained coking coal to 320 C. so as to produce a preheated caking component for the continuous production of shaped coke bodies.
  • the fine-grained caking coal feed has a moisture content of 9 percent and is at the ambient temperature as it is fed from the supply bin 1 into the suspendedparticle dryer 2.
  • the dryer 2 consists of a circulating dryer provided with a sifting hood 3 and a coarse particle-recirculating conduit 3a, which incorprates a hammer mill 4.
  • the dryer 2 is fed with hot combustion gas from a combustion chamber 5, which is fed with air L and gaseous fuel G.
  • the combustion chamber is operated under a slightly superatmospheric pressure and the ratio of fuel gas to air in said chamber is exactly controlled so as to minimize the contents of free oxygen in the combustion gas. Cooled gas from the conduit 18 is recycled to adjust the gas at the outlet of the combustion chamber 5 to a temperature of570 C.
  • the gas is cooled to 140 C.; at the same time, the entrained coal is heated to approximately C. and dried to a residual water content of 1 percent.
  • the coal is separated in the coal-collecting cyclone 6 from the vaporleaving the dryer and is then immediately supplied to further heating means described below.
  • the coalcollecting cyclone 6 is elevated and there is no need for a further conveyor to move the coal to the feeder for the uppermost heat exchange cyclone 9.
  • the drying gases from which the coal has been removed are sucked by the blower 7 and are forced into the electrostatic precipitator 8, in which more dust is collected.
  • the dry coal is conducted from the collecting cyclone 6 through the discharge conduit 6a thereof into the conduit 10a, in which the coal is entrained by hot conveying gases flowing to the heat exchange cyclone 9.
  • the coal enters the conduit 10b, in which it is entrained by gases which are hotter than those in the conduit 10a and flow into the second heat exchange cyclone 10, in which the coal is heated further.
  • the coal is finally supplied through the conduit 11a to the fluidized-bed heater 11, in which it is heated to its end temperature of 320 C. during a residence time of 12 minutes. At this temperature the coal is with drawn as a finished product through the conduit 20 and is directly supplied to a consuming station.
  • the fluidized-bed heater has such a high storage capacity that there is no need for an intermediate bin.
  • the fluidized-bed heater 11 is heated with combustion gases from the combustion chamber 12, which like the combustion chamber 5 is operated with a gas-air ratio which is exactly controlled to ensure that the combustion gases contain only traces of free oxygen. This is important because otherwise the caking capacity of the coal could be substantially reduced by oxidation.
  • Gas at 140 C. is recirculated to adjust the temperature of the gases entering the fluidized-bed heater 11 to 460 C.
  • the recirculated gas is branched by the 'conduits 18 from the exhaust gas stream of the system be hind the electrostatic precipitator and is pressurized by the blower 13 to the required pressure.
  • the remaining exhaust gas is discharged into the open via line 19.
  • the fluidizing gas leaves the heater at about 320 C. and flows through insulated tubes 17 into the more elevated cyclones.
  • the gas flows first through the collecting cyclone 14, in which entrained dust is collected. Depending on the requirements, this dust is recycled through the conduit 15 into the fluidized-bed heater or is conducted through conduit 16 and admixed to the coarser particles which have been withdrawn from the fluidized bed heater.
  • the gas When dust has been collected in the cyclone 14 from the gas withdrawn from the fluidized-bed heater, the gas is supplied by the conduits 10b and 10a, respectively, to the heat exchange cyclones l0 and 9 in succession. In said cyclones, the gas is cooled to 140 C. as it transfers heat to the oppositely moving coal which has been supplied through conduits 9a and 6a. At a temperature of 140 C. the gas together with the vapor from the dryer enters the electrostatic precipitator 8, in which dust is collected. The dust collectes in the precipitators is added in the present example to the finished product through the conduit 21.
  • the dryer 2 will be omitted if the feed has only a very low moisture content.
  • this requirement need not be fulfilled, e. g., when it is desired to heat fine coal for a subsequent dry distillation or coking.
  • the combustion chamber 12 preceeding the fluidized-bed haater 11 may be omitted and the heater may be operated with cold or preheated air whereas the heat required for the process is produced directly by a partial combustion of coke and volatile constituents in the fluidized-bed heater.
  • a fluidized-bed heater in which an internal combustion is carried out may also be used to heat an incombustible feed.
  • This technology is known per se and is described in German Pat. No. 1,758,244. It calls for a supply of fuel and air through mixing nozzles provided in the bottom of the fluidized-bed heater to produce combustion gases near the nozzles, and for the use of these combustion gases as a fluidizing gas.
  • the electrostatic precipitator shown on the drawing must be replaced by a condenser.
  • Process for continuously heating fine-grained coal to a controlled, uniform end temperature by direct contact with hot gases which comprises conveying the coal to be heated to elevated cyclonic zone and subsequently to one or more cyclonic heat exchange zones disposed on a lower level or on successively lower levels, the temperature of the coal being raised in said heat exchange zones, thereafter heating the coal to said end temperature in a fluidized-bed heating zone, the exhaust gas from the fluidized-bed heating zone being supplied to a separate cyclonic collecting zone where dust is collected from the exhaust gas, said gas being then passed as a hot conveying gas through said one or more heat exchange zones, said dust collected in the collecting zone being withdrawn or recycled to the fluidized bed zone.
  • Apparatus for heating fine-grained coal to a controlled, uniform end temperature by direct contact with hot gases which comprises means to convey coal to be heated to elevated cyclone means, a plurality of cyclonic heat exchange means for preheating the coal po sitioned on different levels below said elevated cyclone means, fluidized bed means as a final heating stage, means to supply said bed with fluidizing gas, means for transferring exhaust gas from the fluidized-bed means into the heat exchange means including cyclonic collecting means between the fluidized bed means and the lowermost cyclonic heat exchange means for collecting dust from said exhaust gas and withdrawing or recycling the collected dust to the fluidized bed means, and dust collecting means for collecting fine dust from the exhaust gas leaving the uppermost heat exchange means.
  • said fluidized-bed means includes means for carrying out an internal com- UNITED STATES PATENT OFFICE CERTIFICATE OF CORRECTION Patent No. 5, 8 I-,62O v Dated May 975 lnventofls) Roland Rammler It is certified that error appears in the above-identified patent and that said Letters Patent are hereby corrected as shown below:

