EP3609981B1 - Ofenvorrichtung und verfahren zur herstellung von koks - Google Patents

Ofenvorrichtung und verfahren zur herstellung von koks Download PDF

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Publication number
EP3609981B1
EP3609981B1 EP18716579.0A EP18716579A EP3609981B1 EP 3609981 B1 EP3609981 B1 EP 3609981B1 EP 18716579 A EP18716579 A EP 18716579A EP 3609981 B1 EP3609981 B1 EP 3609981B1
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EP
European Patent Office
Prior art keywords
briquettes
temperature
gas
furnace chamber
heating
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.)
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Application number
EP18716579.0A
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German (de)
English (en)
French (fr)
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EP3609981A1 (de
Inventor
Ronald Kim
Uwe TSCHIRNER
Mathias SCHELLER
Matthias SPÖTTLE
Fabian GRAW
Joanna KÜHN-GAJDZIK
Hans-Werner Schröder
Volker Herdegen
Franz FEHSE
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ThyssenKrupp AG
ThyssenKrupp Industrial Solutions AG
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ThyssenKrupp AG
ThyssenKrupp Industrial Solutions AG
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Publication of EP3609981A1 publication Critical patent/EP3609981A1/de
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • 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 for using coal-containing feedstock and the use of the feedstock in this regard.
  • the invention relates to devices and methods for producing coke from feedstocks that have not been able to be used as standard or that have not yet produced a satisfactory end product.
  • the invention relates to a device and a method according to the preamble of the respective independent claim.
  • the invention relates to the use of the device specifically in connection with these alternative feedstocks.
  • coke ovens for producing coke can be designed as so-called vertical chamber ovens.
  • Vertical chamber ovens are loaded with raw material briquettes or coal briquettes from above.
  • Vertical chamber ovens can have a considerable height, for example in the range of 30 to 40m.
  • the briquettes are placed above the oven using a crane, for example, and slide, particularly due to gravity, through the coking shaft (oven chamber), particularly over a period of several hours, for example 12 or 15 hours, corresponding to the time required to convert the feedstock into coke.
  • the briquettes experience a temperature change, particularly from initial temperatures below 300°C to final temperatures between 900 and 1100°C.
  • Two to ten oven chambers are usually combined to form a so-called oven battery of a coke oven.
  • the shaft of each furnace chamber can have a height of 3.5m to 10m and a width of 150 to 600mm. This shows that the briquettes are subjected to high friction and pressure forces during coking. The strength of the briquettes should therefore be as high as possible. On the other hand, volume changes and "good" material transport within the briquette should also be possible. A certain degree of porosity is therefore also advantageous.
  • the raw material can be crushed beforehand, especially in hammer mills, especially to grain sizes of 0 to 1 mm.
  • the briquettes are then usually compacted in presses by pressing the grains, whereby in many cases a briquette geometry in the form of an elongated cuboid with optionally rounded corners or rounded edges has proven to be advantageous.
  • Briquettes in the shape of an ellipsoid are also common, especially produced using roller presses.
  • Water can be added to increase the baking capacity (the particles stick together during and after pressing) of the crushed raw material.
  • a high water content can have a detrimental effect on the strength of the briquettes as soon as they are coked, with the result that the briquettes disintegrate, particularly in the lower area of a vertical chamber furnace, where the greatest forces or loads act on the briquettes, and impair the coking process.
  • US 4115202 A , FR 841495 A , FR 533765 A and GB12923A disclose furnace devices with at least one vertical furnace chamber for producing coke with specific arrangements of heating walls and heating channels.
  • the object of the invention is to provide a device and a method with the features described at the beginning, which enables the most efficient and at the same time gentle coking of non-classic feedstocks, in particular lignite and/or low-baking hard coal and/or biomass and/or petroleum coal, in particular in vertical chamber furnaces. It is desirable to provide a high-quality end product (in particular coke briquettes) also from non-classic feedstocks.
  • the object can also be seen as preparing, providing and/or handling non-classic feedstocks in such a way that the product obtained after coking can be processed in a similar or identical manner as previously with classic feedstocks, e.g. classic hard coal briquettes.
  • the device and the method should also make the coking of as wide a spectrum of non-classic feedstocks as possible attractive.
  • a furnace device with at least one vertical furnace chamber, in particular a coke oven, for producing coke from at least one solid feedstock, in particular from the group: brown coal, low-baking hard coal, biomass, petroleum coke, petroleum coal; comprising at least one briquette dryer set up for tempering briquettes made from the feedstock and at least one furnace chamber with heating walls coupled to the briquette dryer, in particular below the briquette dryer; wherein the briquette dryer has a heating device and a briquette reservoir that can be heated thereby, and wherein the briquette dryer is set up to set a temperature in the briquette reservoir that increases continuously or stepwise in the conveying direction of the briquettes, in particular at least two or three temperature levels in the range from 60 to 200°C.
  • the furnace device further comprises an inlet system comprising at least one lock device, which inlet system is arranged between the briquette reservoir and the (respective) furnace chamber and is designed to supply briquettes from the briquette reservoir to the (respective) furnace chamber.
  • an inlet system comprising at least one lock device, which inlet system is arranged between the briquette reservoir and the (respective) furnace chamber and is designed to supply briquettes from the briquette reservoir to the (respective) furnace chamber.
  • the temperature level can increase steadily and/or predetermined temperature levels can be defined, especially at different heights 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 continuous process for coking can be set up in the respective vertical furnace chamber.
  • the briquette bed moves through at least one temperature zone with increasing temperature.
  • the desired throughput can be set and regulated in particular by means of a discharge system.
  • the conversion/refinement of, for example, coal into coke can take place continuously.
  • Temperature control can be used, and the process can be influenced in individual temperature zones and/or by-products can be evacuated.
  • the continuous process in the vertical chamber furnace also has advantages with regard to temperature stress on the material of the furnace device, especially silica.
  • the material can be largely kept at temperatures above 600°C or even 800°C and does not need to be repeatedly cooled to lower temperatures. This means that fewer stresses/cracks occur in the material.
  • the furnace device can have a feed unit for providing the briquettes to the briquette dryer.
  • the feed unit is also designed, for example, to feed the produced briquettes from a Press to the briquette dryer. At a minimum, the feed unit is set up to ensure continuous or batch-wise feeding of briquettes to the dryer.
  • a bunker Upstream of the dryer there is a bunker into which the briquettes can be fed continuously or in batches, and from which the briquettes can be conveyed out continuously or in batches, in particular by sliding the briquettes into the briquette dryer.
  • the feed system can be arranged above the (respective) furnace chamber. This enables feeding based on gravitational forces.
  • the furnace device is designed entirely as a vertical chamber furnace with vertical furnace chambers.
  • a vertical furnace chamber is understood to mean a furnace chamber through which the briquettes are conveyed in a vertical direction, in particular based on gravitational forces.
  • the above information in the table is in percent by mass, whereby the volatile components were measured under "waf” conditions, i.e. in a water- and ash-free state.
  • a furnace device with at least one vertical furnace chamber, in particular in the manner of a coke oven, for producing coke from at least one solid feedstock, in particular from the group: lignite, low-baking hard coal, biomass, petroleum coke, petroleum coal; comprising at least one briquette dryer set up for tempering briquettes made from the feedstock, and at least one furnace chamber coupled to the briquette dryer, in particular below the briquette dryer, with heating walls, and burners arranged on the furnace chamber, wherein 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 one horizontal heating channel, which is designed as a horizontal single-level heating channel, and above it, at least also in an upper half or beginning in a middle third, a heating channel extending in a meandering shape in several height levels, which heating channels are each individually fired by at least one burner, wherein the at least one horizontal single-level heating channel opens
  • the briquette dryer provides advantages in particular with regard to the preparation of the briquettes before feeding them into the furnace chamber.
  • the heating channels then act on the briquettes in the furnace chamber at a later stage of the process. Nevertheless, both measures concern the most precisely regulated temperature control or energy supply to the briquettes. The more precise the preparation upstream of the furnace chamber, the more precisely or effectively the energy supply in the furnace chamber can lead to the desired effects.
  • a plurality of horizontal heating channels are formed, which are fired by burners, in particular at least three horizontal heating channels each individually by at least one of the burners.
  • burners in particular at least three horizontal heating channels each individually by at least one of the burners.
  • on at least one side of the furnace chamber in at least one of the heating walls in a lower half, at least three horizontal heating channels and above them a meandering heating channel are formed, which heating channels are each individually fired by at least one burner.
