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EP3609980A1 - Dispositif et procéde pour l'obtention de gaz lors de la cokéfaction d'une matière de départ contenant du charbon, et utilisation - Google Patents

Dispositif et procéde pour l'obtention de gaz lors de la cokéfaction d'une matière de départ contenant du charbon, et utilisation

Info

Publication number
EP3609980A1
EP3609980A1 EP18716213.6A EP18716213A EP3609980A1 EP 3609980 A1 EP3609980 A1 EP 3609980A1 EP 18716213 A EP18716213 A EP 18716213A EP 3609980 A1 EP3609980 A1 EP 3609980A1
Authority
EP
European Patent Office
Prior art keywords
gas
furnace chamber
furnace
height
briquettes
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.)
Pending
Application number
EP18716213.6A
Other languages
German (de)
English (en)
Inventor
Ronald Kim
Uwe TSCHIRNER
Mathias SCHELLER
Matthias SPÖTTLE
Fabian GRAW
Joanna KÜHN-GAJDZIK
Hans-Werner Schröder
Volker Herdegen
Franz FEHSE
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.)
ThyssenKrupp AG
ThyssenKrupp Industrial Solutions AG
Original Assignee
ThyssenKrupp AG
ThyssenKrupp Industrial Solutions 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 ThyssenKrupp AG, ThyssenKrupp Industrial Solutions AG filed Critical ThyssenKrupp AG
Publication of EP3609980A1 publication Critical patent/EP3609980A1/fr
Pending legal-status Critical Current

