US20140352207A1 - Process for dry cooling of coke with steam with subsequent use of the synthesis gas produced - Google Patents

Process for dry cooling of coke with steam with subsequent use of the synthesis gas produced Download PDF

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Publication number
US20140352207A1
US20140352207A1 US14/350,758 US201214350758A US2014352207A1 US 20140352207 A1 US20140352207 A1 US 20140352207A1 US 201214350758 A US201214350758 A US 201214350758A US 2014352207 A1 US2014352207 A1 US 2014352207A1
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Prior art keywords
coke
quenching
gas
steam
dry
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US14/350,758
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English (en)
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Holger Thielert
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ThyssenKrupp Industrial Solutions AG
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ThyssenKrupp Industrial Solutions AG
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Assigned to THYSSENKRUPP INDUSTRIAL SOLUTIONS AG reassignment THYSSENKRUPP INDUSTRIAL SOLUTIONS AG ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: THIELERT, HOLGER
Publication of US20140352207A1 publication Critical patent/US20140352207A1/en
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • 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
    • C10B39/00—Cooling or quenching coke
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • 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
    • C10B39/00—Cooling or quenching coke
    • C10B39/02—Dry cooling outside the oven
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/006—Reducing the tar content by steam reforming
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the invention relates to a method for the dry quenching of coke by means of steam with subsequent use of the synthesis gas generated, said method involving the cyclic coking of coal to coke with the coke being sent to a quenching device after being discharged from the coke oven and steam being introduced into the quenching device for dry quenching, thus creating synthesis gas made up of carbon monoxide (CO) and hydrogen (H 2 ) via a water-gas reaction, and the synthesis gas produced being fed to a further application.
  • This method allows the heat generated during coking to be used for the production of useful synthesis gas which, in turn, can be used for a further purpose or used in the heating process, thus on the whole achieving an extremely even energy balance throughout the entire process.
  • the coking process is performed cyclically, the cycles being charging, coking, discharging and quenching.
  • the coke is pushed out of the coke oven chamber at a temperature of approximately 1100° C. It is pushed out into a quenching car that collects the coke cake and transports it to a quenching device.
  • this is a wet quench tower, where the coke cake is sprayed with water which evaporates and cools the coke cake to a temperature below the kindling temperature of the coke so that it can be transported in the open air without posing a hazard.
  • the temperature of the coke is unevenly distributed in the coke cake but is usually less than 100° C.
  • DE19614482C1 gives one embodiment of a wet quench tower.
  • This teaching describes a plant for the wet quenching of hot coke in a process for the coking of coal using a coke sluice and a coke transfer chute that is located in a quench tower with a water feed device.
  • the chute fits onto a coke quenching car equipped at the bottom end with a coke discharge device and water discharge flaps.
  • the water feed system is located directly at the transfer chute and empties into the coke quenching car, which can be sealed watertightly, and said car is equipped with a control system which keeps the coke discharge flaps closed watertightly while the water is being fed in and opens the water discharge flaps once the water feed has been completed.
  • the gases are passed through the hot coke and collected or extracted until the coke has cooled to a temperature below its kindling temperature.
  • the hot gas is usually passed through a heat recovery unit in which steam is generated, thus recovering the thermal energy.
  • the steam can be used to drive auxiliary units or to generate electric power.
  • inert gases such as nitrogen or blast furnace gas, are often used.
  • WO9109094B1 describes a method for the dry quenching of coke in a quenching chamber with the aid of circulating quenching gas, said method allowing the velocity of the gas corning from the coke to be adjusted so that the grain size of the entrained coke dust particles is less than 3 mm and when the hot quenching gas enters the waste heat recovery boiler the grain size of the entrained coke dust is less than 1 mm, said method involving this gas being passed through a device that consists of a quenching chamber and an antechamber with a round cross section of about equal size and a cylindrical outer casing made of metal, and in particular the roof of the quenching chamber being in an inclined position so that it rises to the hot gas channel, thus increasing the cross section of the annular gas channel above the coke pile enough to allow the gas velocity of the hot quenching gas to be adjusted during quenching so that it remains virtually uniform across the length.
  • WO8602939A1 describes a method for dry coke quenching using quenching gas, said method involving the coke and the quenching gas being fed in countercurrent direction through a two-stage quencher, the first stage involving quenching to coke temperatures of approximately 800° C. and the quenching gas fed through the second quenching stage containing steam, the quenching gas loop thus being directly coupled with a thermal treatment step in which steam is added so that there is essentially no char burnout, which is achieved by the quenching in the first quenching stage taking place solely by indirect heat exchange between the coke and a coolant via heat exchanger walls and the quenching in the second stage being carried out solely by means of the steam-containing quenching gas.