  • 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 sealed observation point is arranged, which can be operated from the outside, in particular by means of a regulating slide.
  • at least one observation point with a regulating slide (open, closed, intermediate positions) for slide blocks and/or with measuring sensors is arranged on at least one of the heating channels, in particular at a reversal point. This enables the type and manner of tempering to be optimized in each case.
  • 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. This also simplifies adjustment.
  • the meandering heating channel has one or more vertical passages. This also opens up expanded possibilities for tempering.
  • the meander-shaped heating channel is designed to be short-circuited at one or more horizontal or vertical positions, in particular by releasing or blocking vertical passages.
  • the meander-shaped heating channel has one or more vertical passages, at each of which at least one adjusting element, in particular a slide block that can be operated from the outside, is arranged. This also enables particularly fine adjustment or locally particularly focused adjustment.
  • the briquette reservoir can be heated in a controlled manner to at least two different temperature levels, in particular at at least two different height positions of the briquette reservoir, depending on measured values that can be measured in the briquette reservoir from the group at least comprising: temperature, humidity; in order to dry the briquettes, 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 in such a way that degassing is not yet caused.
  • the upper limit of the respective temperature level can be taken from temperature values determined in advance for a respective feedstock, e.g. stored in a data storage device, or optionally specified during the process, in particular by means of at least one pressure and/or gas sensor and/or humidity sensor on/in the briquette dryer. This allows the briquettes to be dried continuously and more intensively in a gentle manner, without excessive temperature or material stress.
  • the briquette reservoir can be heated depending on the measured values for controlled drying of the briquettes to minimum moisture values of a maximum of 1 to 5 Ma%, in particular 2 to 4 Ma% at the outlet of the briquette dryer.
  • This makes it possible to gently bring the briquettes from an initial moisture content in the range of 10 to 15 Ma% to moisture values below 5 Ma%, which are advantageous for the subsequent coking.
  • Humidity and/or temperature sensors can be provided in the briquette dryer, in particular at the respective height positions. It can be sufficient to carry out the temperature control solely depending on the moisture content, sufficient accuracy of the measurement is assumed.
  • Capacitive or spectroscopic measuring methods can be used to measure the humidity, for example. However, redundant measuring devices are preferably available, in particular for pressure, volume and/or temperature measurements.
  • the control is carried out at least also via a temperature measurement, optionally exclusively via a temperature measurement.
  • drying is particularly useful for brown coal, particularly in a temperature range of 60 to 200°C, and particularly from 100 to 200°C. It has been shown that drying should preferably be carried out up to an upper temperature limit above which degassing (gas emission) begins in the respective feedstock.
  • This upper temperature limit can be predefined for a particular feedstock, and when controlling the drying process, such upper limits can be called up from a data storage device and taken into account as a target specification.
  • the drying process can also be specifically adapted to each feedstock.
  • the previously mentioned temperature and humidity ranges can be further restricted for lignite or hard coal, for example.
  • the feedstocks have different H2O contents, and material transport processes during drying are specific to each feedstock, particularly due to different material structures (micro/meso/macropores).
  • the furnace device can have a control device and a measuring device coupled thereto, set up for controlling/regulating 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 used for each of the individual Process steps must be set up or provided, each in communication with corresponding sensors of a measuring device.
  • the briquette dryer has at least one dryer unit, in particular a roof dryer unit, which has a hot gas circuit, in particular sealed off from the briquettes, for introducing heat energy into the briquettes.
  • the sealed off hot gas circuit can be used to separate the hot gas from the briquettes.
  • the hot gas can flow in lines covered by roofs or other slanted channels, along which lines the briquettes can slide past without remaining on the lines.
  • the dryer unit can be set up to continuously convey the briquettes based on gravitational forces (continuous operation), with the briquette reservoir being integrated into the dryer unit, in particular separately from the hot gas circuit. It has been shown that other types of drying, e.g. fluidized bed drying, are not feasible or at least not advisable, in particular because they would not allow the briquettes to be pre-treated in the same gentle manner.
  • the dryer unit described here enables gentle drying, with good controllability of the heat energy introduced, and also with a cost-effective and robust construction of the unit.
  • the number/density of the heating lines can increase towards the lower end in order to be able to continuously introduce more heat energy, in particular without the need for complex control.
  • the briquette dryer can also fulfil the function of a buffer.
  • a buffer Preferably, several levels of briquettes are always buffered above a highest/uppermost drying level, in particular to avoid short-circuit flows of drying gases.
  • This multi-layer buffer of briquettes to be supplied also enables drying gases to be extracted in an evenly distributed manner.
  • the geometry and arrangement, in particular the angle and the distances between individual roofs of a height level in the briquette dryer as well as the height distance of the drying levels can be designed in such a way that no solid bridges are formed and that the gravitational movement of the briquettes can take place unhindered. It has been shown that a vertical or diagonal distance of at least a factor of 6 of the briquette diameter a good compromise between temperature profile and (especially exclusively gravity-driven) conveying or freedom of movement of the briquettes.
  • the respective drying circuit can have a fan and can be additionally supplied with fresh, dry exhaust gas (from heating the briquettes in the coking chambers) and/or with externally generated, dry flue gas from a burner (in particular intended exclusively for the dryer in order to ensure redundancy).
  • the briquette dryer has a dryer unit with several drying circuits, each comprising at least two drying levels. This enables particularly specific control of the respective temperature levels.
  • the briquette dryer has a dryer unit with several drying circuits, each comprising at least two drying levels. This provides the greatest possible flexibility when setting a desired temperature profile in the briquette reservoir.
  • the dryer unit defines several drying levels, in particular at least four drying levels, in each of which hot gas lines are arranged, wherein each drying level can be regulated to an individual temperature level, wherein the drying levels are preferably arranged at least 60 cm apart.
  • the briquette dryer or the briquette reservoir has a height extension of at least 2m, preferably at least 2.5 or 5m. This enables the setting of a temperature profile that is advantageous in terms of height, in particular for individual, locally predefined drying levels. A temperature difference of at least 25 to 30°C and a maximum of 35 to 45°C is preferably set between the drying levels. It has been shown that this enables an advantageous drying process to be implemented, in particular when the briquettes are conveyed based on gravitational forces.
  • the dryer unit defines several drying levels, in particular at different height positions, in particular at least four drying levels, in each of which hot gas lines are arranged, whereby each drying level can be regulated to an individual temperature level, for example by means of slides, flaps, flow regulators.
  • each drying level can be regulated 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 moved relative to the individual drying levels, in particular continuously, drying can also take place under comparatively homogeneous, constant temperature stress.
  • the briquette dryer or the feed system is connected to at least two of the furnace chambers, in particular two to six furnace chambers. This makes it easier or more cost-effective to feed the briquettes.
  • the feed system can serve at least two furnace chambers.
  • the feed system has a distributor for this purpose.
  • the briquettes can be evenly distributed to the individual furnace chambers (in particular four to six chambers), supported by a geometry of the distributor that is preferably adapted for gravity-driven bulk material movements, e.g. by means of funnels, tubes, filling nozzles.
  • the lock device can also be used to prevent gas from escaping.
  • the distribution of the briquettes to the furnace chamber(s) can preferably be realized without mechanically moving parts (switches), in particular by means of so-called mandrels.
  • Mandrels arranged in the respective lock device or in front of or behind it can ensure an even, gravity-driven distribution of the briquettes. It is also possible to arrange the lock device in a transversely offset manner, whereby the entry system has an outlet that is wider than half the width of a furnace chamber.
  • a distribution of the briquettes as evenly as possible between the respective furnace chambers is also advantageous in that it ensures consistent process parameters.
  • the operation of a furnace chamber is a sensitive interaction of a wide variety of influencing factors. If the furnace chamber is not completely filled, for example, the type of heat transfer changes, both in connection with the extraction of raw gas and regarding the indirect supply of heat energy to the feedstock. If the furnace chamber is not completely filled, the mass-specific heat input in particular can 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 dry coke cooling. 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 sealing rings can also be used.
  • an internal volume of the lock delimited by the double flap can optionally be evacuated, for example by means of a pump that is provided for evacuation or gas flow to other components of the furnace device.
  • the respective flap or a lock slide can in particular have a square shape.
  • the furnace device can have a double lock system below at least two furnace chambers, so that the coal/coke briquettes or the lump coke from 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 designed to discharge briquettes or coal briquettes converted into coke briquettes from the furnace chamber or from a coke dry cooling system, in particular by gravity.