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Coke Industry (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
US405233A 1972-11-17 1973-10-10 Process and apparatus for continuously heating fine-grained coal Expired - Lifetime US3884620A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE2256385A DE2256385B2 (de) 1972-11-17 1972-11-17 Verfahren zum kontinuierlichen Erhitzen feinkörniger Feststoffe

Publications (1)

Publication Number Publication Date
US3884620A true US3884620A (en) 1975-05-20

Family

ID=5861987

Family Applications (1)

Application Number Title Priority Date Filing Date
US405233A Expired - Lifetime US3884620A (en) 1972-11-17 1973-10-10 Process and apparatus for continuously heating fine-grained coal

Country Status (8)

Country Link
US (1) US3884620A (enExample)
JP (1) JPS4981274A (enExample)
AU (1) AU475650B2 (enExample)
CA (1) CA995617A (enExample)
DE (1) DE2256385B2 (enExample)
FR (1) FR2207592A5 (enExample)
GB (1) GB1437245A (enExample)
IT (1) IT1001767B (enExample)

Cited By (30)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3998583A (en) * 1974-08-21 1976-12-21 Klockner-Humboldt-Deutz Aktiengesellschaft Apparatus for thermal treatment of moist raw material
US4047883A (en) * 1974-07-24 1977-09-13 Commonwealth Scientific And Industrial Research Organization Thermal treatment of materials by hot particulates
US4060458A (en) * 1975-12-24 1977-11-29 Coaltek Associates Separation of gas from solids
US4082498A (en) * 1975-03-12 1978-04-04 Buttner-Schilde-Haas Aktiengesellschaft System for drying and heating particulate coal
US4101264A (en) * 1975-11-20 1978-07-18 Barr & Murphy Limited Drying apparatus and method
US4174946A (en) * 1976-09-09 1979-11-20 Bergwerksverband Gmbh Process for drying coal in two-stage flow-through circulation heaters
US4240877A (en) * 1978-05-02 1980-12-23 Firma Carl Still Gmbh & Co. Kg Method for preheating coal for coking
US4280283A (en) * 1978-12-02 1981-07-28 Klockner-Humboldt-Deutz Ag Method and device for the operation of a hot gas generator within a dryer
US4298340A (en) * 1978-04-07 1981-11-03 Klockner-Humboldt-Deutz Ag Method and apparatus for producing a hydraulic binder
US4321032A (en) * 1979-09-26 1982-03-23 Charbonnages De France Process for the treatment of combustible granular and/or pulverulent material by drying and/or heating, and an installation for carrying out the process
US4445976A (en) * 1981-10-13 1984-05-01 Tosco Corporation Method of entrained flow drying
US4468288A (en) * 1981-03-19 1984-08-28 Didier Engineering Gmbh Method of preheating coal and supplying preheated coal to a coke oven
US4616575A (en) * 1984-10-25 1986-10-14 Krupp Polysius Ag Method and apparatus for the heat treatment of fine-grained material
US4659456A (en) * 1983-07-01 1987-04-21 Metallgesellschaft Ag Process of drying and heating oil-containing solids
US4736692A (en) * 1985-06-20 1988-04-12 Asea Stal Aktiebolag Method of handling fuel
US5122190A (en) * 1990-07-13 1992-06-16 Southdown, Inc. Method for producing a hydraulic binder
EP1306636A1 (de) * 2001-10-02 2003-05-02 Fritz Dr.-Ing. Schoppe Verfahren und Vorrichtung zur gleichmässigen Erhitzung eines Staubkörnergemisches in einer Strömung heisser Gase
