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WO2025012017A1 - Installation de trempe à sec de coke et procédé de trempe à sec de coke et de traitement de gaz - Google Patents

Installation de trempe à sec de coke et procédé de trempe à sec de coke et de traitement de gaz Download PDF

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Publication number
WO2025012017A1
WO2025012017A1 PCT/EP2024/068557 EP2024068557W WO2025012017A1 WO 2025012017 A1 WO2025012017 A1 WO 2025012017A1 EP 2024068557 W EP2024068557 W EP 2024068557W WO 2025012017 A1 WO2025012017 A1 WO 2025012017A1
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WO
WIPO (PCT)
Prior art keywords
gas
conduct
unit
dry quenching
coke dry
Prior art date
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Pending
Application number
PCT/EP2024/068557
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English (en)
Inventor
Andrea Fabbri
Riccardo Calcagno
Matteo Giovannini
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Paul Wurth SA
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Paul Wurth SA
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Publication date
Application filed by Paul Wurth SA filed Critical Paul Wurth SA
Publication of WO2025012017A1 publication Critical patent/WO2025012017A1/fr
Pending legal-status Critical Current
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Classifications

    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases

Definitions

  • coal is subjected in a coke oven (battery) to temperatures of approximately 1400°C to 1000°C, whereby said coal is subjected a dry distillation procedure (or also "carbonization").
  • a dry distillation procedure or also "carbonization"
  • the coke is transferred to a coke quenching plant.
  • the most common quenching techniques are based on coke water/wet quenching (CWQ) or coke dry quenching (CDQ).
  • coke dry quenching permits that the hot coke is quenched from approximately 1100 °C down to 180 °C.
  • Coke dry quenching is considered advantageous because it produces relatively dry coke with a relatively small amount of moisture, which is considered particularly advantageous in cases coke is to be fired within a blast furnace plant.
  • a further advantage is a significantly lower water consumption in comparison to coke water quenching processes.
  • gas mixture usually comprises considerable varying amounts of hydrogen (H2) and carbon monoxide (CO).
  • H2 hydrogen
  • CO carbon monoxide
  • this gas mixture will be generally referred to as “gas” or “excess gas”.
  • This gas is also sometimes referred to as "lower bleeder gas”.
  • it is necessary to allow a continuous gas extraction from the cooling gas ducts of a coke dry quenching plant. This may be achieved, for example, via a chimney that guides the gas towards the atmosphere.
  • the present invention proposes, in a first aspect, a coke dry quenching plant for quenching coke and for treating an off-gas therefrom, wherein the coke dry quenching plant comprises: a cooling chamber (configured) for cooling hot coke down to a predefined temperature; an off-gas conduct (configured) for conducting the off-gas from an off-gas outlet of the cooling chamber to a heat recovery apparatus; a first dedusting unit (configured) for dedusting the off-gas, wherein the first dedusting unit is arranged in the off-gas conduct downstream of the cooling chamber and upstream of the heat recovery apparatus, the heat recovery apparatus being configured for cooling the off-gas down to a predefined first temperature range; and a first fan unit is arranged downstream of the heat recovery apparatus.
  • the coke dry quenching plant further comprises a sub-economizer unit configured to cool the off-gas down to a predefined second temperature range and arranged downstream of the first fan unit, wherein the sub-economizer unit is connected to (an inlet of) the cooling chamber via a process cooling gas conduct for providing process cooling gas to the cooling chamber and wherein the sub-economizer unit is connected to a regenerative thermal oxidizer via an excess gas conduct for providing excess gas to the regenerative thermal oxidizer, and wherein the subeconomizer unit (itself) and/or the process cooling gas conduct and/or the excess gas conduct (to the regenerative thermal oxidizer) is/are configured for (controllably) distributing the process cooling gas into the process cooling gas conduct or the excess gas conduct or into both (i.e.
  • the proposed coke dry quenching plant and method advantageously allow to perform an excess gas treatment before remaining components of the gas are released into the atmosphere. Moreover, the treatment is performed whilst the amount of energy recovered is advantageously maximized.