  • a discharge system comprising at least one lock device and is designed to discharge briquettes or coal briquettes converted into coke briquettes from the furnace chamber or from a coke dry cooling system, in particular by gravity.
  • the respective lock device of the infeed/outfeed system is preferably designed as a construction made of heat-resistant material with anti-slip properties, e.g. with a Teflon coating.
  • the lock device has, for example, sliding slopes with angles between 5 and 35° (in relation to the horizontal plane).
  • the lock device can be motor-controlled and can be operated manually (manual control, push button) or automatically (time or coke temperature controlled).
  • the corresponding motor control can interact with, for example, a hydraulic, pneumatic or electric drive.
  • the discharge system is preferably arranged below the (respective) furnace chamber or below a/the coke dry cooling system.
  • the input system and/or the discharge system can each be designed as a rocker, flap, lever, tap, slide or pendulum construction.
  • a switch or a distributor or at least one mandrel can be provided, in particular in the form of a triangular divider on the floor of the briquette dryer or downstream of the furnace chamber, whereby the briquettes can be evenly distributed into the locks by gravity.
  • the furnace device has a device for dry coke cooling downstream of the (respective) furnace chamber, which can be operated without water and which has at least one inlet and at least one outlet for cooling gas, in particular cooling inert gas.
  • the dry coke cooling enables efficient but nevertheless gentle cooling.
  • the cooling can take place in countercurrent through the bed, in particular in such a way that a continuous temperature profile is established, which can be regulated depending on the amount of purge gas used.
  • the device for dry coke cooling can be described as a solid heat exchanger with a constant temperature profile.
  • the device for dry coke 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 set up to generate steam.
  • a comparatively homogeneous temperature profile or gradient in the briquette bed can be achieved in a simple manner, while at the same time ensuring high energy efficiency.
  • High energy efficiency is of interest at the latest when it comes to the question of the economic viability of the overall process. High energy efficiency therefore also has a direct influence on the possible/realizable measures, e.g. when drying the briquettes.
  • the device for dry coke cooling can be coupled to at least one of the furnace chambers downstream of the furnace chamber, in particular by means of a/the discharge system of the furnace device.
  • the device for dry coke cooling can be coupled to one to six furnace chambers.
  • the device for dry coke cooling has or defines a cooling gas circuit, in particular comprising at least one heat exchanger. This enables efficient use of recovered energy.
  • several temperature zones with increasing temperatures are formed in the (respective) furnace chamber in the conveying direction of the briquettes, comprising at least one 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 enables controlled heating, in particular also in an evaporation area.
  • the dry cooling device can comprise a cooling gas circuit with a heat exchanger, which heat exchanger is connected to a feed water line.
  • the heat exchanger can consist of tube bundles and a steam drum, whereby the heat transfer from the cooling gas heated in the dry cooling device to the feed water can take place in countercurrent, cocurrent or crosscurrent.
  • the device for dry cooling can have several cooling gas inlets and cooling gas outlets, which are arranged in such a way that the flow profile in the briquette bed through which it flows can be adjusted by regulating the volume flows supplied or removed.
  • several horizontal heating channels are formed on at least one side of the (respective) furnace chamber in at least one of the heating walls, which are coupled to at least one vertical exhaust gas flue and which are fired by burners, in particular at least three horizontal heating channels each individually by at least one of the burners.
  • a horizontal heating channel is understood to be a channel which does not extend or does not extend significantly in the vertical direction.
  • a horizontal heating channel extends essentially in a single height position or horizontal plane.
  • heating channel routing in a wall located to the side of the chamber can be referred to as a "grid stone regenerator".
  • heating can be carried out individually at different heights and without switching. Each heating channel can be supplied with heat energy individually.
  • This older design or configuration of the heating channels has proven to be quite inflexible and can only be optimized for one type of feedstock/coal (e.g. Lusatian lignite). This design does not allow for adequate response to different types of coal/feedstock.
  • feedstock/coal e.g. Lusatian lignite
  • indirect heat transfer can take place into the respective furnace chamber.
  • Indirect heat transfer is understood to mean heat transfer through at least one partition wall, i.e. also based on heat conduction through the material of the furnace, in particular heat conduction in silica bricks.
  • the horizontal, individually fireable heating channels can define a degassing space or a degassing zone in which heavily pre-dried briquettes are subjected to a comparatively high temperature stress or a comparatively high energy supply in order to be able to carry out the degassing essentially in a lower section of the furnace chamber.
  • This can also prevent purge gas coking, particularly in an upper area of the furnace chamber, in which the briquettes are still particularly sensitive to temperature stress.
  • the horizontal heating ducts can each (particularly independently of each other) lead into a vertical exhaust duct from which the gas can be removed.
  • a/the drying circuit of the briquette dryer is coupled to at least one heating channel of the (respective) furnace chamber. This enables the waste heat of the furnace chamber to be used to temper the briquette dryer. Flue gases from the heating of the furnace chamber can be used to supply the circuits of the briquette dryer with flue gases that are as "dry” as possible. It has been shown that the temperature level of the extracted flue gases is still high enough to operate the dryer circuits. This not only simplifies the system configuration but also increases energy efficiency. It has been shown that the exhaust gases from the heating (or the flue gases) should have as low an O2 content as possible, which can be ensured in particular by stoichiometric combustion. This makes it possible to prevent the 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 connects 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 duct and from there via a connecting line to the briquette dryer.
  • raw gas can be processed and the processed gas can be further used, in particular as fuel for heating.
  • a/the drying circuit of the briquette dryer is coupled to at least one heating channel of the furnace chamber. This also allows energy advantages to be achieved.
  • At least one of the several horizontal heating channels can be heated by a burner with flame monitoring arranged externally of the furnace chamber, which burner is coupled to the respective heating channel, in particular by a natural gas-operated burner.
  • a burner with flame monitoring arranged externally of the furnace chamber, which burner is coupled to the respective heating channel, in particular by a natural gas-operated burner.
  • This allows the energy input to be controlled to a comparatively precise In particular, a temperature of at least 1000°C can be achieved at each heating channel.
  • a very hot degassing zone can be set specifically in the lower area of the furnace chamber.
  • Burners with flame monitoring offer the advantage of high flexibility and precision in terms of temperature control (heat input).
  • gas was previously generated in separate gas generators arranged in front of the furnace chambers with appropriate piping to the furnace chamber. In these gas generators, the heating gas was generated by burning coal, which was harmful to the environment.
  • horizontal heating channels arranged one above the other and adjacent to one another can be heated by burners arranged opposite one another. This allows a comparatively homogeneous heat input in relation to the total volume of the furnace chamber.
  • Horizontal heating channels that are adjacent to one another in a vertical direction preferably open into vertical exhaust ducts at opposite ends. This offset arrangement of the burners enables a particularly homogeneous heat input.
  • heating channels arranged at the same height on opposite sides can be heated by burners arranged opposite one another. This allows a comparatively homogeneous heat input in relation to the total volume of the furnace chamber.
  • burners can be arranged diagonally opposite each other. At adjacent height positions of a furnace chamber, burners can be arranged on opposite edges/corners on one of the sides of the furnace chamber. This can create a double asymmetry, i.e. 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 in a meandering manner in several height levels and is arranged above at least two or three horizontal heating channels and which can be heated by at least one burner. This makes it easy to set a temperature profile that decreases upwards in the vertical direction.
  • a meandering heating channel with a reversal is formed on at least one side of the (respective) furnace chamber, on which at least one measuring point is arranged at at least one of the reversals, in particular at least one temperature and/or pressure measuring point. In this way, in particular the temperature profile can be measured.
  • a meandering heating channel with at least one reversal is formed on at least one side of the furnace chamber, on which an observation point is arranged at at least one of the reversals, in particular a tightly sealed observation point that can be operated from the outside.
  • an observation point is arranged on at least one of the heating channels.
  • the observation point enables optical control or visual insights. This provides options for monitoring and adjusting operating parameters.
  • several horizontal heating channels are provided in the side heating walls of the furnace chamber, in particular in opposite heating walls, of which the fourth heating channel from below is designed in a meandering shape in several loops, with at least one burner being connected to the fourth horizontal heating channel in the lower area of the furnace chamber and a line arrangement running to the briquette dryer being connected in the upper area of the furnace chamber.