US20060231466A1 (en) * 2002-12-23 2006-10-19 Dirk Nuber Method and apparatus for heat treatment in a fluidized bed
US20060249100A1 (en) * 2002-12-23 2006-11-09 Jochen Freytag Method and plant for the conveyance of fine-grained solids
US20060263292A1 (en) * 2002-12-23 2006-11-23 Martin Hirsch Process and plant for producing metal oxide from metal compounds
US20060266636A1 (en) * 2002-12-23 2006-11-30 Michael Stroder Treatment of granular solids in an annular fluidized bed with microwaves
US20060278566A1 (en) * 2002-12-23 2006-12-14 Andreas Orth Method and plant for producing low-temperature coke
US20070137435A1 (en) * 2002-12-23 2007-06-21 Andreas Orth Method and plant for the heat treatment of solids containing iron oxide using a fluidized bed reactor
US20080124253A1 (en) * 2004-08-31 2008-05-29 Achim Schmidt Fluidized-Bed Reactor For The Thermal Treatment Of Fluidizable Substances In A Microwave-Heated Fluidized Bed
US20090305180A1 (en) * 2005-11-04 2009-12-10 Polysius Ag Plant and method for the production of cement clinker
US7632334B2 (en) 2002-12-23 2009-12-15 Outotec Oyj Method and plant for the heat treatment of solids containing iron oxide
US7651547B2 (en) 2002-12-23 2010-01-26 Outotec Oyj Fluidized bed method and plant for the heat treatment of solids containing titanium
US20100281878A1 (en) * 2007-06-13 2010-11-11 Wormser Energy Solutions, Inc. Mild gasification combined-cycle powerplant
CN101974344A (zh) * 2010-11-12 2011-02-16 中冶焦耐(大连)工程技术有限公司 一种利用焦炉烟道气进行煤调湿的干燥工艺及装置
CN101726167B (zh) * 2008-10-21 2011-11-23 神华集团有限责任公司 一种烟气半闭路循环褐煤直管式气流干燥方法

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4052199A (en) * 1975-07-21 1977-10-04 The Carborundum Company Gas injection method
CA2800166C (en) 2009-05-22 2018-08-21 The University Of Wyoming Research Corporation Efficient low rank coal gasification, combustion, and processing systems and methods
CN102021006B (zh) * 2009-09-22 2014-01-08 山东省冶金设计院股份有限公司 从炼焦煤中去除水分的工艺
CN109135787A (zh) * 2018-10-26 2019-01-04 郑州鼎力新能源技术有限公司 煤炭干燥、干馏提质方法及设备
CN110846060A (zh) * 2019-12-14 2020-02-28 陕西煤业化工技术研究院有限责任公司 一种粉煤热解与焦粉燃烧发电耦合系统及方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2113774A (en) * 1934-11-26 1938-04-12 Schmalfeldt Hans Process for the gasification of dust or fine-grained fuels with circulating gas
US2763478A (en) * 1949-08-22 1956-09-18 Vernon F Parry Apparatus for drying solids in a fluidized bed
US3790334A (en) * 1972-05-22 1974-02-05 Fuller Co Manufacture of lightweight aggregate

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2393766A (en) * 1942-11-28 1946-01-29 Comb Eng Co Inc Drying apparatus
US2658862A (en) * 1950-06-09 1953-11-10 Reilly Tar & Chem Corp Process for the defluidization and fixed-bed coking of a preheated fluidized coal
DE1571650B2 (de) * 1966-01-31 1973-08-09 Institut für Energetik, 7024 Leipzig Verfahren und vorrichtung zur zweistufigen verkokung von steinkohle
DE1671320A1 (de) * 1967-04-21 1971-09-02 Kloeckner Humboldt Deutz Ag Verfahren und Vorrichtung zur kontinuierlichen,thermischen Behandlung,wie Entgasen und/oder Verkoken,von feinkoernigen,wasserhaltigen Brennstoffen

