EP0026707B1 - Procédé de traitement par séchage et/ou chauffage de matériau combustible granuleux et/ou pulvérulent et installation pour la mise en oeuvre du procédé - Google Patents

Procédé de traitement par séchage et/ou chauffage de matériau combustible granuleux et/ou pulvérulent et installation pour la mise en oeuvre du procédé Download PDF

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Publication number
EP0026707B1
EP0026707B1 EP80401365A EP80401365A EP0026707B1 EP 0026707 B1 EP0026707 B1 EP 0026707B1 EP 80401365 A EP80401365 A EP 80401365A EP 80401365 A EP80401365 A EP 80401365A EP 0026707 B1 EP0026707 B1 EP 0026707B1
Authority
EP
European Patent Office
Prior art keywords
entrainment
fluidisation
agent
gaseous
coal
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
Application number
EP80401365A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0026707A1 (fr
Inventor
Roger Marcel Puff
Jean-Claude Kita
Henri Brice
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.)
Charbonnages de France CDF
Original Assignee
Charbonnages de France CDF
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
Priority claimed from FR7923920A external-priority patent/FR2465774A1/fr
Priority claimed from FR8012876A external-priority patent/FR2484069A1/fr
Application filed by Charbonnages de France CDF filed Critical Charbonnages de France CDF
Priority to AT80401365T priority Critical patent/ATE5082T1/de
Publication of EP0026707A1 publication Critical patent/EP0026707A1/fr
Application granted granted Critical
Publication of EP0026707B1 publication Critical patent/EP0026707B1/fr
Expired legal-status Critical Current

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    • 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
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • C10B57/06—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing additives
    • 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