Links

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
    • C10B1/00—Retorts
    • C10B1/02—Stationary retorts
    • C10B1/04—Vertical retorts
    • 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
    • C10B27/00—Arrangements for withdrawal of the distillation gases
    • C10B27/02—Arrangements for withdrawal of the distillation gases with outlets arranged at different levels in the chamber
    • 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
    • C10B3/00—Coke ovens with vertical chambers
    • C10B3/02—Coke ovens with vertical chambers with heat-exchange devices
    • 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
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge
    • C10B47/04—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge in shaft furnaces
    • 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
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/08—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form in the form of briquettes, lumps and the like
    • 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 device and a method in each case for the use of carbonaceous feedstock and the related use of the feedstock or gases obtained therefrom.
  • the invention relates to apparatus and methods for the recovery or use of (by-) products in the production of coke from feedstocks, which hitherto can not be used as standard, or which have not yet provided a satisfactory end product.
  • the invention relates to an apparatus and a method according to the preamble of the respective independent claim.
  • the invention relates to the use of individual components or devices especially in connection with these alternative starting materials.
  • Coke and coal-containing or carbonaceous feedstocks are currently and in the future for most economies of our earth indispensable raw materials or already present as such recyclables per se. So far, mainly hard coal with high baking capacity (so-called fat coals) are coked. However, it is to be expected that certain types of coke will become scarcer on the world market within a short time. In particular, a declining availability of coking coal that is well suited for coking must be expected, with the result that in the future also badly baking or strongly driving coals or other carbon carriers must be used, in particular for the production of blast furnace coke.
  • Coke ovens for producing coke can, as mentioned, be designed as so-called vertical chamber furnaces.
  • Vertical chamber furnaces are loaded with raw material briquettes or coal briquettes from above.
  • Vertical chamber furnaces can have a considerable height, for example in the range of 30 to 40m.
  • the briquettes are placed for example with a crane above the furnace and slip, in particular by gravity, through the coking shaft (furnace chamber), in particular over a period of several hours, for example 12 or 15 hours, according to the time required to convert the charge into coke.
  • the briquettes a temperature change, in particular from initial temperatures below 300 ° C to final temperatures between 900 and 1100 ° C.
  • two to ten furnace chambers are combined to form a so-called furnace battery of a coke oven.
  • the shaft of a respective furnace chamber may have a height of in particular 3.5m to 10m, and a width of in particular 150 to 600mm. It can be seen that the briquettes have high frictional and compressive forces when coking. The strength of the briquettes should therefore be very high.
  • the raw material can be minced in advance, in particular in hammer mills, in particular on particle sizes of 0 to 1 mm
  • the briquettes are subsequently compacted in presses by crimping the grains, hitherto in many cases a briquette geometry in the manner of an elongated cuboid having optionally rounded corners or rounded edges has proved advantageous by means of roller presses.
  • the coke was either in gas ovens with vertical chambers, or in coke ovens with horizontal chambers.
  • the latter can be classified into two types: horizontal chamber (composite) ovens with narrow oven chambers and vertically heated, indirectly heated batch, and so-called heat (non-) recovery ovens with vault-like oven chambers and flat lying therein batch, at least can be heated directly from above.
  • horizontal chamber composite ovens with narrow oven chambers and vertically heated, indirectly heated batch
  • heat (non-) recovery ovens with vault-like oven chambers and flat lying therein batch
  • a furnace device with at least one vertical furnace chamber, in particular a coke oven, for producing coke from at least one solid starting material, in particular from the group: brown coal, low-baking hard coal, biomass, petroleum coke, petroleum coke; comprising at least one for tempering of the Briquette driers equipped with feed stock and at least one oven chamber with heating walls coupled in particular below the briquette drier to the briquette dryer; wherein the briquette dryer has a heating device and a briquette reservoir heatable therewith, and wherein the briquette dryer is set up to set a continuously or stepwise increasing temperature in the briquette reservoir in the conveying direction of the briquettes, in particular at least two or three temperature levels in the range of 60 to 200 ° C.
  • the oven device further comprises an entry system comprising at least one lock device, which entry system between the briquette reservoir and the (respective) oven chamber is arranged and adapted for supplying briquettes from the briquette reservoir to the (respective) oven chamber.
  • an entry system comprising at least one lock device, which entry system between the briquette reservoir and the (respective) oven chamber is arranged and adapted for supplying briquettes from the briquette reservoir to the (respective) oven chamber.
  • the temperature level can increase steadily, and / or predetermined temperature levels can be defined, in particular in different height levels of a reservoir, in which the briquettes are conveyed in the direction of gravity.
  • the desired temperature level can be set individually for each process or feedstock.
  • a Konti process for coking can be set.
  • the briquette bed moves through at least one temperature zone with increasing temperature.
  • the desired throughput can be adjusted and regulated in particular by means of a discharge system.
  • the conversion / upgrading of, for example, coal into coke can be carried out continuously. It can be carried out a temperature control, and in individual temperature zones can influence on the process taken and / or by-products can be evacuated.
  • the continuous process in the vertical chamber furnace has z. B. also in terms of temperature stress of the material of the furnace device, in particular silica advantages. The material can be maintained largely at temperatures above 600 ° C or even 800 ° C and need not be repeatedly cooled to lower temperatures below it. As a result, occur less stress / cracks in the material.
  • the oven apparatus may include a feed unit for providing the briquettes to the briquette dryer.
  • the feeder unit is, for example, also equipped to convey the briquettes produced from a press to the briquette dryer. At a minimum, the feeder unit is arranged to ensure continuous or batch feed of briquettes to the dryer.
  • a bunker Upstream of the dryer is a bunker, to which the briquettes can be fed continuously or batchwise, and from which the briquettes can be conveyed out continuously or in batches, in particular by the briquettes sliding into the briquette dryer.
  • the entry system can be arranged above the (respective) furnace chamber. This allows a supply based on gravitational forces.
  • the furnace device is completely formed as a vertical chamber furnace with vertical furnace chambers.
  • a vertical furnace chamber is a furnace chamber through which the briquettes are conveyed in the vertical direction, in particular based on gravitational forces.
  • feedstocks in particular the entire spectrum of soft, matte and lignite lignite as well as the flame coal can be mentioned. In particular, good results have already been achieved with Rhenish, Loessitzer and Indonesian lignite. It has also been shown that the devices and methods described herein are also suitable for the recovery of Russian brown and flame coals and petroleum coals.
  • the following types of coal and peat can be mentioned as feedstocks, based on a classification according to DIN, ASTM and UN-ECE, which is reproduced here schematically. It has been found in the context of the present invention, with reference to the German DI N, especially the lignite coal classified therein, matte lignite, Glanzbraunkohlen and flame coals as particularly useful. Cabbages and peat volatile
  • a meandering in several height levels extending heating channel which heating channels each individually heated by at least one burner are.
  • This type of heating can provide a variety of the benefits described herein, especially regardless of a particular design or operation of the briquette dryer.
  • the briquette dryer provides advantages in particular with regard to the preparation of the briquettes prior to feeding into the furnace chamber.
  • the heating channels then act on the briquettes present in the furnace chamber at a later stage of the process.
  • the briquette reservoir is at least comprised of: temperature, humidity, as a function of measured values measurable in the briquette reservoir from the group; for drying the briquettes to at least two different temperature levels, in particular controllably heated in at least two different height positions of the briquette reservoir, in particular a first temperature level between 60 and 105 ° C, in particular up to 95 ° C, a second temperature level between 105 and 200 ° C, and optionally at least one further temperature level comprising a temperature level between 95 and 105 ° C.
  • the upper limit of the last temperature level can be set such that a degassing is not yet caused.
  • the upper limit of the respective temperature level can be taken from temperature values determined in advance for a particular feedstock, for example stored in a data memory, or optionally specified during the process, in particular by means of at least one pressure and / or gas sensor and / or moisture sensor on / in the briquette. Dryer. This makes it possible to dry the briquettes continuously in a gentle way more continuously, without too high temperature or stress stress material.
  • the briquette reservoir can be heated depending on the measured values for controlled drying of the briquettes up to minimum moisture values of at most 1 to 5% by mass, in particular 2 to 4% by mass, at the outlet of the briquette drier.
  • moisture and / or temperature sensors can be provided in the briquette dryer, in particular at the respective height positions. It may be sufficient to carry out the temperature control solely as a function of the moisture content, assuming sufficient accuracy of the measurement.
  • capacitive or spectroscopic measuring methods can be used.
  • redundant measuring devices are preferably present, in particular for pressure, volume and / or temperature measurements. Preferably takes place the regulation at least via a temperature measurement, optionally exclusively via a temperature measurement.
  • drying is preferably carried out up to an upper temperature limit, from which the degassing (gas emission) begins with the respective starting material.
  • This upper temperature limit can be predefined for a particular feedstock, and in a control of the drying process, such upper limits can be retrieved from a data store and taken into account as a target specification.
  • the drying process can also be adapted specifically for each feedstock.
  • the aforementioned temperature and humidity ranges may e.g. Lignite or hard coal can be further restricted.
  • the starting materials have different H 2 O contents, and mass transport processes during drying are carried out specifically for each starting material, in particular due to different material structures (micro / meso / macropores).
  • brown coal it has been found that by means of the upper limit of 200 ° C, a good compromise can be found to effectively dry, but also, e.g. to effectively avoid degassing of H2S.
  • An avoidance of degassing of H2S may be particularly desirable if recycled flue gases are to be used for controlling the temperature of the briquette dryer.
  • the oven apparatus may include a controller and a measuring device coupled thereto configured to control drying or coking of the briquettes.
  • the control device can be set up or provided specifically for controlling / regulating the drying process based on the measured values.
  • the control device can also be set up or provided for each of the method steps described here, in each case in communication with corresponding sensors of the measuring device.
  • the briquette dryer has at least one dryer unit, in particular a roof dryer unit, which has a hot gas circuit, which is sealed off in particular by the briquettes, for introducing thermal energy into the briquettes.
  • a separation between hot gas and briquettes can take place.
  • the hot gas can be covered in by means of roofs or other bevelled channels Lines flow on which lines the briquettes can slip past without being left on the lines.
  • the dryer unit can be set up for continuous delivery of the briquettes based on gravitational forces (continuous operation), the briquette reservoir being integrated in the dryer unit, in particular separately from the hot gas cycle.
  • a fluidized bed drying e.g. a fluidized bed drying
  • the dryer unit described here allows gentle drying, with good controllability of the registered heat energy, and also with cost-effective and robust design of the unit.
  • the number / density of the heating lines can become larger towards the bottom in order to register more heat energy continuously, in particular without the need for a complex control.
  • the briquette dryer can also fulfill the function of buffering.
  • more layers of briquettes are always buffered above a highest / highest drying level, in particular also to avoid short-circuit flows of drying gases.
  • This multi-layered buffer of briquettes to be supplied also makes it possible to extract drying gases evenly distributed.
  • the geometry and arrangement, in particular the angle and the distances of individual roofs of a height level in the briquette dryer and the vertical distance of the drying levels can be designed such that there is no formation of solid bridges, and that the gravity movement of the briquettes can be carried out unhindered. It has been shown that a vertical or diagonal distance of at least a factor of 6 of the briquette diameter makes a good compromise between the temperature profile and (in particular solely gravity-driven) conveying or freedom of movement of the briquettes possible.
  • the respective drying circuit may have a fan and may be additionally supplied with fresh, dry exhaust gas (from heating the briquettes in the coking chambers) and / or externally generated, dry flue gas of a burner (especially intended exclusively for the dryer to ensure redundancy) become.
  • the briquette dryer has a dryer unit with a plurality of drying circuits each comprising at least two drying levels. This allows a particularly specific control of the respective temperature levels. According to one embodiment, the briquette dryer has a dryer unit with a plurality of drying circuits each comprising at least two drying levels. This provides maximum flexibility in setting a desired temperature profile in the briquette reservoir.
  • the dryer unit defines a plurality of drying levels, in particular at least four drying levels, in each of which hot gas lines are arranged, each drying level being adjustable to an individual temperature level, wherein the drying levels are preferably arranged at least 60 cm apart. This provides a good compromise between plant engineering effort and fineness of temperature control options.
  • the briquette dryer or the briquette reservoir has a height extent of at least 2m, preferably at least 2.5 or 3m. This makes it possible to set a temperature profile that is advantageous in the height direction, in particular for individual locally predefined drying levels. Between the drying levels, a temperature difference of at least 25 to 30 ° C and a maximum of 35 to 45 ° C is preferably set. It has been found that an advantageous drying process can be realized as a result, in particular when conveying the briquettes based on gravitational forces.
  • the dryer unit defines a plurality of drying levels, in particular in different height positions, in particular at least four drying levels, in each of which hot gas lines are arranged, each drying level being adjustable to an individual temperature level, for example by means of slides, flaps, flow regulators.
  • each drying level being adjustable to an individual temperature level, for example by means of slides, flaps, flow regulators.
  • the drying levels can specify discrete temperature values. Since the briquettes in the briquette dryer can be conveyed or shifted relative to the individual drying levels, in particular also continuously, the drying can also take place under comparatively homogeneous, constant temperature stress.
  • the briquette dryer or the entry system is connected to at least two of the furnace chambers, in particular two to six furnace chambers.
  • the entry system can serve at least two furnace chambers.
  • the entry system has a distributor for it.