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2113774A (en) * 1934-11-26 1938-04-12 Schmalfeldt Hans Process for the gasification of dust or fine-grained fuels with circulating gas
US2763478A (en) * 1949-08-22 1956-09-18 Vernon F Parry Apparatus for drying solids in a fluidized bed
US3790334A (en) * 1972-05-22 1974-02-05 Fuller Co Manufacture of lightweight aggregate

Cited By (44)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4047883A (en) * 1974-07-24 1977-09-13 Commonwealth Scientific And Industrial Research Organization Thermal treatment of materials by hot particulates
US3998583A (en) * 1974-08-21 1976-12-21 Klockner-Humboldt-Deutz Aktiengesellschaft Apparatus for thermal treatment of moist raw material
US4082498A (en) * 1975-03-12 1978-04-04 Buttner-Schilde-Haas Aktiengesellschaft System for drying and heating particulate coal
US4101264A (en) * 1975-11-20 1978-07-18 Barr & Murphy Limited Drying apparatus and method
US4060458A (en) * 1975-12-24 1977-11-29 Coaltek Associates Separation of gas from solids
US4174946A (en) * 1976-09-09 1979-11-20 Bergwerksverband Gmbh Process for drying coal in two-stage flow-through circulation heaters
US4298340A (en) * 1978-04-07 1981-11-03 Klockner-Humboldt-Deutz Ag Method and apparatus for producing a hydraulic binder
US4240877A (en) * 1978-05-02 1980-12-23 Firma Carl Still Gmbh & Co. Kg Method for preheating coal for coking
US4280283A (en) * 1978-12-02 1981-07-28 Klockner-Humboldt-Deutz Ag Method and device for the operation of a hot gas generator within a dryer
US4321032A (en) * 1979-09-26 1982-03-23 Charbonnages De France Process for the treatment of combustible granular and/or pulverulent material by drying and/or heating, and an installation for carrying out the process
US4468288A (en) * 1981-03-19 1984-08-28 Didier Engineering Gmbh Method of preheating coal and supplying preheated coal to a coke oven
US4445976A (en) * 1981-10-13 1984-05-01 Tosco Corporation Method of entrained flow drying
US4659456A (en) * 1983-07-01 1987-04-21 Metallgesellschaft Ag Process of drying and heating oil-containing solids
US4616575A (en) * 1984-10-25 1986-10-14 Krupp Polysius Ag Method and apparatus for the heat treatment of fine-grained material
US4736692A (en) * 1985-06-20 1988-04-12 Asea Stal Aktiebolag Method of handling fuel
US5122190A (en) * 1990-07-13 1992-06-16 Southdown, Inc. Method for producing a hydraulic binder
EP1306636A1 (de) * 2001-10-02 2003-05-02 Fritz Dr.-Ing. Schoppe Verfahren und Vorrichtung zur gleichmässigen Erhitzung eines Staubkörnergemisches in einer Strömung heisser Gase
US20070137435A1 (en) * 2002-12-23 2007-06-21 Andreas Orth Method and plant for the heat treatment of solids containing iron oxide using a fluidized bed reactor
US20100040512A1 (en) * 2002-12-23 2010-02-18 Outotec Oyj Method and plant for the heat treatment of solids containing iron oxide
US20060263292A1 (en) * 2002-12-23 2006-11-23 Martin Hirsch Process and plant for producing metal oxide from metal compounds
US20060266636A1 (en) * 2002-12-23 2006-11-30 Michael Stroder Treatment of granular solids in an annular fluidized bed with microwaves
US20060278566A1 (en) * 2002-12-23 2006-12-14 Andreas Orth Method and plant for producing low-temperature coke
US20060231466A1 (en) * 2002-12-23 2006-10-19 Dirk Nuber Method and apparatus for heat treatment in a fluidized bed
US8048380B2 (en) 2002-12-23 2011-11-01 Outotec Oyj Process and plant for producing metal oxide from metal compounds
US20090274589A1 (en) * 2002-12-23 2009-11-05 Outotec Oyj Process and plant for producing metal oxide from metal compounds
US7625422B2 (en) * 2002-12-23 2009-12-01 Outotec Oyj Method and plant for the heat treatment of solids containing iron oxide using a fluidized bed reactor
US8025836B2 (en) 2002-12-23 2011-09-27 Outotec Oyi Method and plant for the heat treatment of solids containing iron oxide
US7632334B2 (en) 2002-12-23 2009-12-15 Outotec Oyj Method and plant for the heat treatment of solids containing iron oxide
US7651547B2 (en) 2002-12-23 2010-01-26 Outotec Oyj Fluidized bed method and plant for the heat treatment of solids containing titanium
US7662351B2 (en) 2002-12-23 2010-02-16 Outotec Oyj Process and plant for producing metal oxide from metal compounds
US20060249100A1 (en) * 2002-12-23 2006-11-09 Jochen Freytag Method and plant for the conveyance of fine-grained solids
US20100074805A1 (en) * 2002-12-23 2010-03-25 Outotec Oyj Fluidized bed method for the heat treatment of solids containing titanium
US7803268B2 (en) 2002-12-23 2010-09-28 Outotec Oyj Method and plant for producing low-temperature coke
US8021600B2 (en) 2002-12-23 2011-09-20 Outotec Oyj Method and plant for the heat treatment of solids containing iron oxide
US7854608B2 (en) * 2002-12-23 2010-12-21 Outotec Oyj Method and apparatus for heat treatment in a fluidized bed
US7878156B2 (en) 2002-12-23 2011-02-01 Outotec Oyj Method and plant for the conveyance of fine-grained solids
US8021601B2 (en) 2002-12-23 2011-09-20 Outotec Oyj Plant for the heat treatment of solids containing titanium
US20080124253A1 (en) * 2004-08-31 2008-05-29 Achim Schmidt Fluidized-Bed Reactor For The Thermal Treatment Of Fluidizable Substances In A Microwave-Heated Fluidized Bed
US20090305180A1 (en) * 2005-11-04 2009-12-10 Polysius Ag Plant and method for the production of cement clinker
US9709331B2 (en) * 2005-11-04 2017-07-18 Thyssenkrupp Polysius Aktiengesellschaft Plant and method for the production of cement clinker
US20100281878A1 (en) * 2007-06-13 2010-11-11 Wormser Energy Solutions, Inc. Mild gasification combined-cycle powerplant
CN101726167B (zh) * 2008-10-21 2011-11-23 神华集团有限责任公司 一种烟气半闭路循环褐煤直管式气流干燥方法
CN101974344A (zh) * 2010-11-12 2011-02-16 中冶焦耐(大连)工程技术有限公司 一种利用焦炉烟道气进行煤调湿的干燥工艺及装置
CN101974344B (zh) * 2010-11-12 2013-08-07 中冶焦耐(大连)工程技术有限公司 一种利用焦炉烟道气进行煤调湿的干燥工艺及装置