  • the proposed coke dry quenching plant and method further allow to reduce the amount of otherwise required additional combustible gas (for example natural gas or coke oven gas). Indeed, in common prior art processes using post-combustion, such additional combustible gas is necessary for performing a post-combustion treatment. Hence, extra CO2 emissions can be avoided and operational costs of the plant (operated) according to the present invention are also significantly reduced.
  • additional combustible gas for example natural gas or coke oven gas
  • the proposed coke dry quenching plant and/or the method may easily be adapted to already existing coke dry quenching plants in case retrofits are carried out.
  • the proposed coke dry quenching plant and method allow to treat the excess gas, whilst providing the possibility to choose form a certain range of determinable process parameters, which in turn gives an operator or operating system a significantly increased freedom for piloting or adapting the gas treatment process as well as the quenching process.
  • a process cooling gas composition and an excess gas composition i.e. the composition of a gas conducted from a heat recovery apparatus to the cooling chamber or from a heat recovery apparatus to the regenerative thermal oxidizer, may be generated that is identical or at least similar to the composition exemplarily given in the following table:
  • the inventors have further found that a rather small change in the process parameters of the coke dry quenching operation may lead to higher contents of H2 and CO in the excess gas entering the regenerative thermal oxidizer (RTO). Since the process cooling gas used within the cooling chamber has a lower content of reactive oxygen in comparison to the (fresh) cooling gas, or even e.g. to the recirculation gas exiting the RTO, the quantity of coke loss generated in the CDQ plant is lowered. This in turn leads to a lower gasification rate of coke, hence a reduced loss of coke.
  • RTO regenerative thermal oxidizer
  • the process cooling gas of the CDQ which has the same composition than the excess gas, has a reduced amount of CO2 which, in contact with hot coke over 600°C, influences the amount of CO and thus the Boudouard reaction: C + CO2 2 CO.
  • the overall energy balance is in any case positive due to the an “autothermal” reduction of the excess gas combustion.
  • the recirculation conduct which connects the RTO to the off-gas conduct, e.g. to the first dedusting unit, provides additional gas (recirculation gas) and thermal input to the heat recovery apparatus which produces additional steam.
  • the recirculation gas in the recirculation conduct is a gas essentially composed of N2, H2O and CO2, its effect on the chemical composition of the off-gas, and thus of that of the process cooling gas, is very limited, such that the overall effect is a general reduction of H2O and CO2 content in the offgas and thus a lower carbon gasification.
  • Coke dry quenching plant generally refers to facilities configured for quenching or cooling hot coke.
  • a coke dry quenching plant has at least one cooling chamber.
  • Cooling chamber generally refers to an entity that is configured for (temporarily) storing hot coke in order to cool it down. Cooling chambers are used to cool down coke under controlled process conditions, generally from a temperature of about 1100°C to a temperature of about 180°C.
  • Off-gas conduct generally refers to a line, pipeline or other constructional element that is configured to convey the gas released, generated or coming from the cooling chamber, i.e. the off-gas, via an offgas outlet of the cooling chamber to a heat recovery apparatus.
  • a dedusting unit may be arranged within or be an integral part the off-gas conduct.
  • Dedusting unit generally refers to an apparatus for dedusting gas.
  • a dedusting unit may be a filter, a cyclone, a dust chamber, a separator, a Venturi scrubber, or a similar device for separating particles form the gas.
  • the first dedusting unit is preferably formed as a dust chamber.
  • the coke dry quenching plant may comprise more than one dedusting unit.
  • a first dedusting unit may be arranged in the off-gas conduct downstream of the cooling chamber and upstream of the heat recovery apparatus, while a second dedusting unit may be arranged downstream of the sub-economizer unit and upstream of the regenerative thermal oxidizer, as further described below.
  • Heat recovery apparatus refers to an apparatus that is configured for recovering heat from the entering hot off-gas, generally at a temperature range of about 800 to about 950 °C and at a pressure range of about -2000 to about -4000 Pa gauge, and thereby cool down the off-gas to a predefined first temperature range, such as a range of about 160 to about 180 °C, at a preferred pressure range of about -3000 to about -5000 Pa gauge.
  • Fan unit generally refers to a device for moving, conveying or pressurizing a gas, such as a compressor, a fan or a turbine.