  • the briquettes can be evenly distributed to the individual furnace chambers (in particular four to six chambers), supported by a geometry of the distributor which is preferably adapted for gravity-driven bulk material movements, eg by means of funnels, tubes, Filling.
  • the lock device can also be prevented that gas escapes.
  • the distribution of the briquettes on the furnace chamber (s) can preferably be realized without mechanically moving parts (points), in particular by means of so-called mandrels. In the respective lock device or arranged in front or behind mandrels can ensure a uniform, gravity-driven distribution of the briquettes. In this case, a transversely offset arrangement of the lock device can be realized, wherein the entry system has an outlet which is wider than half the width of a furnace chamber.
  • the most uniform possible distribution of the briquettes on the respective furnace chambers is also advantageous in that consistent process parameters can be ensured.
  • the operation of a furnace chamber is a sensitive interaction of various influencing factors. If the oven compartment is e.g. not completely filled, the manner of heat transfer changes, both in connection with a Rohgasabsaugung as well as with regard to the indirect supply of heat energy in the feedstock. If the furnace chamber is not completely filled, in particular the mass-specific heat input may increase.
  • the (respective) lock device has a double flap, by means of which at least two furnace chambers can be coupled to the briquette dryer or the device for Kokstrockkühlung. Gas tightness can be ensured between the individual components, in particular by means of suitable sealing means at the respective interface, which can be static, so that conventional sealing means such as e.g. Sealing rings can be used.
  • the double flap it is optionally possible to evacuate an internal volume of the chamber enclosed by the double flap, for example by means of a pump which is provided for evacuation or gas flow to further components of the furnace device.
  • the respective flap or a sluice gate valve can in particular have a square shape.
  • the furnace device can identify a double lock system below at least two furnace chambers, so that the coal / coke briquettes or the coke of at least two adjacent furnace chambers can be conveyed further, in particular into a dry cooling device.
  • the furnace device further comprises a discharge system comprising at least one lock device and is adapted for discharging briquettes or coke briquettes converted coal briquettes from the furnace chamber or from a Kokstrockenkühlung, in particular gravity-driven.
  • the respective lock device of the input / discharge system is preferably designed as a construction made of heat-resistant material with slip-promoting properties, for example with Teflon coating.
  • the lock device has, for example, slips with angles between 5 and 35 ° (in relation to the horizontal plane).
  • the lock device can be operated motor-controlled and can be operated manually (manual, push-button) or automatically (time or coke temperature controlled).
  • the corresponding engine control can, for. B. interact with a hydraulic, pneumatic, or electric drive.
  • the discharge system is preferably arranged below the (respective) furnace chamber or below a coking dry cooling.
  • the entry system and / or the discharge system can each be designed as a rocker, flap, lever, faucet, slide or pendulum construction.
  • a diverter or at least one mandrel may be provided, in particular in the manner of a triangular divider at the bottom of the briquette dryer or downstream of the oven chamber, whereby the briquettes can be distributed evenly by gravity into the sluices.
  • the furnace device downstream of the (respective) furnace chamber has a water-drivable coking dry cooling device which has at least one inlet and at least one outlet for cooling gas, in particular cooling inert gas.
  • the Kokstrockenkühlung allows efficient, but nevertheless gentle cooling.
  • the cooling can be carried out in countercurrent through the bed, in particular such that a continuous temperature profile is established, which is controllable in dependence on the amount of purge gas used.
  • the device for Kokstrockenksselung can be described as a solid heat exchanger with a steady temperature profile.
  • the device for coke dry cooling defines a cooling gas circuit for cooling gas flowing countercurrently through the briquette bed, in particular comprising at least one heat exchanger.
  • the device for dry cooling preferably comprises a heat exchanger configured for steam generation.
  • the means for Kokstrockenkschreibung may be coupled downstream of the furnace chamber to at least one of the furnace chambers, in particular by means of / a discharge system of the furnace device.
  • the Kokstrockenkschreibung means may be coupled to one to six furnace chambers.
  • the device for coking dry cooling has or defines a cooling gas circulation, in particular comprising at least one heat exchanger. This allows efficient use of recovered energy.
  • the (respective) furnace chamber in the conveying direction of the briquette in the (respective) furnace chamber in the conveying direction of the briquettes several temperature zones formed with increasing temperature, at least comprising a temperature zone at a first temperature level of 60 to 95 ° C and a temperature zone at a second temperature level of 95 to 125 ° C and a Temperature zone at a third temperature level of 125 to 200 ° C, and optionally one or two further temperature zones in between, each with the same temperature difference.
  • This allows a controlled heating, especially in a region of evaporation.
  • the device for dry cooling may comprise a cooling gas circuit with a heat exchanger, which heat exchanger is connected to a feedwater line.
  • the heat exchanger may consist of tube bundles and a steam drum, wherein the heat transfer from the cooling gas heated in the dry cooling device to feed water can take place in countercurrent, direct current or crossflow.
  • the device for dry cooling can have a plurality of cooling gas inlets and cooling gas outlets, which are arranged in such a way that the flow profile in the briquette bed which is flowed through can be adjusted by means of regulation of the respectively supplied or withdrawn volume flows.
  • At least one side of the (respective) furnace chamber in at least one of the heating walls formed a plurality of horizontal heating channels, which are preferably coupled to at least one vertical exhaust flue, and which are heated by burners, in particular at least three horizontal heating channels individually by at least one the burner.
  • a horizontal heating channel is to be understood a channel which does not extend or not appreciably in the vertical direction.
  • a horizontal heating channel extends substantially in a single height position or horizontal plane.
  • This older design or design of the heating channels has been found to be quite inflexible, and is at best optimizable to only one type of feedstock / coal (eg., Lusatian soft lignite). In this construction can not be sufficiently responded to different coal / feedstocks.
  • feedstock / coal eg., Lusatian soft lignite
  • an indirect heat transfer into the respective furnace chamber can take place.
  • an indirect heat transfer is to understand a heat transfer through at least one partition through, so based on heat conduction through the material of the furnace, in particular heat conduction in silica bricks.
  • the horizontal, individually heatable heating channels can define a degassing space or a degassing zone, in which strongly pre-dried briquettes are subjected to a comparatively high temperature stress or a comparatively high energy supply in order to be able to effect the degassing essentially in a lower section of the furnace chamber. Again, this can avoid Spülgasverkokung especially in an upper region of the oven chamber, in which the briquettes are still particularly sensitive to temperature stress.
  • the horizontal heating channels can each lead (in particular independently of one another) into a vertical exhaust gas duct, at which the gas can be taken off.
  • a drying circuit of the briquette dryer is coupled to at least one heating channel of the (respective) oven chamber. This allows use of the waste heat of the furnace chamber for tempering the briquette dryer. Flue gases from the heating of the furnace chamber can be used to maximize the cycles of the briquette dryer It has been shown that the temperature level of the flue gases removed is still high enough to operate the dryer circuits, which not only simplifies system configuration, but also increases energy efficiency Exhaust gases of the heating (or the flue gases) should have the lowest possible O 2 content, which can be ensured in particular by stoichiometric combustion, which makes it possible to prevent a risk of briquette fires.
  • the furnace device has at least one return line for gas emitted in at least one of the heating channels, which couples the (respective) heating channel to the briquette dryer.
  • the gas generated by burners can be fed into an exhaust gas collection channel or into a hot gas flue and from there via a connecting line to the briquette dryer.
  • a recirculation system By means of a recirculation system can be a crude gas treatment and further use of the treated gas, in particular as fuel for heating.
  • a drying circuit of the briquette dryer is coupled to at least one heating channel of the oven chamber. This can also achieve energy benefits.
  • At least one of the plurality of horizontal heating channels can be heated by a burner with flame monitoring arranged externally of the oven chamber, which burner is coupled to the respective heating channel, in particular by a burner operated by natural gas.
  • the energy input can be regulated in a relatively exact manner.
  • a temperature of at least 1000 ° C can be realized at the respective heating channel.
  • a very hot degassing zone can be set specifically in the lower region of the furnace chamber.
  • Burners with flame monitoring provide the advantage of high flexibility and accuracy with regard to tempering (heat input).
  • previously gas generation took place in separate arranged in front of the furnace chambers gas generators with appropriate piping to the furnace chamber.
  • the heating gas was generated by combustion of coal harmful to the environment.
  • mutually adjoining, mutually adjacent horizontal heating channels can be heated by burners arranged opposite one another. In this way, a comparatively homogeneous heat input can take place with respect to the total volume of the furnace chamber.
  • heating channels arranged on opposite sides at the same height position can be heated by burners arranged opposite one another. In this way, a comparatively homogeneous heat input can take place with respect to the total volume of the furnace chamber.
  • burners may be arranged diagonally opposite. At adjacent height positions of a furnace chamber, burners may be disposed at opposite edges / corners on one side of the furnace chamber. As a result, two-fold asymmetry can be generated, ie within the respective height level and with respect to adjacent height levels.
  • a heating channel is formed on at least one side of the (respective) furnace chamber, which extends meandering in several height levels and is arranged above at least two or three horizontal heating channels, and which is heated by at least one burner.
  • a temperature profile sloping upward in the height direction can be set in a simple manner.
  • a meander-shaped heating channel with inversion is formed, on which at least one of the reversals at least one measuring point is arranged, in particular at least one temperature and / or pressure measuring point. In this way, in particular the temperature profile can be measured.
  • a meander-shaped heating channel with at least one inversion is formed on at least one side of the furnace chamber, on which at least one of the reversals an observation point or a measuring point is arranged, in particular a externally operable, tightly closed observation point.
  • This provides a variety of options for monitoring and adjusting the operating parameters in the furnace chamber, particularly the temperature profile.
  • an observation point is arranged on at least one of the heating channels. The observation point allows visual control or visual insights. This provides options for monitoring and setting operating parameters.
  • a plurality of horizontal heating channels are provided in lateral heating walls of the oven chamber, in particular in opposite heating walls, of which the fourth fourth heating channel is meandering in several loops, wherein the fourth horizontal heating channel in the lower region of the furnace chamber at least one burner and in the upper Area of the furnace chamber connected to the briquette dryer line arrangement is connected.
  • a meander-shaped heating channel with at least one reversal is formed on at least one side of the (respective) furnace chamber, on which at least one of the reversals an observation point is arranged, in particular a externally operable, tightly closed observation point.
  • a temperature detection and monitoring can take place.
  • Several observation points can be provided in several height positions, in particular also to detect a temperature gradient. At the observation points, the condition of built-in stones can be inspected from the outside. Also, a measurement of the surface temperature of the stones may be made, e.g. Conclusions on emitted radiant heat allows.
  • At least one observation point is arranged on at least one of the heating channels.
  • one or more sensors can be installed there.
  • the respective observation point is accessible, for example, from the outside via a scaffold.
  • a plurality of horizontal heating channels are provided in lateral heating walls of the oven chamber, in particular in opposite heating walls, of which the fourth fourth heating channel is meandering in several loops, wherein the fourth horizontal heating channel in the lower region of the furnace chamber at least one burner and in the upper Area of the furnace chamber connected to the briquette dryer line arrangement is connected.
  • the temperature profile in the oven chamber can be set in a comparatively exact manner.
  • the highest temperatures can be achieved in a flexible manner, in particular to bring volatile constituents in the briquette to the desired contents of less than 10% by weight and bring the coking process to a close.
  • the number of three individually heatable horizontal channels has proven advantageous on the one hand with regard to the high degree of individual heating, and on the other hand with regard to the high heat energy which can be introduced thereby (for example, the desired briquette end temperature of about 1050 ° C.).
  • this type of heat input can take place over a relatively short distance (in the vertical conveying direction of the briquettes) by achieving furnace chamber temperatures of well over 1000 ° C. It has been found that this heat input can be ensured in a particularly expedient manner by means of a plurality of burners and a plurality of individual heating channels in the lower region (at the bottom) of the respective furnace chamber. With this configuration, it is also possible to respond flexibly to the final temperatures required individually per feedstock / coal grade. Our own investigations have shown that a combination of three horizontal heating channels and a meandering heating channel in relation to the achievable as homogeneous as possible temperature profile and the design effort provides many advantages.
  • a meander-shaped heating channel is understood to be a channel extending over a plurality of height levels, wherein the height levels are connected to one another by a loop-shaped or meandering course of the channel.
  • the channel can rise continuously in height.
  • the angle is in particular a maximum of 90 °.
  • a meandering heating channel on at least one side of the furnace chamber in at least one of the heating walls in a lower half, in particular a lower third at least three horizontal heating channels and above, in particular at least in an upper half or formed in a middle third, a meandering heating channel, which heating channels are individually heated by at least one burner, the meandering heating channel preferably reversing points with observation points arranged thereon or there measuring sensors.
  • the meandering heating channel preferably vertical passages are formed.
  • the meandering heating channel has reversal points with observation points with sensors arranged thereon or measuring there, in particular temperature sensors.
  • the meandering heating channel has at least one reversal point, at which a tightly closing observation point, which can be operated from outside in particular by means of a regulating slide, is arranged.
  • at least one observation point with a regulating slide (open, to, intermediate positions) for slide blocks and / or with measuring sensors is arranged on at least one of the heating channels, in particular on a turning point.
  • a manually accessible access channel for a regulating slide is coupled to at least one of the heating channels, in particular to the meandering heating channel.
  • the meandering heating channel has one or more vertical passages.
  • at least one adjusting element in particular a sliding block operable from the outside, can be arranged in each case.
  • the meandering heating channel is arranged to be shorted at one or more horizontal or vertical positions, in particular by releasing or blocking vertical passages.