  • the invention relates to a process and an installation for treatment by drying and / or heating by fluidization and / or gaseous entrainment of a granular and / or pulverulent combustible material, such as a coal to be dried and / or preheated for charging.
  • a granular and / or pulverulent combustible material such as a coal to be dried and / or preheated for charging.
  • coke ovens of low-coking coals by the techniques known as dry charging and preheated charging, or any other application for subsequent physical or chemical treatment.
  • the preheating of coal fines involves the use of oxygen-free fumes, and at a temperature not to exceed approximately 500 to 800 ° C. To achieve this result, it has been proposed to recycle in the combustion chamber, where neutral combustion is carried out, part of the fumes used for preheating.
  • the carbon particles must be finely ground, for example 80% and even 90% less than 2 mm. These fine particles of coal preheated to 250 ° C. are separated from the entrainment fluid by means of two stages of cyclones, the capture efficiency of which is 98 to 99%.
  • the smoke treatment system achieves the result but it does not only have advantages.
  • the un purified recycled fumes therefore still charged with fine dust, are introduced, by means of a fan, into the combustion chamber, at the level of the burner which operates in stoichiometric combustion and therefore at a close temperature the theoretical temperature which, for coke oven gas, exceeds 2000 ° C. Fine particles of carbon can burn, or melt, which is undesirable.
  • the fumes at the outlet of the cyclones must be purified before being released into the atmosphere.
  • a dry dusting is carried out on the exhaust fumes only, while in a second type, as in FR-A-2 207 592, all of the fumes, recycled or not, are subjected to dry dusting.
  • the installation when the installation is in standby conditions (for example in the event of an incident upstream or downstream of the preheater), the quantity of fumes discharged into the atmosphere becomes very small, so that in the case of the first type, the final dust collector, disposed on the venting pipe, arrives at working at zero or very low flow rate.
  • the dust collector is of the wet type, for example high-energy venturi, the reduction in the flow of smoke is not a problem.
  • a wet dust collector is inappropriate because the dust collected is advantageously to be introduced into the coke fines.
  • a dry type dust collector bag filter and electrostatic precipitator
  • the reduction in the smoke flow causes condensation and consequently corrosions in the device.
  • the dust collector risks being in a vacuum system, thus causing parasitic air to enter the installation.
  • the main object of the invention is to avoid the drawbacks of the two aforementioned types of installations comprising dry dust removal and to propose a new process and a new installation having a dry dust collector that is not overloaded or oversized, and not subject to corrosion by risk of insufficient flow causing the temperature to drop below the dew point, especially during waiting periods with low heat production in the installation. In other words, it is desired to obtain the optimum dedusting efficiency from the deduster.
  • Another object of the invention is to propose a solution to the problem of the recovery, handling and re-use of the dust recovered by means of a particular treatment which will be explained.
  • the objects of the invention are achieved by a method of treatment by drying and / or preheating by entrainment and / or fluidization of a granular or pulverulent combustible material, in which the material is dried and / or heated by entrainment and / or fluidization by introducing it into a drive and / or fluidization enclosure, where a drive and / or fluidization regime is established at a given temperature by means of a neutral gaseous agent obtained at temperature and in regulated quantities in a combustion chamber , and from which the dried and / or heated material is extracted by pneumatic transport within the effluent gas agent, then said material is separated from said effluent gas agent by distributing said gaseous agent in regulated quantities between a recycling line to the combustion chamber and a discharge outlet for the surplus, process in which the surplus gaseous agent is dusted by a dry dust collector, thanks to the fact that dust is also removed at s ec in the latter a regulated part of the recycled gaseous agent, at least during
  • the dry dust collector works in all circumstances at a constant gas flow rate and at a suitable temperature, already already regulated by adjusting the burner of the combustion chamber. For each type of dust, there is an optimal efficiency obtained by a corresponding gas passage speed.
  • the second object is achieved by a process in which a liquid hydrocarbon binder is injected into the solid fuel in one of the treatment stages, thanks to the fact that the dust is trapped in a hot carbonaceous liquid. captured by the dry dust collector and said hot carbonaceous liquid charged with said dust is used as an auxiliary hydrocarbon binder, at least partially.
  • said hot carbonated liquid, charged with said dust is injected into the combustible material after the point of separation from the heat transfer gas having served as a gaseous effluent transport agent.
  • the carbonated liquid it is advantageous for the carbonated liquid to be very mobile and very wetting for dust.
  • it will advantageously be chosen from the group consisting of hydrocarbons liquid at room temperature or after reheating, such as heavy fuel oil, petroleum bitumens. In this way we will obtain a pumpable mixture allowing its incorporation into preheated coal, as indicated above.
  • the means for regulating the quantity of gaseous agent passing through the filter to act directly on said first means for distributing the gaseous agent.
  • the object of the invention is also achieved by an installation of the above type com taking a means for introducing liquid hydrocarbon binder into the solid fuel at one of the stages of the treatment and a device for trapping in carbonaceous liquid the dust collected by the dust collector.
  • the means for introducing the liquid hydrocarbon binder into the solid fuel, such as coal open downstream of the point of exit of said fuel from the coal / gas separator device, preferably in a mixing conveyor screw, such as it is known per se.
  • the installation comprises, in addition to this means of introducing the liquid hydrocarbon binder into the fuel, a conventional contiguous means of direct introduction of hydrocarbon binder and / or carbonaceous liquid.
  • a coal preheating installation comprises a preheater dryer-mill designated as a whole by 10. This comprises a vertical pipe 11 for driving the coal up by hot smoke, a screw conveyor 12 bringing the coal from a hopper 13 to the pipe 11 at a point situated above a venturi 14 provided in the lower part of the pipe 11.
  • a fluidization enclosure 15 in the lower part of which opens the said pipe 11, below a rotary impact mill 16.