  • the coke dry quenching plant may comprise more than one fan unit, the first fan unit being arranged upstream of the subeconomizer and downstream of the heat recovery apparatus.
  • Sub-economizer unit generally refers to an apparatus configured to (further) cool down the entering gas from temperature range of about 170 to about 200 °C, at a pressure of about 6000 to about 8000 Pa gauge, to an outlet temperature (second temperature range) of about 130 to about 160 °C at a pressure of about 6000 to about 8000 Pa gauge. It may optionally itself be configured to distribute/split an entering gas (stream) into two or more outgoing gas streams. Alternatively or additionally, the distribution or splitting may be effected by the process cooling gas conduct and/or the excess gas conduct, such as with one or more appropriate valve arrangements and/or fan units within said conducts. Furthermore, the sub-economizer unit can for example be arranged downstream of the first fan unit.
  • the sub-economizer unit is connected to the cooling chamber via a process cooling gas conduct for conducting process cooling gas to the cooling chamber and likewise connected to a regenerative thermal oxidizer via an excess gas conduct for conducting excess gas to the regenerative thermal oxidizer.
  • the sub-economizer unit or the process cooling gas conduct or the excess gas conduct or a combination thereof is configured to distribute or split the gas into the process cooling gas conduct and/or the excess gas conduct.
  • a control or regulation valve can advantageously be installed in the excess gas conduct at the outlet of or further downstream the sub-economizer.
  • a valve may be configured to control or regulate the pressure inside the cooling chamber in order to set it to a preferred specific value or value range.
  • a further, e.g. second, fan unit may be arranged within said excess gas conduct to effect or assist the distribution/splitting.
  • Regenerative thermal oxidizer also called RTO, refers to a commonly known device, respectively technology, for treating gases.
  • the regenerative thermal oxidizer is a gas treatment device allowing to lessen air pollution and decompose hazardous gases at high temperatures.
  • Regenerative thermal oxidizer may present in various forms, such as for example ceramic-bed based RTO, regenerative catalytic thermal oxidizer, regenerative flameless thermal oxidizer (FTO) or similar forms. Unlike conventional post-combustion burners and even conventional thermal oxidizers, a large part of the generated heat is recovered through the use of e.g. ceramic beds in the regenerative thermal oxidizer.
  • These beds may consist of at least two, but more generally at least three alternately fed sections, wherein the heat generated by the oxidation in a first section is subsequently used to preheat the gas in a second section, while a third section is cleaned with the rest of the hot gas, before the cycle switches sections.
  • the use of a regenerative thermal oxidizer in combination with a cooling chamber of a coke dry quenching plant thus also allows that the heat of waste gas coming from the combustion within the RTO can be recovered and used for heating up the (inlet) gas and air before said gas mixture enters the combustion chamber of the RTO.
  • an arrangement combining an RTO with a coke dry quenching process also allows that in cases where the amount of hydrogen forming part of the gas generated within the cooling chamber has risen to a certain amount, e.g. about even as low as 0.7 vol.-%, the RTO does not require any additional fuel firing during its normal operation. Common RTO require fuel during the start-up phase which only occurs occasionally during the year, such as for a maximum of 1 day of startup periods.
  • an exemplary coke dry quenching plant configured to cool 100 tph (tonnes per hour) of hot coke, it is possible to use an RTO to treat excess gas having a flowrate of about 13000 Nm 3 /h.
  • the coke dry quenching plant further comprises an air introducing unit for introducing air into the excess gas conduct.
  • the air introducing unit allows that air is mixed with the excess gas to form an enhanced excess gas (prior to) entering the RTO, which in turn enables to precisely control the mixing and temperature of the gas entering the RTO.
  • the autothermal energy of excess gas may however be higher than required for (stable) RTO operation. Hence, it may be beneficial or desirable to bleed some gas and heat out from the RTO. This can be advantageously done through a chimney conduct to the chimney.
  • the air introducing unit is advantageously arranged upstream of the thermal oxidizer, preferably fluidly connected to or arranged within the excess gas conduct.