  • At least one gas outlet for a gas discharge line is arranged on the (respective) oven chamber in at least three different height positions, the height positions in particular comprising a height position arranged at least approximately halfway up the furnace chamber.
  • the (respective) furnace chamber may have at least three gas outlets arranged in at least three different height positions of the furnace chamber, by means of which gas outlets at least three gases / gas species evacuable from the furnace chamber (a first gas and at least one further gas) can be provided.
  • the (respective) oven chamber has a plurality of gas outlets that can be arranged in at least one of the height positions at a plurality of locations, in particular circumferentially. This makes it possible to extract the gas in such a way that particularly little material transport takes place in the vertical or horizontal (or radial) direction. The coking process can thus be set even cleaner, more selective.
  • the gas outlets extend over a height corresponding to at least half the height of a furnace chamber, in particular over at least 50% of the height of the furnace chamber.
  • the withdrawal of the gas can take place in such a way that particularly little mass transport takes place in the vertical direction.
  • This also makes it possible to evacuate a wide range of different gases.
  • a first of the height positions is disposed in a lower third of the furnace chamber, and a second of the height positions is disposed in a middle third of the furnace chamber, and a third of the height positions is disposed in an upper third of the furnace chamber. This distribution along the height of the furnace chamber provides particularly many options when adjusting the coking process, or also with regard to the evacuation of usable gas types.
  • a first of the height positions seen from a bottom of a furnace chamber is arranged at a distance of 1 to 3 m, in particular 1.5 to 2.5 m, to a second of the height positions.
  • the first height position is arranged at a distance of 3 to 6 m, in particular 4 to 5 m, to a third of the height positions.
  • the second height position is arranged at a distance of 1 to 3 m, in particular 1.5 to 2.5 m to the third height position.
  • This particular distance is in many cases well suited to avoid Spülgasverkokung or unwanted temperature deviations. Although the distance may be less, especially at more than three height positions, but it has been shown that this distance provides a good compromise between plant / process engineering effort and simple design of the system.
  • the first height position is at a distance of 0 to 2m, in particular Im from the ground and / or the second height position at a distance of 0 to 0.5m with respect to the center and / or the third height position at a distance of 0 to 2m, in particular arranged from the head of the furnace chamber.
  • At least three height positions are defined, which are arranged in an upper half of the furnace chamber. This provides, in particular in an upper region of the furnace chamber, a high process reliability with comparatively fine adjustment with regard to evacuable gases or desired temperature profiles.
  • the height positions are each arranged at a distance from each other of at least 20 to 25% of the total height of the furnace chamber. This makes it possible to cover a large height range.
  • one of the height positions is provided at an upper end at the top of the furnace chamber, and a top gas emitted in the upper region of the furnace chamber is evacuatable from the furnace chamber via the corresponding gas outlet.
  • This makes it possible to set the temperature profile as precisely as possible, especially in the sensitive area of the lower temperatures of the furnace chamber.
  • the uppermost height position does not have to correspond to the uppermost end of the oven chamber, but may e.g. also be arranged slightly lower, depending on the feedstock and process management.
  • the furnace device is designed as a vertical chamber furnace, in which the briquette dryer is arranged above the (respective) furnace chamber. This makes it easier to feed briquettes.
  • the entire material flow can be regulated by means of a discharge system.
  • the temperature profile in the briquette dryer can be matched to the temperature profile in the oven chamber such that the desired temperature profile in the briquette dryer is set when setting the desired material flow in the oven chamber (briquette quantity / h).
  • the briquette dryer has or can define at least four drying levels or temperature levels. Then especially sensitive to changes in the material flow can be reacted.
  • a Kokstrockenkühlung / the device is arranged below the (respective) furnace chamber. As a result, the concept based on gravitational forces can be continued. The entire assembly becomes compact and the flow of material can be easily controlled.
  • the furnace device comprises a measuring device and a control device coupled thereto for controlling a drying of the briquettes in a temperature range of 60 to 200 ° C and / or in a humidity range of 1 to 5% by mass; and / or wherein the furnace device comprises a measuring device and a control device coupled thereto for setting a throughput or briquette material flow, in particular by means of a discharge system coupled to the control device.
  • the temperature regulation during drying and coking as well as the material flow can be regulated, in particular as a function of one another.
  • the (respective) furnace chamber or heating walls of the furnace chamber may be made of refractory silica material.
  • the bulk density of the briquettes in the furnace chamber may be in the range of 650 to 850 kg / m 3 , based on a density of 1,350 kg / m 3 of the respective briquette.
  • a process for the production of coke from at least one solid feedstock in particular from the group: brown coal, low-baking Hard coal, biomass, petroleum coke, petroleum coals; which feedstock is provided in the form of briquettes and is supplied to a vertical furnace chamber, in particular a coke oven, in particular to a furnace device as described above; wherein the briquettes are first fed to a briquette dryer, are dried therein according to a predefined temperature curve continuously according to the advance of the briquettes, in particular to at least two or three temperature levels in the range of 60 to 200 ° C, and then fed to the furnace chamber.
  • the briquettes can be pre-dried in a very vorgebare way pre-fabricate, and treat it gently.
  • the briquettes in the oven chamber according to the advance of the briquettes can be continuously tempered more.
  • a gradual increase in energy with the way allows an efficient process.
  • the energy supply can be increased in particular depending on the residual moisture content, for example by feeding individual heating levels with hotter gas, disproportionately hot gas in relation to the temperature gradient between previous heating levels.
  • Coking of lignite, low-grade coal or biomass is a process that should be controlled in a very precise manner, in particular to prevent the briquettes from softening (and disintegrating). Coking in the temperature range of the so-called "plastic zone" (in the case of certain lignites, in particular about 350 to 410 ° C.), in which the charge softens, should be avoided by adjusting the temperature control or heating curve.
  • the "plastic zone” In the "plastic zone", many of the feedstocks are subject to main degassing, so the structural composition of the briquette is most likely to be subject to change in the "plastic zone".
  • the "plastic zone” can be specifically assigned to a height position in the furnace chamber, in particular at the height of a meandering heating channel.
  • the evacuation of gases can also be carried out specifically in the area of the "plastic zone", in particular in combination with predefined temperature control within the furnace chamber or in combination with predefined indirect heating via individually controllable heating channels Height position, in particular the second height position of (further described in more detail below) gas discharge lines arranged especially in the "plastic zone", in particular centrally in this zone or at an upper end of this zone. At least one gas discharge line is then corresponding to a height position
  • the "plastic zone” is coupled to the furnace chamber, which effectively counteracts convective heating by rising raw gases.
  • the temperature profile can therefore be adjusted both by exhausting emission gases in the different height positions and by controlling / regulating the energy supplied by means of an external burner.
  • measures can also be taken in the meandering heating channel, such as e.g. enabling or blocking of vertical passages to reduce the energy input e.g. also in the "plastic zone" to be able to adjust.
  • briquettes are heated after drying in a briquette dryer according to their feed continuously stronger by tempering indirectly from the outside in the furnace chamber by at least one heating wall of the furnace chamber in a lower Half, in particular in a lower third at least one horizontal heating channel and above, in particular at least in an upper half or starting in a middle third, a meandering in several height levels extending heating channel are each individually fired by at least one burner. It has been found that in this configuration, the heating walls, even with indirect temperature control from the outside in a comparatively precise, homogeneous manner, a desired temperature profile in the furnace chamber is adjustable.
  • the series connection of the individual horizontal sections to a meandering heating channel allows for continuous heat transfer controlled cooling of the flue gases, with controlled over the height of the heating wall decreasing heat flux density.
  • the heat transferred indirectly via the heating channels can be supplied individually to the stocking (batch).
  • the ramp of the rising temperature in the briquettes can be set moderately so that evaporating residual moisture and escaping degassing products are gently expelled from the briquette with only moderate pressure.
  • the temperature or the indirect Heat energy supply are increased more, in particular to complete the degassing to a desired degree.
  • a weakening of the agglomerate structure of the briquettes is no longer to be feared thanks to the previously completed at least one first phase.
  • the determination of how high the rates of increase or how steep the respective temperature ramp can be selected, and in how many intervals with different temperature ramps along the height of the furnace chamber to be preferably adjusted, in particular by means of the device described herein flexible as a function of the selected feedstock or Temperature range are adjusted.
  • different steep temperature ramps are set in the furnace chamber, in particular a first temperature ramp with a slope in the range of 0.7 to lK / min and a second temperature ramp with a slope in the range of 2.5 to 3.5K / min, in particular at a limit temperature between the Ramps in the range of 300 to 350 ° C, in particular after a period of 5 to 7h, in particular exclusively by indirect temperature control on the one hand by means of the meandering heating channel and on the other hand by means of at least one horizontal heating channel.
  • the transition between the temperature ramps can be continuous or unsteady. It has been shown that a continuous transition can be realized, if only because of the continuous advance of the briquettes (slides down).
  • the heating of the briquettes in the briquette dryer is carried out at temperature curves of 0.4 to 2 K / min, in particular at 0.8 K / min.
  • the heat energy is preferably multistage (bottom hot, above less hot) introduced in heating cables of the briquette dryer.
  • emission gas from the furnace chamber and / or externally generated by burners exhaust gas can be used.
  • a temperature rise of 0.8 K / min is very advantageous.
  • this temperature ramp is also set in the oven chamber, in particular in an upper half or even in the two upper thirds. It has been found that this can be achieved by means of a meandering heating channel, in particular in a particularly effective manner in conjunction with an evacuation of gases at several height positions.
  • the briquettes in the briquette dryer are dried to a water content of less than 5% by mass before the briquettes are fed to the furnace chamber.
  • the briquettes can be treated very gently. It has been shown that it is advantageous as preparatory steps before the briquette dryer, when first heating and drying of the feed to 20Ma% water, and then heating and drying of the briquette compressed feed to HMa% water before the Briquettes are supplied to the briquette dryer, and before the briquettes are fed to the furnace chamber, in particular with a water content of less than 5Ma%.
  • the briquettes in the briquette dryer to water contents of 1 to 5Ma%, in particular 3Ma% dried and thereby or brought to a temperature of 120 to 180 ° C, in particular 150 ° C. This can ensure a particularly gentle treatment of the briquettes.
  • the heating of the briquettes in the furnace chamber takes place in particular with respect to the conveying direction of the briquettes or with respect to the vertical at temperature curves of 0.5 to 5 K / min, in particular at most 2 to 3 K / min; and / or wherein the briquettes in the oven chamber are heated for a period of 4 to 15 hours, in particular 6 to 9 hours; and / or wherein the briquettes, in particular with respect to the conveying direction of the briquettes or with respect to the vertical, of starting temperatures between 100 and 200 ° C or between 120 and 180 ° C, in particular from 150 ° C to final temperatures greater than 900 ° C, in particular heated between 900 and 1100 ° C in the furnace chamber.
  • the continuous process in the vertical chamber furnace (continuous process) enables a temperature gradient of eg 100 to 150 ° C per altitude meter.
  • a temperature ramp of 2 to 3 ° C can be passed through.
  • the coking process can also be used to further increase the (coke) compressive strength.
  • the compressive strength of eg 20 or 25 MPa can be increased by 30 to 50% to at least 35 MPa to 45 MPa.
  • the heating of the briquettes in the briquette dryer is carried out in several stages depending on the water content, in particular in two stages with the first stage to 15 to 10Ma%, especially H Ma% water and with the second stage to 1 to 5Ma% or to 2 to 4% by mass, in particular to 3% by mass of water. This allows to dry in a particularly gentle way.
  • the heating of the briquettes in the briquette dryer at several drying levels in different height positions is carried out in each case to a predefinable, individually controlled temperature level, in particular by means of one or more individually controllable drying gas circuits.
  • a predefinable, individually controlled temperature level in particular by means of one or more individually controllable drying gas circuits.
  • the regulation can take place via the volume flow, e.g. by means of sliders or flow regulators.
  • predrying Before the feedstock is pressed, predrying may also be carried out, in particular from 20 .mu.m% to HMa% water.
  • the heating of the feed can be carried out in several stages depending on the water content, in particular in two stages with the first stage to 20Ma% water and with the second stage to HMa% water.
  • the heating of the compacts takes place during the coking process to a maximum of 950 to 1100 ° C, in particular 1000 to 1050 ° C, preferably at most 1050 ° C. It has been shown that both the strength and the grain size of the coke depending on the feed at end temperatures above 1,100 ° C or even above 1,050 ° C were undesirably reduced and application of the coke in the blast furnace would be at risk.
  • high strength briquettes of feedstocks may be provided which may be considered as substitutes for prior blast furnace cokes.
  • the heating of the compacts takes place during the coking process such that the compacts during the coking process volume by 40 to 60%, in particular 50% shrink, and / or such that the compacts during the coking process by mass by 40 to 60%, in particular 50 % lose weight. It has been found that a volume change in this range is still tolerable in order to be able to ensure high strength values and good burning properties of the coke briquettes.
  • the pellets in the briquette dryer are dried to water contents of 1 to 5 .mu.m, in particular 3 .mu.m and thereby or by a temperature of 120 to 180 ° C, especially 150 ° C brought. This provides a good compromise between gentle and efficient / effective drying.
  • cooling gas in particular nitrogen to temperatures less than 200 ° C.
  • this provides an efficient process and, on the other hand, energy can also be recovered immediately after coking, be it for previous process steps or for other plants or processes. Condensation can be avoided in particular by the fact that the cooling takes place below 200 ° C, but the entire device remains temperature-controlled above the dew point.
  • one or more dew point sensors can be provided.
  • the discharge system can also accomplish the discharge from the device for dry cooling.
  • the cooling gas in particular nitrogen
  • the cooling gas can then be used in particular for steam generation.
  • a steam generation the use of steam for generating electrical power (relaxation in a steam turbine) can take place.