  • a meandering heating channel with at least one reversal is formed on at least one side of the (respective) furnace chamber, on which an observation point is arranged at at least one of the reversals, in particular a A tightly sealed observation point that can be operated from the outside.
  • This allows the temperature regime in the furnace chamber to be influenced even more precisely.
  • temperature recording and monitoring can also be carried out.
  • Several observation points can be provided at several heights, in particular to record a temperature gradient.
  • the condition of the bricks used can be inspected from the outside at the observation points.
  • the surface temperature of the bricks can also be measured, which allows conclusions to be drawn about the radiant heat emitted, for example.
  • At least one observation point is arranged on at least one of the heating channels.
  • a control slide for slide stones can be operated there and/or it can be checked whether the material of the furnace chamber walls is still intact.
  • One or more sensors can also be installed there.
  • the respective observation point is accessible from the outside via a scaffold, for example.
  • several horizontal heating channels are provided in the side heating walls of the furnace chamber, in particular in opposite heating walls, of which the fourth heating channel from below is designed in a meandering shape in several loops, with at least one burner being connected to the fourth horizontal heating channel in the lower area of the furnace chamber and a line arrangement running to the briquette dryer in the upper area of the furnace chamber.
  • This configuration of the heating channels allows the temperature profile in the furnace chamber to be set relatively precisely. In the lower area of the furnace chamber, extremely high temperatures can be achieved in a flexible manner, particularly in order to reduce the volatile components in the briquette to the desired levels of less than 1% by mass and to complete the coking process.
  • the number of three individually heated horizontal channels has proven to be advantageous on the one hand in terms of the high degree of individual heating, and on the other hand in terms of the high heat energy that can be introduced (e.g. approx. 1050°C desired final briquette temperature).
  • this type of heat input can be achieved over a relatively short distance (in the vertical direction of the briquettes) by achieving furnace chamber temperatures of well over 1000°C. It has been shown that this heat input can be ensured in a particularly useful way by means of several burners and several individual heating channels in the lower area (on the floor) of each furnace chamber. This configuration also allows for flexible response to the final temperatures required for each feedstock/type of coal. Our own investigations have shown that a combination of three horizontal heating channels and one meandering heating channel offers particularly many advantages in terms of the most homogeneous temperature profile possible and the design effort.
  • a meandering heating channel is a channel that extends over several height levels, with the height levels being connected to one another by a loop-shaped or meandering course of the channel.
  • the channel can increase continuously in height.
  • the angle at the turning points of the channel is a maximum of 90°.
  • a type of coil heat exchanger can be provided using the meandering heating channel.
  • a meandering heating channel is formed, which heating channels can each be individually heated by at least one burner, wherein the meandering heating channel preferably has turning points with observation points with sensors arranged thereon or measuring there.
  • Vertical passages are preferably formed on the meandering heating channel.
  • heating channels equipped with adjusting elements such as slide block elements offer various advantages.
  • the adjusting elements can be adjusted/positioned through observation points using suitable auxiliary structures such as metal hooks, particularly from the outside, so that the volume flows flowing in the heating channels can be adjusted depending on the process requirements (e.g. lowering the flow so that combustion takes place in a meander channel at a defined height level). This allows a desired temperature gradation to be set precisely in the vertical direction.
  • heating channels can also contain further openings, particularly vertical passages, by means of which partial volume flows can flow from below into the horizontal channel above, in the form of a short circuit or bypass, and by means of these bypass flows, both the total pressure loss of the system and any temperature maxima that may occur can be minimized, particularly at the respective reversal point.
  • At least one gas outlet for a gas extraction line is arranged on the (respective) furnace chamber at at least three different height positions, the height positions in particular comprising a height position arranged at least approximately in the middle at half the height of the furnace chamber.
  • the (respective) furnace chamber can have at least three gas outlets arranged in at least three different height positions of the furnace chamber, by means of which Gas outlets can provide at least three gases/gas types (a first gas and at least one further gas) that can be evacuated from the furnace chamber.
  • the (respective) furnace chamber has several gas outlets that can be arranged at several locations, in particular all around, in at least one of the height positions. This allows the gas to be removed in such a way that there is very little transport of material in the vertical or horizontal (or radial) direction. The coking process can thus be set even more cleanly and selectively.
  • 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. This allows the gas to be extracted in such a way that there is very little transport of material in the vertical direction. This also makes it possible to evacuate a wide range of different gases.
  • a first of the height positions is arranged in a lower third of the furnace chamber, and a second of the height positions is arranged in a middle third of the furnace chamber, and a third of the height positions is arranged in an upper third of the furnace chamber.
  • a first of the height positions viewed from a floor of a/the furnace chamber, is arranged at a distance of 1 to 3 m, in particular 1.5 to 2.5 m, from a second of the height positions. This enables selective evacuation in a main degassing zone, in particular in the area of 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, from 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, from the third height position. In many cases, this respective distance is well suited to avoid purge gas coking or unwanted temperature deviations. The distance can also be smaller, especially with more than three height positions, but it has been shown that this distance provides a good compromise between plant/process engineering effort and simple construction of the system.
  • the first height position is arranged at a distance of 0 to 2 m, in particular 1 m from the ground and/or the second height position is arranged at a distance of 0 to 0.5 m in relation to the center and/or the third height position is arranged at a distance of 0 to 2 m, in particular 1 m 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 a high level of process reliability, particularly in an upper region of the furnace chamber, with comparatively fine adjustment with regard to evacuatable gases or desired temperature profiles.
  • the height positions are each arranged at a distance from one another 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 head gas emitted in the upper area of the furnace chamber can be evacuated from the furnace chamber via the corresponding gas outlet.
  • the highest height position does not have to correspond to the top end of the furnace chamber, but can also be arranged somewhat lower, for example, depending on the feedstock and process control.
  • the furnace device is designed as a vertical chamber furnace, in which the briquette dryer is arranged above the (respective) furnace chamber.
  • the entire material flow can be regulated by means of a discharge system.
  • the temperature profile in the briquette dryer can be coordinated with the temperature profile in the furnace chamber in such a way that when the desired material flow in the furnace chamber (briquette quantity/h) is set, the desired temperature profile in the briquette dryer is also set.
  • the briquette dryer has or can define at least four drying levels or temperature levels. This makes it possible to react particularly sensitively to changes in the material flow.
  • a/the device for dry coke cooling is arranged below the (respective) furnace chamber. This allows the conveying concept based on gravitational forces to be continued. The entire arrangement becomes compact and the material flow can be easily regulated.
  • the furnace device comprises a measuring device and a control device coupled thereto, designed to control/regulate drying of the briquettes in a temperature range of 60 to 200°C and/or in a moisture range of 1 to 5% by mass; and/or wherein the furnace device comprises a measuring device and a control device coupled thereto, designed to specify a throughput or briquette material flow, in particular by means of a discharge system coupled to the control device.
  • both the temperature regime during drying and coking and the material flow can be regulated, in particular depending on one another.
  • the (respective) furnace chamber or heating walls of the furnace chamber can be made of refractory silica material.
  • the bulk density of the briquettes in the furnace chamber can 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.
  • At least one of the objects described above is also achieved according to the invention by a previously described furnace device in which the individual heating channels are arranged in relation to at least two different temperature ramps/zones, wherein the upper temperature zone with a more moderate temperature ramp is realized by means of at least one meandering heating channel, and/or wherein a lower temperature zone with a steeper temperature ramp is realized by means of several, in particular at least three individually fired horizontal heating channels.
  • the previously described object can preferably also be achieved by a method according to claim 11, described in more detail below, for producing coke from at least one solid feedstock, in particular from the group: brown coal, low-baking hard coal, biomass, petroleum coke, petroleum coal; which feedstock is provided in the form of briquettes and is fed to a vertical furnace chamber, in particular a coke oven, in particular fed to a previously described furnace device; wherein the briquettes are first fed to a briquette dryer, dried therein according to a predefined temperature curve continuously in accordance with the advance of the briquettes, in particular to at least two or three temperature levels in the range from 60 to 200°C, and then fed to the furnace chamber.
  • a method according to claim 11, described in more detail below for producing coke from at least one solid feedstock, in particular from the group: brown coal, low-baking hard coal, biomass, petroleum coke, petroleum coal; which feedstock is provided in the form of briquettes and is fed to a vertical furnace chamber, in particular a coke
  • the briquettes in the furnace chamber can be continuously tempered to a higher temperature according to the advance of the briquettes.
  • An energy supply that gradually increases with the path enables 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.