  • the pipe 17 makes it possible to drive this coal towards a battery of cyclones 18 comprising two stages, primary cyclone and secondary cyclones , at the tip of which this coal is recovered on a screw conveyor 19 to a storage hopper with a view to its subsequent charging in a coke oven.
  • the fumes are recovered in a recycling pipe 21 by means of a fan 22.
  • the installation comprises a combustion chamber 20 opening at the base of the ascending pipe 11.
  • This combustion chamber is supplied by a double burner 30 in all points similar to that which is described in FR-A-2 378 081, it that is to say that it comprises a burner 31, called the main burner, in normal operation for the preheating of the coal, the other 36, called the auxiliary burner, for putting the installation on standby in the event of interruption of the supply of coal by the conveyor 12.
  • Each burner is provided with means for regulating the combustion air so that the combustion is substantially neutral and also comprises means for regulating the fuel subject to temperature measurements in the fluidization enclosure.
  • the fan 22 recycles by ducts 23 a portion of the fumes withdrawn in 21 in a regulated quantity such that the speed of the total gas flow is kept constant in the fluidization enclosure 15.
  • a regulation assembly 48 makes it possible to regulate the combustion with the double burner 30 as a function of the temperature measured at 43 in enclosure 15.
  • a dry electrostatic dust collector 24 is supplied by a line 2, derived from the recycling line 21, from where it separates from part 3 of the line 21.
  • the dust collector 24 supplies a discharge line 5 and another recycling pipe 7 joining the pipe 3 upstream of the recycling fan 22.
  • Valves, namely 9 on the pipe 2, 6 on the discharge pipe 5 and 42 on the pipe 3 in its short-circuiting part the filter 24, make it possible to distribute at will the normal gas flow rate V of the line 21 between a flow rate V 1 of direct recycling in the line 3, a flow rate V 2 of recycling with dedusting through the line 7 which joins the line 3 and a flow rate V 3 of evacuated gaseous effluent.
  • the pressure drop of cyclones 18, a function of the gas flow rate V, is kept constant, as it is known per se, by the action of a valve 1.
  • the flow rate V 3 of gaseous effluent to be discharged is adjusted by the valve 6 which acts as a pressure regulator to keep the pressure in the electrostatic precipitator 24 constant.
  • a greater or lesser part of the flow recycled in the combustion chamber 20 measured at 4 is diverted to be definitively discharged at 5.
  • the vacuum observed between the inlet and the outlet of the dust collector is measured, the measurement is introduced into a regulator 37 which controls the valve 42 and / or the valve 9 so as to ensure compliance with a set value for vacuum between inlet and outlet of the dust collector.
  • the purpose of the separation stage constituted by the cyclones 18, is to separate the granular and / or powdered coal which is dried and / or heated and the entrainment gases by accepting the minimum loss of one and the other.
  • the purpose of the dedusting stage is to restore to the atmosphere or to recycle a gas as free as possible from the dust, for example about ⁇ 0.05 mm, entrained in the vortex of the cyclones.
  • the total smoke flow V ie 66,000 m 3 N / h which circulates in the preheater, is kept constant by adjusting the flow of smoke V1 + V2 recycled into the combustion chamber by means of the fan 22.
  • the excess flow V3 is rejected at the atmosphere.
  • the volume V3 is 24,000 m 3 N / h of smoke. This is by definition the nominal flow rate of the electrostatic precipitator.
  • the dust collected in the dry dust collector is sent into the screw conveyor 19 through a carbonaceous liquid trapping device, simply shown by the rectangle 60 in FIG. 1, but shown schematically in its entirety at Figure 2.
  • an Archimedes screw 62 supplying a homogenization kneading device 63 of sufficient capacity supplied with liquid and hot hydrocarbon product via a pipe 64.
  • the mixture is put into circulation closed in line 64 by means of a pump 67.
  • the pure liquid is topped up by a line 68 in the device 63.
  • a fraction of mixture, corresponding to the production of soot associated with the quantity of liquid sufficient for handling and necessary for the process, is taken from the closed circulation circuit and brought by a pipe 70 to the point of use.
  • the point of use is the aforementioned screw conveyor 19. It is advantageous to provide an additional point of introduction of the carbonaceous liquid at 74 on the mixing screw 19.
  • All the pipes are heated by steam, the pipes can be swept with steam to be purged and it is advantageous to control the proportion of the liquid / soot mixture to the flow of preheated coal, as is known per se adding hydrocarbon binder to preheated coal.
  • the invention makes it possible to recover the soot recovered in a dry dust collector without humidifying with water, to handle the soot safely and without pollution and to transport it to a point of use at a height compatible with the pressure. pump discharge.
  • the invention also makes it possible to recycle the sootings of dry dedusting in the coke paste preheated with fuel.
  • the invention also makes it possible to limit takeoffs during charging and to limit takeoffs during charging with the fuel mixture.
  • a fraction of the fuel at the rate of approximately 400 kg / h is sprayed with steam in the mixer.
  • the rest, about 150 kg / h, is sprayed pure onto the preheated coal in the mixing auger.
  • the invention also makes it possible to recycle the soot in the coke paste preheated with a petroleum bitumen, which, moreover, used alone, would have allowed to bring to the preheated coke paste the cohesion necessary to form either balls, or a bread pounded from dry and hot coal and to prepare either balls or a pounded bread after adding in the mixing screw the quantity total of necessary binder of which all or part will have been used to handle the soot.
  • soot is produced using an electrostatic precipitator.
  • a total of 6% by weight of a petroleum bitumen heated to 150 ° C. is added (percentage based on the total quantity of preheated coal).
  • a fraction of the bitumen, for example 650 kg (or less) is sprayed with steam in the mixer.
  • the rest, or 3,250 kg / h, is added to the mixing screw with preheated coal. This produces a charcoal-binder mixture suitable for either pelletizing or pounding. by recycling the soot from the dry dust collector.
  • the invention has been described with regard to a fluidization drying and / or preheating installation. It also applies equally well to a drying and / or preheating installation by co-current drive by hot fumes.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Coke Industry (AREA)
  • Drying Of Solid Materials (AREA)
  • Electrostatic Separation (AREA)
EP80401365A 1979-09-26 1980-09-25 Procédé de traitement par séchage et/ou chauffage de matériau combustible granuleux et/ou pulvérulent et installation pour la mise en oeuvre du procédé Expired EP0026707B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT80401365T ATE5082T1 (de) 1979-09-26 1980-09-25 Verfahren zur behandlung durch trocknen und/oder erhitzen teilchenfoermigen und/oder pulverfoermigen brennbaren materials und anlage zur durchfuehrung des verfahrens.