  • State-of-the-art methods for dry coke quenching may include a variety of embodiments.
  • EP0317752A2 describes a method for improving the performance of coke dry quenchers which involves hot coke being broken up before entering the quenching shaft.
  • DE3030969A1 describes a method for the dry quenching of hot raw coke that is pushed out of the chambers of a coke oven battery and discharged in a quenching chamber, where it is quenched by means of direct or indirect contact, or both, with a quenching agent, and therefore the raw coke is preclassified into two or more size fractions before entering the quenching chamber and the individual size fractions are subjected to quenching in separate quenching chambers.
  • DE2435500A1 describes a method for preheating coking coal using superheated waste heat steam which is generated in a dry coke quencher by the coke releasing, at its highest temperature level, some of its heat to the walls of a steam jacket.
  • DE3217146A1 describes a device for dedusting the loop gas of a coke dry quencher in which the gas inlet channel and the gas outlet channel are located at right angles to each other, the gas outlet channel being directly connected, via a conical expansion, with the inlet opening of the waste heat recovery boiler integrated into the gas loop and a dust collection chamber with an inclined dust discharge area being positioned on the opposite side to the gas inlet channel.
  • the said methods and their embodiments have the disadvantage that during quenching the heat of the coke either cannot be recovered or the heat of the coke can only be inefficiently recovered as during quenching a large gas volume is generated and this needs to be passed through a heat recovery unit, making quenching technically difficult or economically inefficient. For this reason, it would be advantageous to utilise the heat that exists in the pushed coke via an endothermic chemical reaction that makes this energy available in chemical form.
  • GB347601A describes a method for the production of a gas mixture made up of nitrogen and hydrogen which is suitable for the synthesis of ammonia and which is produced in a coke quenching device in which the coke is sprayed with water and permeated by air and in which the carbon monoxide is directed into a plant section in which the carbon monoxide is converted into an equivalent of hydrogen via a subsequent conversion of the carbon monoxide using steam.
  • the steam for converting the carbon monoxide comes from the water that is sprayed into the coke cake in order to quench the coke.
  • the application does not describe quenching the coke cake with permeating gaseous steam.
  • the objective is to provide a method that cyclically carbonises coal and uses gaseous steam (H 2 O) to dry quench hot coke after a coking cycle, with the steam (H 2 O) thus reacting at least partially with the coke to form hydrogen (H 2 ) and carbon monoxide (CO) according to the water-gas equilibrium, the hydrogen (H 2 ) obtained being collected and the gas mixture thus obtained being used for a further purpose. In this way synthesis gas is obtained.
  • gaseous steam H 2 O
  • CO carbon monoxide
  • coke quenching using steam takes place in a quenching device that is preferably designed as a quenching shaft.
  • the coke cake is taken to, or tipped onto, a quenching car, which transports the coke cake to the quenching device.
  • the coke cake is sealed off from the surrounding atmosphere and gaseous steam is passed through it.
  • gaseous steam is passed through it.
  • this is done in a vertically upward gas flow direction so that the specifically heavier steam is displaced by the lighter hydrogen during the quenching process.
  • the steam may be a gas mixture in any state and even be in a mixture with other gases, but it is preferably used in pure form.
  • the synthesis gas generated may also contain impurities, but if the reaction is carried out correctly, it consists mainly of the constituents hydrogen (H 2 ) and carbon monoxide (CO).
  • the steam is preferably generated in a steam boiler.
  • Said steam is kept hot through suitable possibilities for intermediate storage and is then fed into the coke quenching device under pressure using a metering device.
  • the feed pipes can, in an advantageous embodiment, be heated.
  • hydrogen (H 2 ) and carbon monoxide (CO) are produced.
  • the gaseous steam used is dry, i.e. there are no adhering water droplets or mist.
  • the synthesis gas generated and the hydrogen contained therein can be used for any further purpose.
  • use of this gas mixture for a further purpose involves it being added to the fuel gas of the coke oven(s).
  • the coke oven is heated with the gas generated during quenching of the coke.
  • the hydrogen used to heat the coke oven can be mixed with a hydrocarbonaceous fuel gas before being fed to the coke oven.
  • the fuel gas is natural gas.
  • the fuel gas is coke oven gas. It is also possible to use blast furnace gas from a blast furnace process as the fuel gas instead of a hydrocarbonaceous fuel gas.
  • the synthesis gas is subjected to a heat recovery process before being used for a further purpose or being fed to the coke oven for heating purposes. This may, for example, be achieved by passing the gas through a waste heat recovery boiler.
  • steam is generated during the heat recovery process.
  • the steam is then used to generate mechanical energy by driving a turbine. This can, in turn, be used to generate electric power. It is also possible to direct the synthesis gas generated through a heat exchanger in which the steam used for quenching is preheated in countercurrent direction.
  • a water-gas shift reaction is carried out to convert the carbon monoxide (CO) into carbon dioxide (CO 2 ) after the coke has been quenched with steam (H 2 O).
  • CO carbon monoxide
  • CO 2 carbon dioxide
  • This gas mixture mainly consists of hydrogen (H 2 ) and carbon dioxide (CO 2 ) and can be easily converted into pure hydrogen, for example by means of pressure-swing adsorption.
  • the steam required for this can be added in excess to the quenching process or added to the synthesis gas already generated. It may also be sprayed in as liquid water after the coke has been quenched.