  • the coking of lignite, low-baking hard coal or biomass is a process that should be controlled very precisely, 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 lignite types, in particular around 350 to 410°C), at which the feedstock softens, should be avoided. This can be achieved by adjusting the temperature control or heating curve.
  • 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. This allows the process to be monitored and controlled particularly well, and the feedstock to be coked particularly gently.
  • the temperature profile can therefore be adjusted both by extracting emission gases at different heights and by controlling/regulating the energy supplied by external burners.
  • measures such as opening or blocking vertical passages can also be taken in the meandering heating channel in order to be able to adjust the energy input, for example in the "plastic zone".
  • a solid feedstock in particular from the group: Lignite, low-baking hard coal, biomass, petroleum coke,
  • a desired temperature profile in the furnace chamber can be set in a comparatively precise, homogeneous manner even with indirect tempering from the outside.
  • the series connection of the individual horizontal sections to form a meandering heating channel enables controlled cooling of the flue gases with continuous heat transfer, with a heat flow density that decreases in a controlled manner over the height of the heating wall.
  • the heat indirectly transferred via the heating channels can be supplied to the load (the charge) in an individually adapted manner.
  • 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 (as a function of the height position) can be increased more strongly, in particular in order 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 at least one first phase previously completed.
  • the determination of how high the increase rates 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 should preferably be set, can be flexibly adjusted as a function of the selected feedstock or temperature range, in particular by means of the device according to the invention.
  • temperature ramps of different steepness are set in the furnace chamber, in particular a first temperature ramp with a gradient in the range of 0.7 to 1K/min and a second temperature ramp with a gradient 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 duration of 5 to 7h, in particular exclusively by indirect tempering on the one hand by means of the meander-shaped 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 discontinuous. It has been shown that a continuous transition can be achieved, simply because of the continuous advance of the briquettes (sliding downwards).
  • the briquettes are heated in the briquette dryer at temperature curves of 0.4 to 2 K/min, in particular at 0.8 K/min. This allows drying to be carried out in a very gentle manner.
  • the heat energy is preferably introduced into the heating lines of the briquette dryer in several stages (hot at the bottom, less hot at the top). Emissions gas from the furnace chamber and/or exhaust gas generated externally by burners can be used for this purpose.
  • a temperature increase of 0.8 K/min is particularly advantageous for brown coal briquettes.
  • advantages arise when working in a temperature range of 60 to 200°C, especially 100 to 200°C.
  • this temperature ramp is also set in the furnace chamber, especially in an upper half or even in the two upper thirds. It has been shown that this can be achieved using a meandering heating channel, especially in a particularly effective way in conjunction with an evacuation of gases at several height positions.
  • a measurement in particular a temperature measurement, is carried out in the meandering heating channel at reversal points with observation points.
  • a regulation is carried out in the meandering heating channel at at least one reversal point, in particular by means of a regulating slide from the outside.
  • at least one measurement and/or at least one regulation is carried out by means of slide blocks at at least one of the heating channels, in particular at a reversal point.
  • a short circuit or bypass is carried out at one or more vertical passages of the meandering heating channel, in particular by opening or blocking the vertical passages.
  • At least one adjusting element is arranged for regulation, in particular a slide stone that can be operated from the outside.
  • the briquettes are first fed to a briquette dryer and dried therein according to a predefined temperature curve continuously in accordance with the advance of the briquettes, in particular at at least two or three temperature levels in the range from 60 to 200°C, and are then fed to the furnace chamber and dried in the briquette dryer to a water content of less than 5% by mass before the briquettes are fed to the furnace chamber. This allows the briquettes to be treated particularly gently.
  • the briquettes are dried in the briquette dryer to water contents of 1 to 5% by mass, in particular 5% by mass, and thereby brought to a temperature of 120 to 180°C, in particular 150°C. This can ensure particularly gentle treatment of the briquettes.
  • the briquettes are heated in the furnace chamber, 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 a maximum of 2 to 3 K/min; and/or wherein the briquettes are heated in the furnace chamber over 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, are heated from initial 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 between 900 and 1100°C in the furnace chamber.
  • These temperature relationships provide an efficient process with gentle treatment of the briquettes.
  • the continuous process in the vertical chamber furnace (continuous process) enables a temperature gradient of e.g. 100 to 150°C per meter of altitude.
  • a temperature ramp of e.g. 2 to 3°C can be achieved.
  • the coking process can also be used to further increase the (coke) compressive strength.
  • the compressive strength can be increased from 20 or 25MPa by 30 to 50% to at least 35MPa to 45MPa.
  • the briquettes are heated in the briquette dryer in several stages depending on the water content, in particular in two stages with the first stage up to 15 to 10 ma%, in particular 11 ma% water and the second stage up to 1 to 5 ma% or up to 2 to 4 ma%, in particular 5 ma% water. This enables drying in a particularly gentle manner.
  • the briquettes are heated in the briquette dryer on several drying levels at different heights, each at a predefined, individually controlled temperature level, in particular by means of one or more individually controllable drying gas circuits.
  • the control can be carried out in particular via the volume flow, e.g. by means of slides or flow regulators.
  • pre-drying can also take place, in particular from 20% by mass to 11% by mass water.
  • the feedstock can be heated in several stages depending on the water content, in particular in two stages with the first stage up to 20% by mass water and the second stage up to 11% by mass water.
  • the pressed parts are heated during the coking process to a maximum of 950 to 1100°C, in particular 1000 to 1050°C, preferably a maximum of 1050°C. It has been shown that both the strength and the grain size of the coke, depending on the feedstock, would be undesirably reduced at final temperatures above 1100°C or even above 1050°C, and the use of the coke in the blast furnace would be jeopardized. According to the present process, high-strength briquettes can be made from feedstocks if these temperature ranges are maintained, which can be considered as substitutes for previous blast furnace coke.
  • the heating of the pellets during the coking process takes place in such a way that the pellets shrink by 40 to 60%, in particular 50%, in terms of volume during the coking process, and/or in such a way that the pellets decrease in weight by 40 to 60%, in particular 50%, in terms of mass during the coking process. It has been shown 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 pressed pieces are dried in the briquette dryer to water contents of 1 to 5% by mass, in particular 5% by mass, and thereby brought to a temperature of 120 to 180°C, in particular 150°C. This provides a good compromise between gentle and efficient/effective drying.
  • the briquettes from at least two adjacent coking chambers are transferred to a dry cooling device via a discharge system or a component thereof, in particular with a double lock, and cooled there to temperatures below 200°C using cooling gas, in particular nitrogen.
  • a discharge system or a component thereof in particular with a double lock
  • cooling gas in particular nitrogen.
  • This provides an efficient process on the one hand, and energy can also be recovered immediately after coking, either for previous process steps or for other systems or processes. Condensation can be avoided in particular by cooling below 200°C, but keeping the entire device at a temperature above the dew point.
  • One or more dew point sensors can be provided for this purpose.
  • the discharge system can also carry out the removal from the dry cooling device.
  • heat energy is extracted from the cooling gas (in particular nitrogen) heated due to dry cooling in the briquette bed, in particular in a heat exchanger.
  • the cooling gas can then be used in particular to generate steam.
  • the steam can be used to generate electrical current (relaxation in a steam turbine).
  • the electrical current can in turn be used to operate electrical consumers such as pumps, compressors, fans, locks, valves. Any surplus electricity can be fed into the local supply network.
  • the steam can also be used as auxiliary heating, e.g. for the raw gas processing of the white side of the furnace device.
  • the steam can also be used as a reactant in a chemical process, e.g. methanol synthesis (keywords: steam reforming, synthesis gas, H20 to increase the hydrogen yield (shift reaction), primary reformer).
  • coke in particular lignite coke with a fixed carbon content Cfix of greater than 55 Ma% is produced.
  • Cfix of greater than 55 Ma%
  • the briquettes produced can be used in the DRI (direct reduced iron) process.
  • coke in particular brown coal coke
  • CRI coke reactivity index
  • CSR strength after reaction
  • the CRI value is determined by heating the feedstock under predefined conditions to 1100°C in particular and determining the mass loss due to outgassing.
  • the CSR value can be determined in particular by spinning the outgassed material sample in a drum under predefined conditions and is also quantified as a mass loss value.
  • the coke is cooled downstream of the furnace chamber to temperatures below 200°C by passing reaction-inert cooling gas, in particular nitrogen, in countercurrent through a briquette bed formed in a dry cooling device, and is evacuated from the dry cooling device downstream of a discharge system of the furnace device.