  • the electrical current may in turn be used to operate electrical consumers such as e.g. Pumps, compressors, blowers, locks, valves are used. Any surplus electricity can be fed into the local supply network.
  • use of the steam as heat tracing can be done, e.g. for the raw gas treatment of the white side of the furnace device.
  • use of the vapor as starting material can be carried out in a chemical process, e.g. Methanol synthesis (keywords: steam reforming / steam reforming, synthesis gas, H20 to increase the hydrogen yield (shift reaction), primary reformer).
  • coke in particular lignite coal coke with fixed carbon content Cfix of greater than 55% by mass is produced.
  • Cfix of greater than 55% by mass
  • coke in particular lignite coke with the smallest possible coke reactivity index (CRI) of less than 24% by mass and the highest possible strength index after reaction or a strength after reaction (CSR) greater than 65% by mass are produced.
  • CRI coke reactivity index
  • CSR strength after reaction
  • the CRI value is determined by heating the feed under predefined conditions to 1100 ° C. in particular, thereby determining the mass loss through outgassing.
  • the CSR value can be determined by spinning the outgassed material sample in a drum under predefined conditions, and is also quantified as a mass loss indication.
  • the coke downstream of the furnace chamber is cooled to temperatures below 200 ° C. by passing reaction inert cooling gas, in particular nitrogen, countercurrently through a briquette bed formed in a dry cooling device and downstream of a discharge system of the furnace device is evacuated from the device to dry cooling. This allows for a comparatively easy-to-control method in which energy can also be efficiently recovered.
  • the dry cooling device can be operated in a circuit, wherein the cooling gas accumulates due to Nachentgasungsvor réellen in the coke with combustible constituents such as H2 and CO.
  • the cooling gas can be evacuated from the bed and cleaned.
  • air-oxygen is added to the enriched cooling gas to combust the combustible components before the heat energy stored in the cooling gas can be transferred to feedwater in the heat exchanger.
  • the briquettes are converted into coke briquettes within a period of 4 to 15 hours, in particular 6 to 9 hours, on the conveying path from the briquette dryer to the (respective) oven chamber.
  • the (respective) oven chamber is operated continuously by the briquettes are continuously conveyed in the oven chamber (in particular down) and fed and discharged in batches, in particular via a lock device for at least two furnace chambers (double lock).
  • the bed can migrate continuously, and since input and discharge can be carried out batchwise, in particular 2 to 4 times per hour.
  • the rate of discharge can be used to control the residence time of the bed in the furnace chamber. It can also be taken into account that the mass and volume flow of the briquettes change in the course of the coking process, in particular due to Degassing and shrinkage.
  • the entry or supply can therefore be set at a higher mass flow than the discharge.
  • the briquettes are fed in the vertical direction by gravitational forces of the furnace chamber and / or discharged from the furnace chamber. This provides various advantages, especially with regard to self-regulating promotion and positioning of the briquettes within the device.
  • the feedstock or briquettes have or consist of low volatiles in the range of 28 to 45 mass% (waf) or 12 to 22 mass% (waf). Even with this particular composition, the advantages described above can be achieved.
  • the material flow of the feedstock is controlled or regulated by the (respective) oven chamber by means of a discharge system arranged below the (respective) oven chamber, in particular exclusively gravity-driven based on gravitational forces.
  • a discharge system arranged below the (respective) oven chamber, in particular exclusively gravity-driven based on gravitational forces.
  • gas is selectively withdrawn / evacuated from the furnace chamber at at least three different height positions. As a result, a desired temperature profile can be set or controlled even more effectively.
  • the object of the invention is to provide a device and a method with the features described above, which coking is also made possible by non-classical starting materials with process parameters that are as precisely adjustable as possible, in particular lignite and / or low-baking hard coal or biomass, in particular Vertikalhuntöfen.
  • the object can also be seen in preparing, providing and / or handling the non-classical starting materials in such a way that the entire process can also be regulated as precisely as possible or optimized in terms of energy, and that energy or by-products arising during the process can be used sustainably. It should be possible to proceed with the product obtained after coking as possible in a similar or the same way as before with classic feedstocks, eg, classic hard coal briquettes.
  • a Gasevakuieran Aunt for obtaining usable gases from a furnace device with at least one vertical furnace chamber in the coking of at least one solid feedstock from the group: lignite, low-baking hard coal, biomass, petroleum coke, petroleum coals; to coke, wherein the gas evacuator assembly is adapted for coupling to at least one of the vertical furnace chambers of the furnace apparatus; wherein the gas evacuation assembly comprises at least three gas exhaust ducts arranged in at least three different height positions of the respective furnace chamber adapted to be coupled in the at least three height positions to the (respective) furnace chamber, the gas evacuator assembly being arranged to selectively handle at least three selectively by means of the respective gas exhaust duct evacuated gas types (a first gas and at least one other gas).
  • this enables the use of byproducts formed during the coking, on the other hand exact temperature control and regulation and control of the reactions taking place in the furnace chamber, in particular by avoiding (flushing) gases which propagate in the vertical direction.
  • the selective handling can be done by coupled to the gas exhaust ducts / detachable pumps, valves, mixers of Gasevakuieranaku.
  • the withdrawal of the gaseous products can be temperature-dependent, in order to ensure liquid and gaseous products in high quality of the products and to be able to utilize them in particular from an economic and / or ecological point of view. It has been shown that the release of gaseous emissions in coal is done in a very specific manner depending on the coalification level of the coal at different temperature levels, and that this effect can be exploited if the furnace chamber is heated as precisely and homogeneously as possible at the respective temperature level. can be held. Both the arrangement of the heating channels and the arrangement of gas vents / gas outlets has an effect on the setting options here.
  • this can be deducted hydrogen. Methanol can be won.
  • the gas evacuation arrangement therefore contributes to a comprehensive, sustainable use of the input material, and to a very efficient overall process, in particular including coking. In this way, a protection of the briquettes in the upper region of the furnace chamber before hot gases from the lower region can take place.
  • the briquettes can be passed more precisely along desired temperature curves. Thermal stress is reduced. Purge gas coking can be avoided.
  • it can also be avoided, for example, that emitted tar vapors condense on briquettes at a different altitude.
  • the gas evacuation arrangement can be set up for the selective forwarding or further processing of the at least three selectively evacuated gases.
  • the handling of the gases does not necessarily have to be selective, but the gases can be further processed or used individually. This option makes it possible to react flexibly to the potentially usable emitted by-products, depending on the application.
  • the Gasevakuieran Aunt may also be adapted for selectively setting process parameters individually at a respective height position, in particular a specific negative pressure. As a result, the evacuation of byproducts or the flow path of emitted gases in the furnace chamber can be adjusted even more precisely even with comparatively few (for example only three) height positions.
  • the selective handling can also include a use of the evacuated gases in connection with a method for operating the furnace device described here, for example as a fuel / fuel gas burner for the furnace device.
  • the raw gases may e.g. used as fuel for burners on the dryer. In terms of energy, it is advantageous to provide a cycle for this purpose.
  • the gas evacuation arrangement has a plurality of gas discharge lines that can be arranged in at least one of the height positions at a plurality of locations, in particular circumferentially.
  • the flow path of emitted gases in the radial direction can also be set or controlled.
  • the gas evacuation arrangement extends over a height corresponding to at least half the height of a furnace chamber, in particular over at least 75% of the height of the furnace chamber.
  • the Gasevakuieranssen extends over a height of at least 2m to 3m in furnace chambers with a height of 4m, or at least 5m to 8m in furnace chambers with a height of 10m.
  • a first of the height positions seen from a bottom of a furnace chamber is arranged at a distance of 1 to 3 m, in particular 1.5 to 2.5 m, to a second of the height positions. This allows for selective evacuation in a main degassing zone, especially in the area of individual, individually fired horizontal heating channels.
  • the first height position is arranged at a distance of 3 to 6 m, in particular 4 to 5 m, to a third of the height positions. This provides a large sphere of influence with only comparatively few height positions.
  • the second height position is arranged at a distance of 1 to 3 m, in particular 1.5 to 2.5 m to the third height position. This improves the accuracy and selectivity of the evacuation with respect to each type of gas.
  • the first height position is at a distance of 0 to 2m, in particular Im from the ground and / or the second height position at a distance of 0 to 0.5m with respect to the center and / or the third height position at a distance of 0 to 2m, in particular arranged from the head of the furnace chamber. This distribution provides a good compromise between plant engineering effort and selectivity and effectiveness in avoiding vertical gas flows. In particular, a selective evacuation of gases in a main degassing zone is made possible.
  • the gas evacuation assembly for the gas exhaust ducts defines at least three height positions, at least two of which are located in an upper half of the furnace chamber. This also provides an effective arrangement for avoiding purge gas coking.
  • the respective gas discharge line or related gas fittings or flanges or seals can be designed specifically for the relevant temperature range.
  • a first gas discharge line or first fittings temperature resistant to at least 900 ° C, in particular to 1000 or 1100 ° C a second gas discharge line or second fittings temperature resistant in the range of 300 to 600 ° C, and a third gas discharge line or third fittings temperature resistant in the range of at least 150 to 300 ° C.
  • each Gas discharge line or fitting can be designed specifically for the respective gas type (in particular also with regard to corrosive resistance) or specifically for the respective temperature regime.
  • the materials of the lines can be selected accordingly.
  • the optimum compromise of, for example, material, cost, durability can be selected by the skilled person based on the particular type of gas to be handled.
  • the height positions are each arranged at a distance from each other of at least 20 to 45% of the total height of the furnace chamber. In this way, a broad height section of the respective furnace chamber can be covered, in particular in conjunction with a pressure and / or volume flow-dependent regulation of the evacuation.
  • one of the height positions is provided at the top of the furnace chamber, wherein the gas evacuation assembly comprises at least one port or at least one gas withdrawal conduit arranged and adapted for coupling to a corresponding gas outlet at the top of the furnace chamber.
  • the gas evacuation assembly comprises at least one of the following components for handling the evacuated gases from the (respective) furnace chamber: separate raw gas cooling, tar catchment / separation vessel, tar discharge device, electrostatic precipitator adapted for dust reduction, desulfurization unit.
  • the further processing of evacuated gas can be gas-specific and individual.
  • the discharge device especially gases evacuated from certain height positions, it can be avoided that tar condenses in the lines placed in the ambient atmosphere and causes blockages therein.
  • the Gasevakuieran Aunt a plurality of parallel arrangement provided in the same function gas exhaust ducts, which can be coupled in the same height position to different furnace chambers, wherein the Gasevakuieran Aunt comprises a mixer to which the equal-functional gas exhaust ducts are coupled / coupled.
  • This arrangement allows the further handling of the same types of gas from a plurality of furnace chambers. This makes the arrangement more compact and handling becomes easier.
  • the aforementioned object is also achieved by a furnace device having at least one vertical furnace chamber, in particular by a previously described vertical chamber furnace device, with a gas evacuation arrangement described above. At least one of the objects described above is also achieved according to the invention by a coke oven, in particular a vertical chamber oven, with a previously described gas evacuation arrangement.
  • the coke oven preferably has vertically aligned furnace chambers, which can be tempered in the vertical direction specifically with respect to a respective height position.
  • the above object is also achieved by a method for recovering gases from a furnace apparatus with at least one vertical furnace chamber in the coking of solid feedstock, in particular starting material from the group: brown coal, low-baking hard coal, biomass, petroleum coke, petroleum coals; to coke from the at least one vertical furnace chamber of the furnace device and to further handle the gases; wherein at least three different types of gas (a first gas and at least one further gas) are selectively withdrawn / evacuated from the (respective) furnace chamber at at least three different height positions of the furnace chamber and are selectively handled in subsequent process steps, in particular recycled, in particular by means of a previously described Gasevakuieran Aunt.
  • This provides benefits previously described.
  • the different gases can optionally be handled separately.
  • one (only) recyclable material can be recycled from two gases / gas types taken at different height positions.
  • the gases are in particular under the influence of temperature in the furnace chamber during the coking process resulting and rising upwards through the bed of raw gases.
  • the evacuated and handled gases / gas species may in particular be formed from one or more gases from the following group of gases: C 2 H 6, N 2, NH 3, CO, CH 4, H 2, H 2 S, CO 2, SO 2, C 2 H 2, C 2 H 4, C 3 H 6, C 3 H 8, in particular BTX (benzene, toluene, xylene) and other high hydrocarbons.
  • the evacuation takes place over a height corresponding to at least half the height of a furnace chamber in at least three height positions, of which at least two are arranged in an upper half of the furnace chamber, wherein the height positions each at a distance from each other of at least 20 to 45% of the total Are arranged at least three different types of gases from at least three different height positions each from a lower, middle and upper third of the furnace chamber.
  • a first gas in a temperature range of 150 to 300 ° C is selectively withdrawn, and selectively withdrawn another gas in a temperature range of 300 to 600 ° C, and another gas in a temperature range of 600 to 950 ° C or 700 selectively deducted up to 900 ° C.
  • This allows for the recovery of at least three selectively withdrawn gas types, on the other hand, but also in a very effective way, the avoidance of vertical convective heat transfer within the furnace chamber.
  • At least three different types of gases from at least three different height positions are each withdrawn from a height section over 20 to 30% of the height of the furnace chamber or from a lower, middle and upper third of the furnace chamber.
  • a first gas is selectively withdrawn in a first height position in a range of up to 2m below the head of the furnace chamber and another gas in a further height position in a range of 35 to 65%, especially 45 to 55% of the height the furnace chamber selectively withdrawn, and another gas in a further height position in one Range of up to 2m above the bottom of the furnace chamber is selectively subtracted, each with a furnace chamber with a height of at least 4 to 6m.
  • the handling of the at least three types of gas per gas type comprises an individual regulation of evacuated volume flows, in particular with regard to evacuated volumes. This can be influenced both on the composition of evacuated gases and on the temperature profile within the briquette bed.
  • at least one flow sensor can be provided on each gas discharge line.