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
FR7923920 1979-09-26
FR7923920A FR2465774A1 (fr) 1979-09-26 1979-09-26 Procede de traitement de charbon a cokefier et installation pour la mise en oeuvre du procede
FR8012876A FR2484069A1 (fr) 1980-06-10 1980-06-10 Procede et installation de sechage et/ou chauffage d'un materiau combustible granuleux et/ou pulverulent
FR8012876 1980-06-10

Publications (2)

Publication Number Publication Date
EP0026707A1 EP0026707A1 (fr) 1981-04-08
EP0026707B1 true EP0026707B1 (fr) 1983-10-19

Family

ID=26221371

Family Applications (1)

Application Number Title Priority Date Filing Date
EP80401365A Expired EP0026707B1 (fr) 1979-09-26 1980-09-25 Procédé de traitement par séchage et/ou chauffage de matériau combustible granuleux et/ou pulvérulent et installation pour la mise en oeuvre du procédé

Country Status (10)

Country Link
US (1) US4321032A (enExample)
EP (1) EP0026707B1 (enExample)
AU (1) AU534099B2 (enExample)
BR (1) BR8006070A (enExample)
CA (1) CA1127401A (enExample)
DE (1) DE3065381D1 (enExample)
ES (1) ES495305A0 (enExample)
IN (1) IN153919B (enExample)
NO (1) NO802837L (enExample)
RO (1) RO81931A (enExample)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NO164608C (no) * 1988-04-20 1990-10-24 Elkem Technology Fremgangsmaate for fremstilling av metaller eller ferrolegeringer ved direkte reduksjon samt kolonne for behandling av finkornede materialer med gass.
JP3783071B2 (ja) * 2002-07-11 2006-06-07 味の素株式会社 化粧料組成物
DE102005052753A1 (de) * 2005-11-04 2007-05-10 Polysius Ag Anlage und Verfahren zur Herstellung von Zementklinker
CN104807346A (zh) * 2015-04-30 2015-07-29 云南创森环保科技有限公司 粉状物料冷却系统

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1265397A (fr) 1960-05-21 1961-06-30 Charbonnages De France Procédé perfectionné pour l'obtention de coke sidérurgique à partir de charbons peu cokéfiants
GB1232030A (enExample) 1967-10-31 1971-05-19
US3687431A (en) * 1970-12-18 1972-08-29 Aluminum Co Of America Preheating of dry aggregate for carbon electrodes
DE2256385B2 (de) * 1972-11-17 1981-04-16 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zum kontinuierlichen Erhitzen feinkörniger Feststoffe
US4008042A (en) * 1974-08-16 1977-02-15 Coaltek Associates Coal heating temperature control
DE2457528A1 (de) * 1974-12-05 1976-06-10 Bergwerksverband Gmbh Verfahren zur verminderung der staubentwicklung bei der einfuehrung vorerhitzter kohle in verkokungsoefen
US4030983A (en) * 1975-04-04 1977-06-21 Bergwerksverband Gmbh Method of restricting dust development when feeding coal into coke ovens
DE2659335C2 (de) 1976-12-29 1985-10-24 Bergwerksverband Gmbh Betrieb einer Kohleerhitzungsanlage
FR2378081A1 (fr) * 1977-01-24 1978-08-18 Charbonnages De France Installation et procede de regulation du prechauffage de charbon a cokefier
DE2719189C2 (de) * 1977-04-29 1984-07-19 Carl Still Gmbh & Co Kg, 4350 Recklinghausen Verfahren zum Betrieb einer Kohlevortrocknungs- bzw. -erhitzungsanlage in Verbindung mit einer Kokerei
DE2748423A1 (de) * 1977-10-28 1979-05-03 Bergwerksverband Gmbh Verfahren zur inertisierung von kohleerhitzungsanlagen

Also Published As

Publication number Publication date
ES8200715A1 (es) 1981-11-01
RO81931A (ro) 1983-06-01
AU6267480A (en) 1981-04-09
CA1127401A (fr) 1982-07-13
EP0026707A1 (fr) 1981-04-08
IN153919B (enExample) 1984-09-01
BR8006070A (pt) 1981-04-07
RO81931B (ro) 1983-05-30
AU534099B2 (en) 1984-01-05
DE3065381D1 (en) 1983-11-24
ES495305A0 (es) 1981-11-01
NO802837L (no) 1981-03-27
US4321032A (en) 1982-03-23

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