  • reaction-inert cooling gas in particular nitrogen
  • the dry cooling system can be operated in a circuit, whereby the cooling gas is enriched with flammable components such as H2 and CO due to post-degassing processes in the coke bed.
  • the cooling gas can be evacuated from the bed and cleaned.
  • air oxygen is added to the enriched cooling gas in order to burn the flammable components before the thermal energy stored in the cooling gas can be transferred to feed water 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 conveyor path from the briquette dryer to the (respective) furnace chamber.
  • the (respective) furnace chamber is operated continuously in that the briquettes are continuously conveyed in the furnace chamber (in particular downwards) and are fed and discharged in batches, in particular via a lock device for at least two furnace chambers (double lock).
  • the fill can move continuously in the furnace chamber, and the feed and discharge can take place in batches, in particular 2 to 4 times per hour.
  • the residence time of the fill in the furnace chamber can be regulated via the speed of the discharge. It can also be taken into account that the mass and volume flow of the briquettes change during the coking process, in particular due to degassing and shrinkage.
  • the feed and discharge can therefore be set at a larger mass flow than the discharge.
  • the briquettes are fed into the furnace chamber and/or removed from the furnace chamber in a vertical direction by gravitational forces. This provides various advantages, in particular with regard to self-regulating conveyance and positioning of the briquettes within the device.
  • the feedstock or the briquettes comprise or consist of low-caking hard coal with volatile components in the range of 28 to 45 Ma% (waf) or 12 to 22 Ma% (waf). The advantages described above can also be achieved with this respective composition.
  • the material flow of the feedstock through the (respective) furnace chamber is controlled or regulated by means of a discharge system arranged below the (respective) furnace chamber, in particular exclusively gravity-driven based on gravitational forces.
  • a discharge system arranged below the (respective) furnace 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. This allows a desired temperature profile to be set or controlled even more effectively.
  • the raw gas mixture generated in the bed in furnace chambers and flowing upwards from escaping gas components leads to undesirable secondary coking (purge gas or raw gas coking) of the upstream briquettes (undesirable accelerated, convective heat transfer to the upper briquettes) due to the high energy content (high temperatures).
  • Such secondary coking is particularly disadvantageous in high, voluminous vertical chamber furnaces. There is a risk that this effect overlays or distorts the temperature profile generated over the side walls by targeted burner control. It has been shown that this effect can be reduced or completely prevented by evacuating raw gas at different vertical height positions, in particular at at least three height positions including a height position at the head of the furnace chamber.
  • At least one of the previously described objects is also achieved according to the invention by use according to claim 20, wherein a feedstock from the group: brown coal, low-caking hard coal, biomass, petroleum coke, petroleum coal; in a vertical chamber furnace with at least one vertical furnace chamber, for coking the feedstock to coke with the following properties: solid carbon content Cfix of greater than 55 Ma%, and/or CRI ⁇ 24 Ma% and CSR >65 Ma%; in a furnace device according to the invention, wherein the feedstock is tempered in a controlled manner along at least two temperature ramps comprising at least one temperature ramp in a briquette dryer arranged upstream of the furnace chamber and at least one temperature ramp in the furnace chamber, wherein the second temperature ramp is set by a meandering heating channel and optionally also by horizontal heating channels, preferably along at least three temperature ramps comprising at least two temperature ramps with a gradient increasing in the feed direction in the furnace chamber. It has been shown that thanks to the specific tempering described here, these values can be achieved, especially for all hard coal cokes
  • a gas evacuation arrangement is also provided for the extraction of usable gases during the coking of at least one solid feedstock from the group: brown coal, low-baking hard coal, biomass, petroleum coke, petroleum coal; to coke, wherein the gas evacuation arrangement is designed to be coupled to at least one vertical furnace chamber of a furnace device; wherein the gas evacuation arrangement has at least three gas discharge lines that can be arranged in at least three different height positions of the furnace chamber, which are designed to be coupled to the (respective) furnace chamber in the at least three height positions, wherein the gas evacuation arrangement is designed to selectively handle at least three types of gas (a first gas and at least one further gas) that are selectively evacuated by means of the respective gas discharge line.
  • the gas evacuation arrangement is designed to be coupled to at least one vertical furnace chamber of a furnace device; wherein the gas evacuation arrangement has at least three gas discharge lines that can be arranged in at least three different height positions of the furnace chamber, which are designed to be coupled to the (respective) furnace chamber in the at least three height positions, wherein the
  • the gaseous products can be removed depending on the temperature in order to ensure that liquid and gaseous products are of high quality and to be able to use them in particular from an economic and/or ecological point of view. It has been shown that the release of gaseous emissions from coal occurs in a very specific way at different temperature levels depending on the degree of coalification of the coal, and that this effect can be exploited if the furnace chamber can be tempered/maintained at the respective temperature level as precisely and homogeneously as possible. Both the arrangement of the heating channels and the arrangement of gas extractors/gas outlets have an effect on the setting options.
  • the gas evacuation arrangement therefore contributes to comprehensive, sustainable use of the feedstock and to a very efficient overall process, particularly including coking. This also protects the briquettes in the upper area of the furnace chamber from hot gases from the lower area. The briquettes can be guided more precisely along the desired temperature curves. Thermal stress is reduced. Purge gas coking can be avoided. Furthermore, it can also prevent emitted tar vapors from condensing on briquettes at a different altitude, for example.
  • the gas evacuation arrangement can be set up for the selective forwarding or further processing of 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 gas evacuation arrangement can also be set up for selectively setting process parameters individually at a respective height position, in particular a specific negative pressure. This allows the evacuation of by-products or the flow path of emitted gases in the furnace chamber to be set even more precisely, even with comparatively few (e.g. only three) height positions.
  • the selective handling can also include the use of the evacuated gases in connection with a method for operating the furnace device described here, for example as fuel/combustion gas for burners of the furnace device.
  • the raw gases can be used, for example, as fuel for burners on the dryer. From an energy point of view, it is advantageous to provide a circuit for this purpose.
  • the gas evacuation arrangement has several gas extraction lines that can be arranged at several locations, in particular all around, in at least one of the height positions. This also makes it possible to adjust or control the flow path of emitted gases in the radial direction.
  • connections for gas extraction lines can be provided distributed around the circumference between two and, for example, six or eight circumferential positions/locations.
  • 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. This makes it possible to avoid emitted gases causing side reactions or distorted temperature profiles over a large height range.
  • the gas evacuation arrangement extends over a height of at least 2m to 3m for furnace chambers with a height of 4m, or over at least 5m to 8m for furnace chambers with a height of 10m.
  • a first of the height positions viewed from a floor of a/the furnace chamber, is arranged at a distance of 1 to 3 m, in particular 1.5 to 2.5 m, from a second of the height positions. This enables selective evacuation in a main degassing zone, in particular in the area of 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, from a third of the height positions. This provides a large range of influence with only a comparatively small number of height positions.
  • the second height position is arranged at a distance of 1 to 3 m, in particular 1.5 to 2.5 m, from the third height position. This improves the accuracy and selectivity of the evacuation with respect to a particular type of gas.
  • the first height position is arranged at a distance of 0 to 2 m, in particular 1 m from the floor and/or the second height position is arranged at a distance of 0 to 0.5 m in relation to the center and/or the third height position is arranged at a distance of 0 to 2 m, in particular 1 m from the head of the furnace chamber.
  • This distribution provides a good compromise between plant engineering effort and selectivity or effectiveness with regard to avoiding vertical gas flows.
  • a selective evacuation of gases in a main degassing zone is made possible.
  • the gas evacuation arrangement defines at least three height positions for the gas exhaust lines, at least two of which are located in an upper half of the furnace chamber. This also provides an arrangement effective in preventing purge gas coking.
  • the height positions are each arranged at a distance from one another of at least 20 to 45% of the total height of the furnace chamber. This allows a wide height section of the respective furnace chamber to be covered, in particular in conjunction with a pressure and/or volume flow-dependent control of the evacuation.
  • one of the height positions is provided at the top of the furnace chamber, wherein the gas evacuation arrangement comprises at least one connection or at least one gas discharge line arranged and set up for coupling to a corresponding gas outlet at the top of the furnace chamber.
  • the gas evacuation arrangement comprises at least one of the following components for handling the evacuated gases from the (respective) furnace chamber: separate raw gas cooling, tar collection/separation container, discharge device for Tar, electrostatic precipitator set up to reduce dust, desulfurization unit.