  • the regulation also allows a targeted influence on possibly not completely preventable vertical gas flows. For example, a greater negative pressure can be built on a gas discharge line arranged further down than in a gas discharge line of a higher height position. Effect: A gas flow to vertical top can be counteracted, or the gas flow can even be reversed and used to influence the temperature profile in the briquette bed. In this context, it makes sense to individually measure the gas composition on each gas exhaust duct, in particular by means of at least one gas sensor or at least one gas analyzer (e.g., spectroscopically, chromatographically).
  • the (respective) furnace chamber from the (respective) furnace chamber withdrawn at least three different gases / gas species in the further handling chemical recyclables such.
  • gases / gas species such as methanol, di-methyl ether, olefins, humic acids or synthetic natural gas produced. Last but not least, this enables a sustainable, economic overall process.
  • At least one of the at least three different gases / gas types withdrawn from the (respective) furnace chamber is supplied as fuel to a burner which indirectly heats the furnace chamber.
  • the gas withdrawn for the burners may consist of the following components, in particular at least 97%: C2H6, N2, CO, CH4, H2, CO2.
  • the gas provided for the burner can be withdrawn at different height positions, in particular at three of the height positions.
  • a gas purification can take place, in particular with respect to BTX and high hydrocarbons. This improves the operation of the burner.
  • solid carbon coke coal (Cfix) of greater than 55Ma% is produced. The process makes it possible to provide high quality coke for wide use.
  • the reference quantity Cfix can also be defined as coke yield minus ash content.
  • a measurement in particular a temperature measurement, takes place in a meandering heating channel on at least one side of the oven chamber at points of reversal with observation points.
  • a regulation takes place in the meandering heating channel in at least one turning point, in particular by means of a regulating slide from the outside.
  • at least one heating channel carries out at least one measurement and / or at least one regulation by means of pusher blocks, namely at least one heating channel from the group of at least three horizontal heating channels and a meandering heating channel disposed above, in particular at a reversal point.
  • a short circuit or bypass takes place at one or more vertical passages of the meandering heating channel of the furnace chamber, in particular by releasing or blocking the vertical passages.
  • at least one adjusting element is arranged for regulation on one or more vertical passages of the meandering heating channel, in particular a sliding block actuatable from the outside.
  • At least one of the objects described above is also achieved by using a previously described gas evacuation assembly on at least one vertical furnace chamber for evacuating at least three types of gas from the furnace chamber to establish a vertical temperature profile within a briquette bed in the furnace chamber.
  • At least one of the objects described above is also achieved by using at least one gas species evacuated from a vertical furnace chamber by means of a previously described gas evacuation arrangement to provide fuel gas to at least one burner indirectly heating the furnace chamber.
  • a furnace assembly for producing coke briquettes comprising a gas evacuation arrangement described above and a furnace device, which furnace device on at least one side of the furnace chamber in at least one heating wall in a lower half, in particular a lower third at least one horizontal heating channel and above, in particular at least in an upper half or beginning in a middle third, a meandering in several Has height levels extending heating channel, which heating channels are individually heated by at least one burner, in particular by evacuated from the furnace chamber gas.
  • At least one of the objects described above is also achieved according to the invention by a process for producing briquettes from carbonaceous solid feedstocks, comprising both the drying of feed briquettes in a briquette dryer and the coking of the briquettes into coke briquettes in a furnace chamber, wherein At least three distributed over at least half the height of the furnace chamber height positions of the furnace chamber gas is evacuated, which gas is at least partially performed to heat the furnace chamber to the furnace chamber arranged burners.
  • This method can be carried out by means of a previously described furnace arrangement.
  • the raw material briquettes are passed through the respective furnace chamber in a period of 4 to 15 hours, in particular from 6 to 9 hours.
  • the raw material briquettes are heated from initial temperatures between 100 to 200 ° C, especially 150 ° C to final temperatures between 900 and 1100 ° C, in particular multi-stage.
  • the required heat can be generated in two laterally to the respective chamber arranged channels, which can be heated by a plurality of external burners, and transmitted indirectly through a stone partition into the respective furnace chamber.
  • 2 to 10 in particular 4 to 6 manhole chambers are connected together to form a furnace battery.
  • the respective shaft has a height of 3.5 to 10m, in particular a height of 5 to 8m.
  • the respective shaft has a width of 150 to 600 mm, in particular a width of 200 to 400 mm.
  • Binders can be added to the weakly-baked coal in a preceding mixing process, thereby increasing the adhesion or baking property of the carbon particles during the briquetting process. Due to their crucible coke properties, especially the charcoal is a good baking coal (classic "coking coal") .Also the so-called “Ess” and “Gas” coals are good baking coals All other types of coals are referred to in this description as low baking coals
  • the briquettes are also made from types of hard coal such as anthracites (fB ⁇ 12%), malt coals (12% ⁇ fB ⁇ 19%), gas coals (28% ⁇ fB ⁇ 35%), gas flame coals (35% ⁇ fB ⁇ 45 %) or alternatively may consist of a mixture of these types of coal, optionally also using high quality fat (coke) carbons (19% ⁇ fB ⁇ 28%). These percentages, based on standards for carbon species, allow even more specific assignment.
  • hard coal such as anthracites (fB ⁇ 12%), malt coals (12% ⁇ fB ⁇ 19%), gas coals (28% ⁇ fB ⁇ 35%), gas flame coals (35% ⁇ fB ⁇ 45 %) or alternatively may consist of a mixture of these types of coal, optionally also using high quality fat (coke) carbons (19% ⁇ fB ⁇ 28%).
  • the raw material can be comminuted in a perforated disc roller mill to pellets, in particular with a grain size of 0 to 2mm. It has been found that pellets / grains produced by means of a perforated disc mill are particularly easy to bond (they cake easily) and therefore simplify the downstream briquetting process (compression).
  • This compacting process is preferably carried out in a molding channel stamp press. It has been found that it is possible to realize particularly pressure-resistant briquettes by means of a channel template geometry in the manner of a Venturi tube with a cross-sectional constriction and an expansive cross-sectional enlargement. Other types of press could not deliver comparably good results.
  • briquettes in flat cylindrical form provide particularly good strength values, be it before or after coking.
  • a ratio of briquette diameter to briquet height of 1 to 5, in particular 2 to 3 gives good results also with regard to the heating and coking process.
  • the briquette preferably has a diameter of 20 to 100 mm.
  • the briquette is produced in particular from coal grain sizes between 0 and 2mm. Should it be shown that the required strength can also be achieved by another die or another type of press, the briquettes can optionally also have a different geometry, such as, for example, cubes, cuboids, platelets, mussels, pillows , spherical or egg-shaped geometries. In previous experiments, however, the best experiences were made with the puck shape.
  • the pressing takes place in particular at pressures of 120 to 150 MPa, in particular at 140 MPa.
  • the pressing takes place in particular at temperatures between 60 and 100 ° C.
  • the compression takes place for a period of up to 15 seconds.
  • At least one coking aid is added to the briquetting process (during pressing), in particular to improve the efficiency of the subsequent coking process.
  • Coking auxiliaries can be selected individually or in combination, in particular from a group of coking aids which have hitherto been regarded as useful in connection with conventional starting materials.
  • Back (adhesive) and coking auxiliaries are preferably added to the raw material before the pressing and coking process in single or multi-stage mixing processes, in particular in order to improve the quality of the coke produced or to facilitate the briquetting process from low-baking coals.
  • adjuvants are preferably added before briquetting at temperatures in the range of 30 to 120 ° C.
  • the auxiliaries can be selected in particular from the following group, optionally in combination: molasses, sulfite liquor, sulfate liquor, propane bitumen, cellulose fibers, HSC (High Conversion Soaker Cracking) residue, HSC / ROSE (Residue Oil Supercritical Extraction) mixed residues from the oil industry.
  • molasses sulfite liquor, sulfate liquor, propane bitumen, cellulose fibers
  • HSC High Conversion Soaker Cracking residue
  • HSC / ROSE Residue Oil Supercritical Extraction
  • the subsequent briquetting takes place in particular in the temperature range between 40 to 90 ° C, in particular between 55 to 65 ° C.
  • the briquettes may be placed with a crane above a main dryer and may pass through the main dryer, through the coking pit and further into a coke drying cooling device. It has been shown that it is advantageous to gently dry the briquette in a main drying process after agglomeration to water contents of 2 to 4% by mass.
  • the main drying process of the briquettes is done in particular by roof dryer units and serves to further reduce the water content of the briquette of approx. 20Ma% to about 3Ma%. In this way it can be ensured that heat transferred into the chamber is not dissipated to a high proportion for water evaporation, which according to experience can also lead to breaking up of the briquette.
  • the main drying process takes place in particular in two stages, but can also take place in one or more stages.
  • the drying medium used is preferably hot exhaust gas / raw gas, which results from combustion processes in heating channels of the oven chamber arranged below the dryer and can be conducted upwards into the roof-shaped channels.
  • a main drying unit configured for main drying may be coupled to an external burner with flame monitoring, by means of which additional waste gas for all or several or even only one drying stage can be provided.
  • the main drying unit and the respective furnace chamber can be separated from one another by a hermetically sealable, in particular airtight, lock system.
  • the lock system can be coupled in particular in the form of a double flap to at least two furnace chambers.
  • the raw material / feedstock (or the briquettes) is preferably heated in the coking shaft (or furnace chamber) located below the main dryer by using a raw material-specific temperature regime.
  • a raw material-specific temperature regime provides advantages: In a first stage, in particular over a period of 0 to about 4 to 7 h, the briquettes are heated to a temperature range of 300 to 400 ° C, working with a temperature increase of 0.75 to 0.9 K / min becomes . In at least one further step, in which the briquettes are brought into the temperature range of 300 to 1100 ° C, is heated at a heating rate of 2.6 to 3 K / min.
  • the quality level defined by these limits could not be achieved so far with the described inferior coal qualities.
  • previous methods and devices have led to crack formation in the briquette or even complete destruction of the briquette form. Mass and volume changes can take place here in particular in the same ratio. Thanks to the method described here, the briquette shape (puck shape) can be maintained, with the result that pressure loss, heat transfer, flow profile and other process parameters remain predefinable.
  • the respective furnace chamber consists in particular of refractory silica material.
  • Heating channels can be arranged integrated into the wall on the side of the respective furnace chamber, in particular on both sides.
  • the heating channels can be fired by at least one, preferably four, external burners.
  • the burners are in particular coupled one above the other to horizontal heating channels.
  • the exhaust gases or flue gases from the heating walls can also be utilized energetically, including optionally a flue can be supported by a flue gas fan.
  • three burners are provided / coupled to three lower or lowest horizontal channels.
  • the lower three channels run horizontally to the opposite side of the oven chamber and go there in a respective upward leading vertical heating shaft. It has been found that the concentrated arrangement of three burners in the lower part of the shaft / furnace can form an intense heat source there, which results in temperatures of> 500 ° C. forming in the chamber, which are required for coke formation .
  • a meandering upwardly leading channel in the heating wall is formed above the lower or lowermost horizontal channels, in particular as a fourth channel (counted from below).
  • a burner can also be coupled to the meandering channel. It has been shown that an advantageous heat distribution can be ensured by means of this meandering channel, in particular in the vertical direction.
  • the exhaust gases produced by the corresponding (in particular fourth) burner can slowly cool down, whereby a gradual heat transfer into the charge / bed of the briquettes can be ensured in the vertical direction.
  • a step-shaped heat transfer provides various advantages, be it energy benefits, be it advantages in terms of dimensional stability of the briquettes or generally with regard to a gentle coking process.
  • the burners can in particular be fired with natural gas and / or coke oven gas from the coking shaft. Thanks to the configuration described above, it can be dispensed with to provide a previously used expensive generator gas system in front of the respective furnace chamber for generating combustion gas from coal, which would also disadvantages in terms of emissions.
  • resulting high-calorific gases are taken at 1 to 5 sampling points in different height positions, ie evacuated from the chamber and fed to further utilization.
  • a nozzle with a predetermined angle can be provided.
  • this measure has the advantage that the gases released in the individual stages of the coking process can be fractionally evacuated from the coking process and can thus be fed to a specific gas treatment or converted into chemical recyclables. Fractionated extraction is to be understood as a removal at different height positions and different types of gas or gas compositions. It has been shown that by means of a (per input material or type of coking process) predefinable spacing of the sampling points can make a very selective pre-selection with regard to the composition of the extracted gases.
  • one, several, or even all sampling points in the vertical direction are at least 50% above the manhole / floor outlet of the respective chamber.
  • This has advantages not least with regard to the arrangement of a pending zone in front of the discharge system.
  • raw gases can be sucked out of the upper areas and returned to the shaft via the lower "suction.”
  • the respective lower gas discharge line can also be converted into a gas supply line, thus allowing gases to be conducted locally over hot briquettes, which results in a quality-increasing effect leaves.
  • the following describes aspects related to the sustainable use of energy spent or given off in coking.
  • the use of the flue gases from the heating or from the coker for the circuits of the dryer can be done.
  • a controlled partial removal for dehumidification of the circulating drying gases take place.
  • the generation of steam can be carried out, in particular for steam stations for heating apparatus, pipelines, fittings.
  • steam can be recovered or used for raw gas treatment in the form of process steam.
  • a supply to a waste heat recovery unit can take place, or a supply of hot flue gases to a dry cooling device.
  • a gas-tight discharge system is arranged below the (respective) furnace chamber, through which the warm coke can be transferred into a dry cooling device.
  • the discharge system can be formed like a shaft.
  • the discharge system may be configured to receive the amount of coke of two adjacent chambers.
  • the coke is cooled from a temperature level in the range of> 900 ° C to a temperature level below 200 ° C, in particular by introducing cold inert gas, in particular introducing from below without addition of water.
  • a vacuum system may be provided, in particular in the form of a blower, which vacuum system may be coupled to the dry cooling device and / or the heat exchanger.
  • coking temperatures below the dry cooling device of less than 200 ° C can be realized. It can be used for coke withdrawal, e.g. a rocker or pendulum construction can be realized. This cold cold gas can be introduced via a free bed surface in the dry cooling device.