  • the regenerative thermal oxidizer and/or a (downstream) chimney conduct and/or the (downstream) recirculation conduct may be configured to (controllably) distribute or split the gas (exiting the regenerative thermal oxidizer) into the chimney conduct configured for conducting the gas to a chimney and/or the recirculation conduct configured for conducting the gas as recirculation gas into the first dedusting unit.
  • the control or regulation of the distribution/splitting e.g. using control or regulation valves similar to those described above in the context of the sub-economizer is made to control the temperature inside oxidizer chamber or RTO.
  • the autothermal energy may be higher than required for a stable operation of the RTO and, in such cases, some thermal energy may advantageously be removed (or bled) from the system, the overall aim or priority being to send the hot recirculation gas (with its extra thermal energy) back to the heat recovery unit, thereby increasing the steam production.
  • a second dedusting unit may be arranged downstream of the subeconomizer unit and upstream of the regenerative thermal oxidizer. Such a second dedusting unit advantageously allows for further removal of dust from the excess gas, which in turn improves the reliability of (RTO) plant due to a reduced risk of dust clogging.
  • the air introducing unit may be arranged downstream of the second dedusting unit such that the air introducing unit is configured to introduce air into the excess gas conduct downstream of the second dedusting unit and upstream of the regenerative thermal oxidizer to provide an enhanced excess gas.
  • a second fan unit is advantageously arranged in the excess gas conduct, upstream of the regenerative thermal oxidizer and preferably downstream of the second dedusting unit. Indeed, a second dedusting (further) reduces the dust load in the excess gas, thereby rendering the operation of the second fan unit more reliable.
  • the air introducing unit is arranged within/fluidly connected to the excess gas conduct, upstream of the second fan unit.
  • a second fan unit allows for enhanced control of the conveying of the excess gas and preferably the air introduced into the excess gas.
  • air When air is introduced, it further facilitates its thorough mixing with the excess gas to form the so-called enhanced excess gas and allows for an improved control of the pressure within the RTO.
  • the invention also concerns a method for coke dry quenching and off-gas treating.
  • the advantages and embodiments given in view of the coke dry quenching plant also apply to the method.
  • the invention thus also proposes a method for coke dry quenching and offgas treating, wherein the method comprises the following steps: evacuating an off-gas from a coke dry quenching cooling chamber of a coke dry quenching plant, conducting the off-gas via a first dedusting unit to a heat recovery apparatus, wherein the first dedusting unit is arranged downstream of the coke dry quenching cooling chamber and upstream of the heat recovery apparatus; cooling down the off-gas in the heat recovery apparatus to a predefined first temperature range; and accelerating the cooled off-gas, by a first fan unit arranged downstream of the heat recovery apparatus.
  • the method further comprises distributing or splitting the gas (leaving/about to leave the sub-economizer) as process cooling gas into a process cooling gas conduct and/or as excess gas into an excess gas conduct within or downstream the sub-economizer unit configured to cool the off-gas down to a predefined first temperature range and arranged downstream of the first fan unit, wherein the sub-economizer unit is connected to the cooling chamber via the process cooling gas conduct and wherein the sub-economizer unit is connected to a regenerative thermal oxidizer via the excess gas conduct; and wherein the sub-economizer unit itself, or the process cooling gas conduct, or the excess gas conduct, or a combination thereof, is configured to distribute or split the gas into the process cooling gas conduct or the excess gas conduct; and feeding gas from the regenerative thermal oxidizer as a recirculation gas through a recirculation conduct into the off-gas conduct.
  • the method may further comprise introducing air into the excess gas conduct, upstream of the thermal oxidizer, to provide an enhanced excess gas.
  • the method may further comprise separating gas, within or downstream the regenerative thermal oxidizer, such that the gas is (controllably) distributed or split into a chimney conduct conducting the gas to a chimney or into a recirculation conduct feeding the gas back into the off-gas conduct as a hot recirculation gas.
  • the gas entering the regenerative thermal oxidizer may be preheated, preferably inside ceramic packing media of the RTO itself, advantageously by residual heat of the exhaust gas at the exit of the RTO, preferably to temperatures within a temperature range of about 700 to about 850 °C.