Also Published As

Publication number Publication date
IT1001767B (it) 1976-04-30
FR2207592A5 (enExample) 1974-06-14
JPS4981274A (enExample) 1974-08-06
GB1437245A (en) 1976-05-26
CA995617A (en) 1976-08-24
AU6104773A (en) 1975-04-10
DE2256385B2 (de) 1981-04-16
DE2256385A1 (de) 1974-05-22
AU475650B2 (en) 1976-08-26

Similar Documents

Publication Publication Date Title
US3884620A (en) Process and apparatus for continuously heating fine-grained coal
US3565408A (en) Production of alumina from aluminum hydroxide
CN108753368B (zh) 一种循环流化床煤气化系统及方法
US2763478A (en) Apparatus for drying solids in a fluidized bed
JPH02290406A (ja) 循環流動層反応器における固体炭質材料のガス化または燃焼用装置
US4529579A (en) Method for producing anhydrous alumina
UA48201C2 (uk) Спосіб одержання окису алюмінію із гідроокису алюмінію
US3705086A (en) Coal carbonizing in trickling streams
KR890000861B1 (ko) 시멘트 클링커 제조방법
CN109982775B (zh) 用于流化床反应器中热处理的方法和设备
CN107723012B (zh) 多级流化床粉煤热解及除尘耦合制取煤焦油煤气的系统及方法
US3020227A (en) Process and apparatus for heating solid inert heat-carrying bodies
NO134875B (enExample)
JPS61132551A (ja) 白色セメントのクリンカ−を製造する方法およびその装置
US3823073A (en) Calcining coke in vertical kiln
US3427008A (en) Installation and method for the treatment at high temperature and cooling of granular or divided solid products utilizing a fluidized layer
US4292064A (en) Glass batch feeding using a fluidized bed for predrying agglomerates
US4345914A (en) Method of heating fine-grained solids
US4563264A (en) Method of dry distillation of volatile substances from mineral matter containing same
US2773018A (en) Continuous process for drying, preheating, and devolatilization of carbonaceous materials
US4318798A (en) Process of cooling hot granular solids
US2924556A (en) Heat processing of fine-granular coal products
US3836435A (en) Method of heat treatment of coal
US3974572A (en) Process and heat exchanger for continuous circulation of fluidized powder in heat exchange with a hot gas
CN105176547B (zh) 一种煤快速热解工艺