  • At least one of the objects described above is also achieved by a furnace assembly for producing briquettes, comprising a previously described furnace device and a Gasevakuieran extract described above, which is coupled by at least three gas discharge lines in at least three height positions to at least one furnace chamber of the furnace device.
  • At least one of the above-described objects is also achieved by a method of making briquettes of carbonaceous solid feedstock comprising both drying feedstock briquettes in a briquette dryer along a predefinable first temperature ramp and coking the briquettes into coke briquettes in one Furnace chamber along at least one predefinable second temperature ramp, wherein for adjusting the second temperature ramp to at least three over at least half the height of the furnace chamber distributed height positions of the furnace chamber gas is evacuated.
  • the method is carried out by means of a previously described furnace arrangement.
  • the briquettes are pre-dried with a water content of 10 to 12Ma% provided for the briquette dryer, and then there is a drying on less than 5% by mass before the briquettes are fed to the oven chamber. This allows a particularly gentle treatment of the starting material.
  • an adjustable temperature profile over the height of a furnace device according to an embodiment according to an embodiment comprising the furnace device according to an embodiment;
  • FIG. 1A an oven apparatus 10, in particular a coke oven with a plurality of vertical chambers 11 is shown.
  • Feedstock 1 in the form of briquettes 5 is supplied by means of a feed unit 10.1 a briquette dryer 15 and preheated therein, which briquette dryer 15 is disposed above the furnace chambers 11.
  • the pre-dried starting material 5 can then be coked by indirect heating via heating walls 12 of the furnace chambers 11, in particular according to an exactly predefinable temperature profile, as explained in more detail below (in particular FIGS. 4A, 4B). After coking, drying can take place.
  • a device for Kokstrockenkühlung 19 is coupled to the bottom of the respective furnace chamber 11.
  • the feeding and removal of the feedstock 1, 5, 6 can be done in an elegant manner by means of an entry system 16 and a discharge system 17 each comprising one or more locks 16.1, 17.1, in particular gravity-driven.
  • a collecting device 17.9 coked and dried briquettes 6 can be collected and stored.
  • the furnace device 10 has, for example, four to six vertically aligned, vertically loadable furnace chambers, which are each heated by two heating walls along the yz plane laterally (in the view of FIG. 1A, ie, from the right and left). The heat transfer takes place indirectly via the heating walls.
  • FIG. 1B indicates a temperature profile T over the height z, in which case six phases are emphasized.
  • phase I Drying takes place in the briquette dryer, here indicated schematically with a linear temperature profile, which temperature profile can optionally also not be linear.
  • phase II the feedstock is transferred into the respective furnace chamber, and thereby at least approximately at the final temperature of the phase I. held.
  • the entry system can optionally be tempered or have a heating device.
  • phase III is shown schematically that the dryer 15 may be coupled to a plurality of chambers 11.
  • the device for Kokstrockenkühlung 19 may be coupled to a plurality of chambers 11.
  • FIG. 1B indicates a temperature profile T over the height z, in which case six phases are emphasized.
  • phase II the feedstock is transferred into the respective furnace chamber, and thereby at least approximately at the final temperature of the phase I. held.
  • the entry system can optionally be tempered or have a heating device.
  • phase III In phase III.
  • a first coking phase is indicated, with a comparatively low temperature increase or a flat temperature ramp. This allows a particularly gentle heating and gentle expulsion of foreign substances / gas components done.
  • the temperature ramp may be steeper, especially since the feedstock has already emitted a majority of the emissive impurities.
  • the energy supply can be intensified without overstressing the feedstock.
  • phase V the maximum final temperature for coking has been reached and cooling in the coke dry cooling can take place.
  • the temperature profile in phase IV and V. is here indicated in each case schematically linearly, and can optionally also be set non-linear, depending on the application.
  • phase VI the coked briquettes are available or accessible for further processing in any subsequent process steps.
  • the heating can initially be carried out in a very gentle manner at a temperature ramp in the range of 0.8 K / min, in particular monotonically increasing without Un continuities up to a temperature in the range of 320 ° C or over a period of up to 6h (Phase IV. ). Thereafter, the slope of the temperature ramp can be significantly increased, in particular values in the range of 2.8 K / min, in particular monotonically increasing without discontinuities up to a temperature in the range of 1050 ° C or over a period of up to 5 or 6 h (Phase V.).
  • the transition can also be continuous, continuous.
  • the upper (first in the material flow direction) temperature zone (for example, the upper, first 4m of the furnace chamber, as seen in the material flow direction) can be realized with the moderate temperature ramp by means of at least one meandering heating channel.
  • the lower temperature zone (second in the material flow direction) temperature zone (for example, the lower 2m of the oven chamber) can be realized with the steeper temperature ramp by means of at least three individually fired horizontal heating channels.
  • FIG. 2 shows an overview of the relationship between individual plant components of a furnace arrangement 50 and a carbonization arrangement 80.
  • Feedstock / feedstock 1 is fed to a plant component for compression / compaction (in particular two-stage agglomeration), and leaves this plant component as pellets or coal briquettes, in particular in slice or puck shape. After coking then there are coke briquettes 6.
  • the coal assembly 80 includes not only at least one previously described furnace apparatus 10, but also a gas evacuation assembly (FIG. 6) and / or the plant component for compacting.
  • the individual plant components can be connected to each other in a clever way, especially for the purpose of high energy efficiency.
  • a return system 18 is provided with at least one return line from the (respective) furnace chamber back to the dryer 15, so that exhaust gas G2 from a respective furnace chamber 11 can also be used for controlling the temperature of the dryer 15.
  • raw gas Gl can be withdrawn by means of a gas evacuation arrangement 30 and handled for further / reuse.
  • Fig. 3 shows details of the dryer 15.
  • each heating elements 15.4, 15.5 are provided in particular hot gas lines at different temperatures.
  • the upper heating elements 15.5 are less hot than the lower heating elements 15.4, and may be formed for example by a return line of a circuit.
  • hot gas of a hot gas cycle 15a can be supplied to the lowest drying level 15.8, in particular with a particularly high energy content.
  • temperature and humidity sensors can be provided in the briquette dryer, in particular at least two levels.
  • the individual sensors may be components of a measuring device 14 coupled to a control device 20.
  • one or more temperature sensors 14.1, H20- Sensors 14.2, and / or pressure sensors 14.3 be provided whose position is indicated here only schematically.
  • the dryer 15 comprises at least one reservoir 15.1, in particular dimensioned for continuous gravity-driven operation.
  • a heating device 15.2 of the reservoir can be formed by the above-described lines 15.4, 15.5 or optionally comprise further heating elements.
  • the lines are preferably arranged below roof elements 15.3, around which the briquettes can slide down.
  • the drying circuits 15.7, 15.8 can in each case in particular comprise two drying levels 15.6, wherein the respective upper of the two drying levels 15.6 is the cooler level in which extraction of drying gas can take place, which heat energy has already delivered.
  • the arrangement has at least two inlet and two Absauworkingen, wherein the temperature and amount of drying gas can be set individually on the respective introduction levels.
  • Each drying cycle can be regulated at least with regard to the volume flow and the inlet temperature of the hot gas.
  • a uniform distribution of the drying gases over the individual lines or roofs of a plane can be used, for example. via valves, manually adjustable perforated discs or the like.
  • the individual lines or roofs can be arranged offset from one another.
  • a vertical or diagonal distance between the conduits is preferably at least a factor of 6 of the diameter of the briquettes.
  • a heating wall 12 is shown in a side view or in a sectional plane yz.
  • Three horizontal heating channels 12.1 each extend in a single height level and each lead into a vertical exhaust flue (exhaust line) 12.3, and are each fired individually by a burner 13.
  • train is used exclusively for a line oriented vertically in the direction of conveyance of the coal / coke briquettes, in particular for exhaust pipes, ie not for horizontal heating channels
  • a burner axis 13.1 in each case coincides, at least approximately, with a longitudinal axis of the respective channel 12.1
  • a meander-shaped heating channel 12.2 extends over a plurality of height levels above the horizontal single-plane channels, and therefore also has a multiplicity of reversals or reversal points 12.21
  • the meander-shaped heating channel 12.2 is also fired by a burner 13.
  • the briquettes supplied to the oven chamber are first tempered very carefully, and further down in the area of the horizontal single-plane channels 12.1 they are subjected to a continuously increasing energy supply.
  • At least one observation point 12.22 or measuring point for measuring sensor 14 may be provided on the respective channel 12.1, 12.2, in particular also at the reversal points 12.21.
  • the meandering heating channel 12.2 may have one or more vertical passages 12.5.
  • the vertical passages 12.5 allow, in a sense, a short circuit in terms of power supply and vertical or horizontal power distribution.
  • the vertical passages 12.5 can be switched for example by means of pusher blocks 12.9 (open, closed, intermediate positions).
  • measuring sensor 14.4 can also be provided specifically in the observation point.
  • a particularly manually accessible access channel can be provided there within the heating wall.
  • the arranged in front of the end faces of the heating walls vertical flues may have connections to each Bankkanalabintroductory the fourth heating channel, in particular to allow additional heating control as a function of the feedstock used.
  • the heating channels slide blocks 12.9, in particular from the fourth heating channel from below, there is the possibility to divert the exhaust gas before also in the exhaust flue or at certain horizontal positions hotter directly upwards.
  • a meander channel 12.2 can thereby be short-circuited at one or more horizontal or vertical positions. This makes it possible to heat the individual heating channels according to a desired, individually predefinable temperature profile, be it in the vertical or horizontal direction.
  • critical temperature ranges for example, 350 to 410 ° C or 410 ° to 470 ° C can be specifically avoided, or at least limited to a short, locally small temperature zone.
  • the positioning of the pusher blocks can be done for example via regulating slide at observation openings 12.22.
  • the vertical passages 12.5 may be matrix-shaped distributed over the heating channels, so that a variety of options can be realized when setting / regulating the energy input into the oven chamber.
  • a control device can communicate not only with all burners, but also with valves or flaps for air supply, and / or with Valves or flaps on the respective vertical passage or with a device for relocating stones for opening and closing a respective vertical passage.
  • observation points 12.22 in particular equipped with sensors 14.4, it is possible to monitor the temperature of the furnace chamber and to optimize / regulate in a relatively accurate manner.
  • FIG. 4B is a plan view of the xy plane.
  • FIG. 4C shows an xz side view. Gas outlets 12.6, 12.7, 12.8 in three different height positions are already indicated in FIG. 4C, which is shown in FIG. 6 is explained in more detail.
  • At least four external burners 13, which are aligned in the direction of the x or y axis and arranged alternately opposite one another in front of and behind the chamber 11, ensure an optimum heating regime.
  • the three lower heating channels 12.1 each extend in (only) one height position / height level and are each heated separately from an individual burner. From the three lower heating channels exhaust gas is passed directly into the extending in the vertical direction flue 12.3.
  • the horizontal heating channels 12.1 are aligned in particular parallel to each other and perpendicular to the corresponding vertical exhaust flue 12.3.
  • the lower part of the furnace is preferably no longer heated and is intended for the Ausgarung of the coke and the pre-cooling of the coke (about Im).
  • This part can be described as a stop zone, which can support a complete through-cooking and complete outgassing, which has a positive influence on the coke quality.
  • the briquette dryer is located above the oven chambers and can be fed via the (vertical) flues with exhaust gas from the respective burner.
  • This waste gas can be used as a drying medium in two separate drying circuits within the briquette dryer, referred to herein as the dryer precursor and dryer primary stage.
  • two drying circuits can be provided, in particular each fed by heat energy from Burners of the oven device. Both circuits can optionally be equipped with additional, external burners, in particular for the purpose of redundancy or more flexible settings.
  • Hot exhaust gas from primary heat generation may be provided by at least three external burners connected in particular to three horizontal heating ducts arranged at the bottom of the respective furnace chamber.
  • Hot waste gas from secondary heat generation may be provided by at least one external burner connected to a meandering heating channel located above the horizontal heating channels.
  • a gas circuit 19.5 is operated in which the coked briquettes 6 are cooled countercurrently in a cavity 19.7, the gas being passed through at least one Inlet 19.9 is passed into the cavity and is evacuated again by at least one outlet 19.8.
  • the outlet is located just below the oven chamber 11 and in contrast sealed off by baffles or protruding walls.
  • Centric within the cavity 19.7 at least one flow-inhibiting roof or a Gasumleitmaschine 19.6 is arranged. This allows the flow profile to be adjusted. In particular, it can be avoided that a main energy or mass transport is formed in the center of the cavity 19.7.
  • the coke drying cooling is arranged "precisely" under the furnace chamber, ie the cavity of the dry cooling device can have the same cross-sectional profile as the furnace chamber, which promotes direct, gravity-driven conveyance of the briquettes and can simplify continuous operation In particular, the transition is seamless in that there is no physical separation between the oven chamber and the dry cooler.
  • At least one in the radial direction, in particular centrally arranged roof or a Gasumleitmaschine 19.6 can ensure that the cooling gas is divided homogeneously in the radial direction and in particular is also conducted in a homogeneous manner to the outlets 19.8.
  • 6 shows a furnace arrangement 50 comprising a gas evacuation arrangement 30 with one or more gas discharge lines 31 for a first height position, which can be coupled to the respective furnace chamber 11 via a coupling or a connection 31.1.
  • one or more gas discharge lines 33 are provided for at least one further height position, here for a second and a third height position, likewise in each case comprising a coupling 33.1.
  • a plurality of mixers 35.1 and at least one pump 35.2 are provided for further handling of the evacuated gases.
  • the raw gas can be extracted on at least three levels, each individually for each oven chamber: via a riser in the furnace roof (top height position), by one or more arranged on a predefined height position of the furnace chamber ports and further by one or more vertical exhaust trains, especially within the respective heating wall (middle height position), and further by one or more arranged on a predefined height position of the oven chamber ports and further by one or more vertical exhaust trains, in particular within the heating wall (lowest height position).
  • the withdrawn raw gas can be cooled and collected via separate / separate raw gas manifolds and then combined in one or more Rohgassammel Oberen. It has been shown that, in the case of a direct exhaust gas extraction (in particular immediately downstream of a lock device of the briquette introduction system), the risk of a transfer of raw gas from the furnace chamber into the pre-dryer can be reduced, in particular due to the negative pressure that arises here. This can further increase the quality.
  • Heating element in particular line / hot gas line with first temperature 15.5 heating element, in particular line / hot gas line with second temperature