  • the excess gas within the excess gas conduct has a flowrate within a range of within a range of about 40 to about 240 Nm 3 /T coke quenched, such as from about 50 to about 200 Nm 3 /T coke quenched, and within a temperature range of approximately 130 °C up to approximately 200 °C and/or with a pressure of about +3000 to about +7000 Pa gauge. Due to the proposed coke dry quenching plant and method, a continuously flow of (excess) gas of the coke dry quenching plant can be treated whilst having a particularly high flowrate (in comparison to known processes and plants).
  • the recirculation gas exiting the regenerative thermal oxidizer into the recirculation conduct preferably has a temperature within a temperature range of about 800 to about 950 °C, a gas flowrate in a range of about 4 Nm 3 /T to about 30 Nm 3 /T, and a pressure in a range of about 2000 to about 5000 Pa gauge.
  • the gas exiting the chimney comprises a mix of the following typical composition: about 3.1 vol.-% H2O, about 13.5 vol.-% CO2, about 0 vol.-% CO, about 0 vol.-% H2, about 77.5 vol.-% N2 and about 5.9 vol.-% O2, wherein said values may vary within 0.3 vol.-%, preferably within 0.2 vol.-%, the total (including potential trace amounts of other gases) adding up to 100 vol.-% of the gases present.
  • numeric value covers a range of values from -10 % to +10 % of said numeric value, preferably a range of values form -5 % to +5 % of said numeric value.
  • Fig. 1 is a schematic illustration of the coke dry quenching plant and gas treatment method.
  • Fig 1. illustrates schematically an example of a coke dry quenching plant according to an embodiment.
  • Fig. 1 also schematically illustrates an example of how the method according to an embodiment of the invention is performed.
  • Fig. 1 shows a coke dry quenching plant 10 for quenching coke and for treating an off-gas.
  • the hot coke is quenched, meaning cooled down, within a cooling chamber 12 of the coke dry quenching plant 10 to a predefined temperature, such as from temperatures of about 1100 °C to a predefined temperature of for example about 180 °C.
  • the quenching is done with a (fresh) cooling gas admitted through cooling gas conduct 28 into the cooling chamber 12 and with the process cooling gas admitted through process cooling gas conduct 26.
  • fresh cooling gas can be any cool gas, e.g. at ambient temperature, available on-site, it generally comprises or consists of air at ambient temperature.
  • the cooling chamber 12 has at least one off-gas outlet 14 for evacuating the (hot) off-gas from said cooling chamber 12, the (hot) off-gas being the result of the cooling gases introduced into the cooling chamber 12 (i.e. fresh cooling gas through cooling gas inlet 28 and process cooling gas through process cooling gas conduct 26) and generated during quenching.
  • the off-gas outlet 14 is fluidly connected to an offgas conduct 15 which conveys, respectively guides, the off-gas from the off-gas outlet 14 of the cooling chamber 12 to a heat recovery apparatus 18 via a first dedusting unit 16.
  • the dedusting unit 16 is configured as a dust chamber, but other configurations are also possible.
  • the first dedusting unit 16 is arranged in the off-gas conduct 15 downstream of the cooling chamber 12 and upstream of the heat recovery apparatus 18. In other words, the first dedusting unit 16 is arranged in between (the off-gas outlet 14 of) the cooling chamber 12 and the heat recovery apparatus 18 to at least partially dedust the off-gas.
  • the heat recovery apparatus 18 cools the entering (at least partially dedusted) off-gas down from temperatures of about 800 to about 950 °C to temperatures of about 160 to about 180 °C, whereby heat is recovered and can be transferred to other processes (not shown) for heating purposes. Thermal energy recovered in the heat recovery apparatus may amount for example to about 1620 MJ/T coke.
  • the (partially cooled down) off-gas is extracted from the heat recovery apparatus 18 by means of a first fan 20 downstream of the heat recovery apparatus 18.
  • the (partially cooled down) off-gas is subsequently conveyed to a sub-economizer unit 24 downstream of the first fan unit 20 to further cool down the off-gas to temperatures of about 130 to about 140 °C, the first fan unit 20 being arranged within a cooled off-gas conduct 22 of the heat recovery apparatus 18.
  • the sub-economizer unit 24 is connected to the cooling chamber 12 via a process cooling gas conduct 26 for conducting process cooling gas to the cooling chamber 12, as well as to an excess gas conduct 30 for conducting excess gas to a regenerative thermal oxidizer 40.