  • use for a further purpose relates to a conversion of the carbon monoxide with steam and subsequent purification of the hydrogen obtained during the conversion in a pressure-swing adsorption unit.
  • the hydrogen can then be used, for example, in a chemical process in a subsequent application.
  • Pressure-swing adsorption units for the purification of hydrogen from hydrogenous gases are well-known in the state of the art.
  • WO2006066892A1 teaches one example of a method for purifying hydrogen by means of pressure-swing adsorption.
  • the steam is split into at least two part streams for quenching.
  • a part stream of the steam is introduced into the coke quenching device from below in a vertically upward flow direction and a further part stream of the steam is fed into a part of the shaft in which the coke to be quenched has a temperature of 500 to 900° C. This may, for example, be done via feed nozzles installed in the side of the shaft that inject the steam directly into the coke.
  • the coke quenching device is a coke quenching shaft.
  • the coke quenching device is a coke quenching chamber.
  • this may, for example, be equipped with an antechamber.
  • the quenching device or the subsequent transfer line for the hydrogen may also be equipped with a dedusting device. This allows the dust to be reduced if a dust-laden coal is used or large amounts of dust are created during quenching.
  • the coke oven battery or coke oven bank may be of any design and configured in any way.
  • the coke oven battery from which the coke comes and which is heated by the synthesis gas may, for example, be a coke oven battery in which the coking gas is collected and processed.
  • the coke oven bank from which the coke comes may, for example, be a “heat-recovery”-type coke oven battery.
  • the coke oven bank from which the coke comes may also be a “nonrecovery”-type coke oven battery.
  • Even the coke ovens that are located in a coke oven battery or bank may ultimately be of any design as long as they are suitable for the production of coke and for being heated by synthesis gas when appropriate.
  • the coke pushing may also be carried out at a different coke oven battery or bank from that to which the synthesis gas obtained during quenching is fed, but this is not usual practice.
  • auxiliary equipment such as storage tanks for liquids or gases, pumps, valves, heating or quenching equipment, knock-out drums or meters for measuring temperatures or concentrations of gas constituents may be used at any point in the method according to the invention.
  • the invention has the advantage of utilising the thermal energy of the coke after coking by means of an endothermic chemical reaction and so the thermal energy of the hot coke can be utilised much better than in prior-art methods. Furthermore, the invention has the advantage of providing hydrogen as a useful product without the addition of further energy, thus allowing the energy balance of the overall method to be improved. The environmental compatibility of this method can thus be considerably improved.
  • FIG. 1 shows a coke oven which serves to carbonise coal. It depicts the coke oven chamber ( 1 ) with the coal cake ( 2 ), the coke oven chamber doors ( 3 ), the primary heating space ( 4 ) above the coke cake ( 2 ) and the secondary heating space ( 5 ) below the coke cake ( 2 ).
  • the quenching car ( 6 ) which collects the coke cake ( 2 ) for quenching, is parked in front of the coke oven chamber ( 1 ). Said quenching car ( 6 ) is brought in front of the coke quenching chamber ( 7 ) and the coke cake ( 2 ) is emptied into the coke quenching chamber ( 7 ) via a feed flap ( 7 a ).
  • Said flap ( 7 a ) is closed once the coke quenching chamber ( 7 ) has been filled.
  • Steam ( 8 , H 2 O) then flows into the coke quenching chamber ( 7 ) from below and reacts with the hot coke cake ( 5 a ) according to the water-gas equilibrium to form hydrogen and carbon monoxide ( 9 , H 2 and CO) as synthesis gas.
  • the steam ( 8 ) is generated via a steam boiler ( 10 ) with a downstream metering device ( 10 a ).
  • the synthesis gas ( 9 ) generated during quenching is extracted in an upwards direction and, following dedusting in a dedusting unit ( 11 ), it is directed into the secondary heating space ( 5 ) of the coke oven ( 1 ) as fuel gas ( 9 a ). This is done via a heat exchanger ( 12 ), which, in countercurrent direction, preheats the steam ( 8 ) fed in to quench the coke ( 2 ).
  • a heat exchanger ( 12 ) which, in countercurrent direction, preheats the steam ( 8 ) fed in to quench the coke ( 2 ).
  • it is added to the partially combusted coking gas which has already flowed into the secondary heating space ( 5 ) from the primary heating space ( 4 ) and combusted. As a result, it contributes to the heating of the coke cake ( 2 ) through the floor of the coke oven chamber ( 1 ).
  • the fully combusted coking gas is exported out of the secondary heating space ( 5 ) as waste gas ( 13 ) and sent to a gas scrubbing device ( 14 ).
  • the cleaned waste gas ( 14 a ) is exported from the gas scrubbing device ( 13 ) and sent to a heat recovery unit ( 15 ).
  • a generator ( 15 a ) that generates electric power is driven via a turbine.
  • the cooled waste gas ( 15 b ) is exported via a flue ( 16 ).
  • the quenched coke ( 5 a ) or the coke to be quenched ( 5 a ) is discharged via a discharge flap ( 7 b ) and sent for final quenching.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Coke Industry (AREA)
  • Industrial Gases (AREA)
US14/350,758 2011-10-12 2012-09-22 Process for dry cooling of coke with steam with subsequent use of the synthesis gas produced Abandoned US20140352207A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102011115698A DE102011115698A1 (de) 2011-10-12 2011-10-12 Verfahren zur trockenen Kühlung von Koks mit Wasserdampf mit anschliessender Verwendung des erzeugten Synthesegases
DE102011115698.8 2011-10-12
PCT/EP2012/003969 WO2013053427A1 (de) 2011-10-12 2012-09-22 Verfahren zur trockenen kühlung von koks mit wasserdampf mit anschliessender verwendung des erzeugten synthesegases