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Drying Of Solid Materials (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)

Abstract

L'invention concerne un système d'évacuation de gaz (30) destiné à obtenir des gaz lors de la cokéfaction, en coke, d'au moins une matière de départ solide du groupe consistant en le lignite, la houille à faible pouvoir cokéfiant, la biomasse, le coke de pétrole, le charbon de pétrole, le système d'évacuation de gaz étant conçu pour couplage à au moins une chambre de four verticale (11) d'une installation de four (10) ; le système d'évacuation de gaz présentant au moins trois lignes d'extraction de gaz (31, 33) pouvant être disposées à différentes positions en hauteur dans la chambre de four, qui sont conçues pour couplage à la chambre de four sur les au moins trois positions en hauteur, le système d'évacuation de gaz étant conçu pour la manipulation sélective d'au moins trois types de gaz, évacués sélectivement, chacun par sa ligne d'évacuation de gaz. L'invention concerne en outre un procédé pour l'obtention de gaz, ainsi que l'utilisation d'au moins un type de gaz récupéré à l'aide d'un tel système d'évacuation de gaz.
EP18716213.6A 2017-04-13 2018-04-04 Dispositif et procéde pour l'obtention de gaz lors de la cokéfaction d'une matière de départ contenant du charbon, et utilisation Pending EP3609980A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102017206460.9A DE102017206460A1 (de) 2017-04-13 2017-04-13 Vorrichtung und Verfahren zur Gewinnung von Gasen bei Verkokung von kohlehaltigem Einsatzstoff sowie Verwendung
PCT/EP2018/058529 WO2018188998A1 (fr) 2017-04-13 2018-04-04 Dispositif et procéde pour l'obtention de gaz lors de la cokéfaction d'une matière de départ contenant du charbon, et utilisation

Publications (1)

Publication Number Publication Date
EP3609980A1 true EP3609980A1 (fr) 2020-02-19

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EP18716213.6A Pending EP3609980A1 (fr) 2017-04-13 2018-04-04 Dispositif et procéde pour l'obtention de gaz lors de la cokéfaction d'une matière de départ contenant du charbon, et utilisation

Country Status (6)

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EP (1) EP3609980A1 (fr)
JP (1) JP2020518683A (fr)
CN (1) CN110520506B (fr)
DE (1) DE102017206460A1 (fr)
UA (1) UA125095C2 (fr)
WO (1) WO2018188998A1 (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112226240B (zh) * 2020-09-21 2021-05-18 大连理工大学 煤制备兰炭的装置与方法
CN112708434A (zh) * 2021-01-08 2021-04-27 中国科学院青岛生物能源与过程研究所 一种模块组合单元列装连续式低阶煤热解炉
CN115418241B (zh) * 2022-08-19 2024-02-13 湖北沃凯工程技术有限公司 一种兰炭熄焦转运系统

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GB191012923A (en) * 1910-05-27 1911-05-11 Arthur Owen Jones Improvements in or connected with Coke Ovens.
GB136880A (en) * 1918-12-19 1919-12-19 William Everard Davies Improvements in or relating to the Carbonisation of Fuel by Vertical Coke-ovens and the like.
DE366273C (de) * 1920-07-02 1923-01-03 Henri Hennebutte Senkrechte Retorte fuer fraktionierte Trockendestillation
FR533765A (fr) * 1921-04-05 1922-03-10 Low Temp Carbonisation Ltd Perfectionnements au montage des cornues
DE491312C (de) * 1929-03-15 1930-02-08 Karl Sassenhoff Verfahren zum Verkoken von Brennstoffen in mittelbar beheizten Verkokungskammern
AT134280B (de) * 1930-06-25 1933-07-25 Gabriel Szigeth Verfahren und Einrichtung zur Entgasung von Braunkohle in senkrechten, außenbeheizten Retorten oder Kammern.
DE658299C (de) * 1935-10-23 1938-04-02 Hermann Niggemann Dr Vorrichtung zum getrennten Absaugen der Aussen- und Innengase aus waagerechten Kammeroefen
US4115202A (en) * 1975-02-22 1978-09-19 Firma Carl Still Apparatus for producing non-abrasive coke forms from brown-coal briquets
US4165216A (en) * 1977-03-23 1979-08-21 Enerco, Inc. Continuous drying and/or heating apparatus
JPS5485201A (en) * 1977-12-21 1979-07-06 Kansai Coke & Chemicals Method of manufacturing molded coke and inner thermal vertical carbonization furnace therefor
DE3123141A1 (de) * 1981-06-11 1982-12-30 Krupp-Koppers Gmbh, 4300 Essen Verfahren und vorrichtung zum betrieb einer kokereianlage
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JPH05263078A (ja) * 1992-03-23 1993-10-12 Nkk Corp 連続式竪型コークス炉およびコークス製造方法
CN201010626Y (zh) * 2006-07-08 2008-01-23 高耀君 生物质高能值高洁净旋流床燃烧分段气化装置
KR100978390B1 (ko) * 2008-12-18 2010-08-30 (주)피이알이엔티 열분해를 이용한 에너지 회수장치
CN105154119B (zh) * 2015-09-25 2017-11-03 神雾科技集团股份有限公司 快速热解反应装置

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Publication number Publication date
DE102017206460A1 (de) 2018-10-18
CN110520506B (zh) 2022-03-18
UA125095C2 (uk) 2022-01-05
WO2018188998A1 (fr) 2018-10-18
JP2020518683A (ja) 2020-06-25
CN110520506A (zh) 2019-11-29

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