  • the sub-economizer unit 24 itself, or the process cooling gas conduct 26, or the excess gas conduct 30, or any combination of these three components is configured to (controllably) distribute the gas into the process cooling gas conduct 26 or the excess gas conduct 30, or both, wherein the respective flow rates of process cooling gas and excess gas can be adjusted as desired or necessary, e.g. by one or more regulating valves and/or or fan units.
  • the excess gas entering the excess gas conduct 30 is advantageously subjected to a further (i.e. second) dedusting within a second dedusting unit 32, which is preferably configured as a cyclone.
  • the second dedusting unit 32 is advantageously arranged within the excess gas conduct 30 downstream of the sub-economizer unit 24 and upstream of an air introducing unit 36.
  • An air introducing unit 36 installed within the excess gas conduct 30 is provided to inject air into said excess gas conduct 30, thereby providing an enhanced excess gas with changed gas composition and temperature.
  • the air introducing unit 36 is arranged downstream of the second dedusting unit 32 and upstream of the second fan unit 38.
  • the temperature and/or the oxygen content of the enhanced excess gas may thus be precisely controlled before it enters the regenerative thermal oxidizer, RTO, 40.
  • Preferred temperatures at this point can be e.g. between 120 and 140 °C, such as between 125 and 130 °C.
  • the second fan unit 38 is arranged in the excess gas conduct 30 downstream of the inlet of the air introducing unit 36.
  • the second fan allows to accelerate the enhanced excess gas before entering the RTO 40.
  • the gas is preheated by an internal (regenerative) preheating system (not shown) that advantageously uses the heat energy of the (part of the) gas that is discharged through the chimney conduct 42 and the chimney 44.
  • the hot gas which is present in the RTO is partially recirculated as a recirculation gas to the coke dry quenching process via recirculation conduct 46 and partially discharged via chimney 44 into the atmosphere, wherein a regulated discharging through chimney 44 allows to bleed some gas and heat out of the process, e.g. to improve stable operation of the RTO 40.
  • the (part of the) gas which is recirculated as recirculation gas via the recirculation conduct 46 is advantageously injected via an inlet (not shown) upstream of or into the primary dedusting unit 16.
  • the advantage of recirculating (part of the) gas from the RTO is that the volume of the gas entering the heat recovery apparatus 18 is increased while keeping essentially the same temperature.
  • the heat recovery apparatus 18, which is advantageously configured as a heat recovery steam generator in the embodiment of Fig. 1 increases the production of valuable high-pressure steam.
  • the recirculation gas within recirculation conduct 46 mainly comprises CO2 and H2O and will constitute part of the process cooling gas admitted to the cooling chamber 12 through process cooling gas conduct 26, less fresh cooling gas is required from cooling gas conduct 28, thereby reducing coke loss during quenching, as the oxygen contents of the fresh cooling gas is higher than that of the process cooling gas. While, the reduced coke loss is of course desirable for reducing CO2 emissions and/or to maximize the amount of coke, it would on the other hand mean that the off-gas of the cooling chamber 12 would be less hot (due to the lack of part of heat generated by coke burning), thereby reducing the amount of heat recoverable in the heat recovery apparatus 18.
  • this apparently unavoidable loss in recoverable heat is in fact advantageously compensated by this same recirculation of part of the hot gas from the RTO 40 through the recirculation conduct 46 to the off-gas conduct 15 or the first dedusting unit 16, upstream of the heat recovery apparatus 18.
  • the heat recovery apparatus 18 will treat a gas in a temperature range over 800°C with a pressure in a range of -2000 kPa to 0.0 kPa.
  • the hot gas stream of recirculation gas re-collected from the RTO 40 and conducted within recirculation conduct 46 has similar temperatures of 800 to 900 °C and a pressure above 0.0 kPa.
  • the recirculation of hot gas from the RTO is all the more advantageous, as this hot gas has temperatures which are similarly high than those of the off-gas from the cooling chamber 12.
  • the bleeding of part of the (excess) heat of the RTO allows for a better temperature control within the RTO itself, as it allows to take away that part of the heat that is not required to preheat the regenerative bed to a temperature sufficient for triggering the thermal oxidation of the excess gas.