  • the discharge device can be used to prevent tar from condensing in the pipes placed in the ambient atmosphere and causing blockages, especially in the case of gases evacuated from certain heights.
  • the gas evacuation arrangement has a plurality of gas extraction lines with the same function arranged in parallel, which can be coupled to different furnace chambers at the same height position, wherein the gas evacuation arrangement has a mixer to which the gas extraction lines with the same function can be coupled/are coupled.
  • This arrangement enables the further handling of the same types of gas from several furnace chambers. This makes the arrangement more compact and handling easier.
  • a furnace device with at least one vertical furnace chamber is also provided, in particular by a previously described vertical chamber furnace device, with a previously described gas evacuation arrangement.
  • a method for the extraction of gases during the coking of solid feedstock, in particular feedstock from the group: brown coal, low-baking hard coal, biomass, petroleum coke, petroleum coal; to coke from at least one vertical furnace chamber of a furnace device and for further handling of 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 gas evacuation arrangement.
  • 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 gas evacuation arrangement.
  • the different gases can optionally be handled separately.
  • one (single) recyclable material can be recycled from two gases/gas types extracted at different heights.
  • the gases are in particular raw gases that are created under the influence of temperature in the furnace chamber during the coking process and rise upwards through the bed.
  • the evacuated and handled gases/gas types can in particular be made up of one or more gases from the following group of gases: C2H6, N2, NH3, CO, CH4, H2, H2S, CO2, SO2, C2H2, C2H4, C3H6, C3H8, in particular BTX (benzene, toluene, xylene) and other high hydrocarbons.
  • H2 has a thermal conductivity that is approximately 6 to 7 times higher than N2.
  • a first gas is selectively extracted in a temperature range of 150 to 300°C, and a further gas is selectively extracted in a temperature range of 300 to 600°C, and a further gas is selectively extracted in a temperature range of 600 to 950°C or 700 to 900°C.
  • At least three different types of gases are extracted from at least three different height positions, each from a height section above 20 to 50% of the height of the furnace chamber or from a lower, middle and upper third of the furnace chamber. This ensures that a large height section can be influenced, with comparatively little technical outlay on the system.
  • a temperature range that experience has shown to be rather critical in particular the range of 350 to 470°C, can be bridged or passed through in the most gentle way possible, e.g. in a time-optimized manner.
  • the feedstock can be conveyed through this temperature zone/temperature range in such a way that the disadvantageous processes that experience has shown to occur with some feedstocks, such as "expansion” or “contraction/resolidification”, can therefore be deliberately avoided or passed through.
  • a type of gas that proves to be particularly valuable can be extracted/evacuated, for example at 450°C, whereby the targeted height-level-related evacuation can enable this temperature range to develop in only a small (height) zone in the respective furnace chamber.
  • a first gas is selectively extracted at a first height position in a range of up to 2 m below the top of the furnace chamber, and a further gas is selectively extracted at a further height position in a range of 35 to 65%, in particular 45 to 55% of the height of the furnace chamber, and a further gas is selectively extracted at a further height position in a range of up to 2 m above the bottom of the furnace chamber, in each case in a furnace chamber with a height of at least 4 to 6 m.
  • the handling of the at least three types of gas includes individual regulation of evacuated volume flows for each type of gas, in particular with regard to evacuated volumes. This makes it possible to influence both the composition of evacuated gases and the temperature profile within the briquette bed.
  • at least one flow sensor can be provided on each gas discharge line.
  • the control also enables targeted influence on vertical gas flows that may not be completely preventable. For example, a greater negative pressure can be built up in a gas extraction line located further down than in a gas extraction line at a higher altitude. Effect: A gas flow vertically upwards 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 is useful to measure the gas composition individually on each gas extraction line, in particular using at least one gas sensor or at least one gas analysis method (e.g. spectroscopic, chromatographic).
  • valuable chemical substances such as methanol, dimethyl ether or synthetic natural gas are produced from the at least three different gases/gas types extracted from the (respective) furnace chamber during further handling. This enables a sustainable, economical overall process.
  • At least one of the at least three different gases/gas types extracted from the (respective) furnace chamber is fed as fuel to a burner that indirectly heats the furnace chamber.
  • the gas extracted for the burners can consist of the following components, in particular at least 97%: C2H6, N2, CO, CH4, H2, CO2.
  • the gas intended for the burners can be extracted at different heights, in particular at three of the heights.
  • the gas can be cleaned, in particular with regard to BTX and high hydrocarbons. This improves the functioning of the burners.
  • lignite coke with a fixed carbon content (Cfix) of more than 55 mass% is produced.
  • the process makes it possible to provide high-quality coke for widespread use.
  • the reference value Cfix can also be defined as the coke yield minus the ash content.
  • a gas evacuation arrangement on at least one vertical furnace chamber for evacuating at least three types of gas from the furnace chamber in order to set a vertical temperature profile within a briquette bed in the furnace chamber.
  • At least one type of gas from at least three types of gas evacuated from a vertical furnace chamber to provide fuel gas to at least one burner indirectly heating the furnace chamber.
  • a furnace arrangement for producing coke briquettes comprising a previously described gas evacuation arrangement and a furnace device, which furnace device has 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 it, in particular at least also in an upper half or beginning in a middle third, a heating channel extending in a meandering shape in several height levels, which heating channels can each be individually heated by at least one burner, in particular by means of gas evacuated from the furnace chamber.
  • a method for producing briquettes from carbon-containing solid feedstock comprising both drying briquettes made from feedstock in a briquette dryer and coking the briquettes to form coke briquettes in a furnace chamber, wherein gas is evacuated at at least three height positions of the furnace chamber distributed over at least half the height of the furnace chamber, which gas is at least partially fed to burners arranged on the furnace chamber for heating the furnace chamber.
  • This method can be carried out using a furnace arrangement as described above.
  • the raw material briquettes are passed through the respective furnace chamber over a period of 4 to 15 hours, in particular 6 to 9 hours.
  • the raw material briquettes are heated from initial temperatures between 100 and 200°C, in particular 150°C, to final temperatures between 900 and 1100°C, in particular in several stages.
  • the required heat can be generated in two channels arranged to the side of the respective chamber, which can be heated by several external burners, and transferred indirectly through a stone partition wall into the respective furnace chamber.
  • Each shaft has a height of 3.5 to 10m, in particular a height of 5 to 8m.
  • Each shaft has a width of 150 to 600mm, in particular a width of 200 to 400mm.
  • the low-baking hard coals themselves have only low baking properties. Binders can be added to the low-baking hard coals in a preceding mixing process, which increases the adhesive effect or baking properties of the coal particles during the briquetting process.
  • fat coal in particular is a good-baking coal (classic "coking coal”).
  • edible coal and gas coal are also good-baking coals. All other types of coal are referred to in this description as weak-baking coals.
  • the briquettes can also consist of hard coal types such as anthracite (fB ⁇ 12%), lean coals (12% ⁇ fB ⁇ 19%), gas coals (28% ⁇ fB ⁇ 35%), gas flame coals (35% ⁇ fB ⁇ 45%) or alternatively of a mixture of these coal types, optionally also using high-quality fat (coke) coals (19% ⁇ fB ⁇ 28%).
  • hard coal types such as anthracite (fB ⁇ 12%), lean coals (12% ⁇ fB ⁇ 19%), gas coals (28% ⁇ fB ⁇ 35%), gas flame coals (35% ⁇ fB ⁇ 45%) or alternatively of a mixture of these coal types, optionally also using high-quality fat (coke) coals (19% ⁇ fB ⁇ 28%).
  • the raw material can be crushed into pellets in a perforated disc roller mill, especially with a grain size of 0 to 2 mm. It has been shown that pellets/grains produced using a perforated disc roller mill are particularly easy to bind (they cake easily) and therefore simplify the subsequent briquetting process (pressing).
  • This compaction process is preferably carried out in a mold channel stamping press. It has been shown that particularly pressure-resistant briquettes can be produced using a channel matrix geometry in the form of a Venturi tube with a narrowing of the cross-section and a tapering cross-section expansion. Other types of presses were unable to deliver comparably good results.
  • briquettes in a flat cylindrical shape provide particularly good strength values, whether before or after carbonization.
  • a ratio of briquette diameter to briquette height of 1 to 5, especially 2 to 3, also delivers good results in terms of the heating and coking process.