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US20140352207A1 true US20140352207A1 (en) 2014-12-04

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US (1) US20140352207A1 (de)
EP (1) EP2766453A1 (de)
AR (1) AR088302A1 (de)
DE (1) DE102011115698A1 (de)
RU (1) RU2605125C2 (de)
TW (1) TW201335353A (de)
WO (1) WO2013053427A1 (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20140251784A1 (en) * 2011-10-12 2014-09-11 Thyssenkrup Industrial Solutions Ag Process for dry cooling of coke with carbon dioxide with subsequent use of the carbon monoxide produced

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CN103881735B (zh) * 2014-01-03 2016-03-30 科利特环能科技（大连）有限公司 防止红焦烧损及回收焦炭热能的熄焦工艺
CN104673333B (zh) * 2015-02-03 2017-10-10 天津大学 熄焦及回收能量的方法与装置
CN105754618B (zh) * 2016-03-30 2018-09-28 沈阳环境科学研究院 一种气相化学还原法熄焦工艺方法
CN106479542B (zh) * 2016-10-27 2019-08-20 武汉钢铁有限公司 基于干法熄焦及炼焦煤除湿的水煤气制备工艺
CN111019680A (zh) * 2019-12-10 2020-04-17 上海交通大学 一种促进煤炭焦化及提高煤气产量与品质的方法

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US4037330A (en) * 1975-06-13 1977-07-26 Waagner-Biro Aktiengesellschaft Method and means for dry cooling bulk materials
US4211607A (en) * 1977-03-01 1980-07-08 Ananievsky Mikhail G Dry coke quenching process
US4422858A (en) * 1980-08-27 1983-12-27 Firma Carl Still Gmbh & Co. Kg Coke gasification method
US4529483A (en) * 1982-09-23 1985-07-16 Hartung, Kuhn & Co. Maschinenfabrik Gmbh Process for utilizing waste heat and producing water gas during the cooling of coke
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DE102009022509A1 (de) * 2009-05-25 2010-12-09 Uhde Gmbh Verfahren zur Herstellung von Synthesegas

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GB347601A (en) 1930-01-28 1931-04-28 Daniel Tyrer Improvements in and relating to the cooling of coke and obtaining a nitrogen hydrogen mixture
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