  • the regulation of the different gas flows e.g. in the subeconomizer unit 24 or the RTO 40 is generally realized by controlled or automated valves (not shown). Due to such an arrangement of automated valves in the RTO 40 and an appropriate bleeding through chimney conduct 42 and chimney 44, the RTO may be operated in stable conditions and the temperature of its oxidation chamber (not shown) can be kept in a predefined and advantageous range of about 800 to 850 °C. Legend:

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Coke Industry (AREA)

Abstract

L'invention concerne une installation de trempe à sec de coke (10) et un procédé de trempe à sec de coke et de traitement de dégagement gazeux, l'installation de trempe à sec de coke (10) comprenant : une chambre de refroidissement (12) pour refroidir le coke chaud jusqu'à une température prédéfinie ; un conduit de dégagement gazeux (15) pour conduire le gaz d'une sortie de dégagement gazeux (14) de la chambre de refroidissement (12) à un appareil de récupération de chaleur (18) ; une première unité de dépoussiérage (16) pour dépoussiérer le gaz, la première unité de dépoussiérage (16) étant disposée dans le conduit de dégagement gazeux (15) en aval de la chambre de refroidissement (12) et en amont de l'appareil de récupération de chaleur (18) ; l'appareil de récupération de chaleur (18) étant configuré pour refroidir le gaz jusqu'à une première plage de températures prédéfinie ; une première unité de ventilateur (20) disposée en aval de l'appareil de récupération de chaleur ; l'installation de trempe à sec de coke comprenant en outre une unité de sous-économiseur (24) disposée en aval de la première unité de ventilateur (20) et reliée à la chambre de refroidissement (12) par l'intermédiaire d'un conduit de gaz de refroidissement de processus (26) et l'unité de sous-économiseur (24) étant reliée à un dispositif d'oxydation thermique régénératif (40) par l'intermédiaire d'un conduit de gaz en excès (30) ; l'unité de sous-économiseur (24) et/ou le conduit de gaz de refroidissement de processus et/ou le conduit de gaz en excès étant configuré(s) pour distribuer ou diviser le gaz dans le conduit de gaz de refroidissement de processus (26) et/ou le conduit de gaz en excès (30) ; et l'alimentation en gaz sortant du dispositif d'oxydation thermique régénératif (40) en tant que gaz de recirculation à travers un conduit de recirculation (46) dans le conduit de dégagement gazeux (15).
PCT/EP2024/068557 2023-07-10 2024-07-02 Installation de trempe à sec de coke et procédé de trempe à sec de coke et de traitement de gaz Pending WO2025012017A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
LU504708A LU504708B1 (en) 2023-07-10 2023-07-10 Coke dry quenching plant and method for coke dry quenching and gas treating
LULU504708 2023-07-10

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WO2025012017A1 true WO2025012017A1 (fr) 2025-01-16

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LU (1) LU504708B1 (fr)
TW (1) TW202511458A (fr)
WO (1) WO2025012017A1 (fr)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009072999A1 (fr) * 2007-12-07 2009-06-11 Yevheniy Alekseevich Danilin Installation et procédé de refroidissement à sec du coke
EP3029130A1 (fr) * 2013-08-01 2016-06-08 Nippon Steel & Sumikin Engineering Co., Ltd. Dispositif d'extinction à sec du coke et procédé associé
KR20220088566A (ko) * 2020-12-18 2022-06-28 주식회사 포스코 코크스 건식 소화 설비의 코크스 손실율 예측 시스템 및 그 예측 방법

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009072999A1 (fr) * 2007-12-07 2009-06-11 Yevheniy Alekseevich Danilin Installation et procédé de refroidissement à sec du coke
EP3029130A1 (fr) * 2013-08-01 2016-06-08 Nippon Steel & Sumikin Engineering Co., Ltd. Dispositif d'extinction à sec du coke et procédé associé
KR20220088566A (ko) * 2020-12-18 2022-06-28 주식회사 포스코 코크스 건식 소화 설비의 코크스 손실율 예측 시스템 및 그 예측 방법

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