  • the briquette preferably has a diameter of 20 to 100 mm.
  • the briquette is made in particular from coal grain sizes between 0 and 2 mm.
  • the briquettes can optionally have a different geometry, such as cube, cuboid, plate, shell, pillow, sphere or egg-shaped geometries. In experiments to date, however, the best results have been achieved with the puck shape.
  • Process parameters include: pressing pressure, duration and temperature. Pressing is carried out at pressures of 120 to 150MPa, particularly at 140MPa. Pressing is carried out at temperatures between 60 and 100°C. Pressing is carried out for a duration of up to 15 seconds.
  • coal types described here can be mixed with coking aids in upstream process steps, making coking more efficient and giving the coke product higher quality, e.g. higher strength or higher reactivity.
  • At least one coking aid is added to the briquetting process (during pressing), in particular to improve the efficiency of the downstream coking process.
  • Coking aids can be selected individually or in combination, in particular from a group of coking aids that have previously been considered useful in connection with classic feedstocks.
  • baking (gluing) and coking aids are added to the raw material before the pressing and coking process in one or multi-stage mixing processes, in particular to improve the quality of the coke produced or to facilitate the briquette pressing process from low-baking coal types.
  • such aids are mixed in before briquetting at temperatures in the range of 30 to 120°C.
  • the auxiliary materials can be selected in particular from the following group, optionally in combination: molasses, sulphite waste liquor, sulphate waste liquor, propane bitumen, cellulose fibres, HSC (high-conversion soaker cracking) residue, HSC/ROSE (residue oil supercritical extraction) mixed residues from the petroleum industry.
  • the subsequent briquetting process takes place in the temperature range between 40 and 90°C, especially between 55 and 65°C.
  • the briquettes can be placed above a main dryer by a crane and can slide through the main dryer, through the coking shaft and further into a coke dry cooling device.
  • the main drying process of the briquettes is carried out in particular by roof drying units and serves to further reduce the water content of the briquettes from approx. 20% by mass to around 3% by mass. This ensures that the heat transferred into the chamber is not dissipated to a large extent for water evaporation, which experience has shown can also lead to the briquettes breaking open.
  • the main drying process is usually carried out in two stages, but can also be carried out in one or more stages.
  • the drying medium used is preferably hot exhaust gas/raw gas, which results from combustion processes in heating channels in the furnace chamber located under the dryer and can be directed upwards into the roof-shaped channels.
  • channels are arranged in a cross-shaped manner, for a cross-flow arrangement.
  • a counter-current or co-current arrangement can also be provided, at least in sections.
  • a main drying unit set up for the main drying can be coupled to an external burner with flame monitoring, through which additional exhaust gas can be provided for all or several or even just one drying stage.
  • 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 to at least two furnace chambers, in particular in the form of a double flap.
  • the raw material/feedstock (or briquettes) is heated in the coking shaft (or furnace chamber) located below the main dryer by applying 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 hours, 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. In at least In a further step, in which the briquettes are brought into the temperature range of 300 to 1100°C, they are heated at a heating rate of 2.6 to 3 K/min.
  • the method according to the invention in particular in combination with a specific agglomeration technique for preparing the briquettes, it is possible to provide coal or coke of comparatively high quality in relation to the input materials.
  • the maintenance of the desired briquette shape, in particular a cylindrical puck shape, even during coking can be ensured.
  • the coal shrinks by 40 to 60%, in particular 50%, both in terms of mass and volume, and thereby also achieves the desired high compressive and abrasion strengths of >30MPa (in particular coke strength after reaction (CSR)) as well as low reactivities with CRI (Coke Reactivity Index) values ⁇ 55%.
  • CSR coke strength after reaction
  • the briquette shape (puck shape) can be maintained, with the result that pressure loss, heat transport, flow profile and other process parameters remain predefinable.
  • the respective furnace chamber consists primarily of refractory silica material.
  • Heating channels can be 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 coupled in particular one above the other to horizontal heating channels.
  • the exhaust gases or flue gases from the heating walls can also be used for energy purposes, for which purpose an exhaust duct can optionally be supported by a flue gas blower.
  • three burners are provided/coupled to three lower or lowest horizontal channels.
  • the lower three channels run horizontally to the opposite side of the furnace chamber and there merge into a respective vertical heating shaft leading upwards. It has been shown that the concentrated arrangement of three burners in the lower area of the shaft/furnace can create an intensive heat source there, which leads to temperatures of > 500° C being formed in the chamber, which are necessary for coke formation.
  • a meandering channel leading upwards is formed in the heating wall above the lower or lowest horizontal channels, in particular as a fourth channel (counting from the bottom).
  • a burner can also be coupled to the meandering channel. It has been shown that advantageous heat distribution can be ensured by means of this meandering channel, in particular in the vertical direction. On the way up, the exhaust gases generated by the corresponding (in particular fourth) burner can cool down slowly, which can ensure a step-like heat transfer into the charge/pile of briquettes in the vertical direction. Such a step-like heat transfer provides various advantages, be it energetic advantages, advantages with regard to the 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.
  • high-calorific gases generated during coking in the respective furnace chamber are removed at 1 to 5 extraction points at different heights, i.e. evacuated from the chamber and fed for further use.
  • a nozzle with a predetermined angle can be provided at the respective extraction point.
  • This measure also has the advantage that the gases released in the individual stages of the coking process can be fractionally evacuated from the coking process and thus fed into a specific gas processing or converted into valuable chemical substances. Fractional extraction is to be understood as extraction at different heights and different gas types or gas compositions. It has been shown that by means of a pre-definable spacing of the sampling points already allows a fairly selective pre-selection with regard to the composition of the gases extracted.
  • one, several or even all extraction points are located at least 50% vertically above the shaft/floor outlet of the respective chamber.
  • This has advantages not least with regard to the arrangement of a stand-off zone in front of the discharge system.
  • This allows raw gases to be extracted from the upper areas and fed back into the shaft via the lower "extraction".
  • the respective lower gas extraction line can also be converted into a gas supply line. This means that gases can be fed locally over hot briquettes, which can have a quality-enhancing effect.
  • the flue gases from the heating or from the coker can be used for the dryer circuits.
  • a controlled partial extraction can be carried out to dehumidify the circulating drying gases.
  • Steam can also be generated, particularly for steam stations for heating equipment, pipes and fittings. Steam can also be obtained or used for raw gas processing in the form of process steam. If the temperature level is high enough (particularly for exhaust gases from the lowest burners), it can be fed to a waste heat recovery unit or hot flue gases can be fed to a dry cooling system.
  • a gas-tight discharge system is arranged below the (respective) furnace chamber, through which the warm coke can be transferred to a dry cooling device.
  • the discharge system can be designed like a shaft.
  • the discharge system can be set up to receive the amount of coke from 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 it from below without adding water. It has been shown that cooling gas flowing upwards through the cooling shaft coke bed and heating up in this way can be fed to a heat exchanger, in particular a heat exchanger for generating steam, which in particular also results in an improvement in the energy balance.
  • a vacuum system can be provided, in particular in the form of a fan, which vacuum system can be coupled to the dry cooling device and/or the heat exchanger.
  • coke temperatures below the dry cooling device of less than 200°C can be achieved.
  • a rocker or pendulum construction can be implemented for the coke discharge. This allows cold cooling gas to be introduced into the dry cooling device via a free filling surface.
  • a furnace arrangement for producing briquettes comprising a furnace device as described above and a gas evacuation arrangement which is coupled to at least one furnace chamber of the furnace device by means of at least three gas extraction lines in at least three height positions.
  • a method for producing briquettes from carbon-containing solid feedstock comprising both drying briquettes made from feedstock in a briquette dryer along a predefinable first temperature ramp and coking the briquettes to form coke briquettes in a furnace chamber along at least one predefinable second temperature ramp, wherein the second temperature ramp is set by a meandering heating channel and optionally also by horizontal heating channels, and wherein, in order to set the second temperature ramp, gas is evacuated at at least three height positions of the furnace chamber distributed over at least half the height of the furnace chamber.
  • the method is carried out by means of a furnace arrangement as described above.
  • the briquettes are pre-dried with a water content of 10 to 12% by mass and provided for the briquette dryer, and then dried to less than 5% by mass before the briquettes are fed into the furnace chamber. This enables particularly gentle treatment of the feedstock.
  • a specific tool device can also be provided for compacting solid, in particular carbon-containing feedstock, in particular from the group: lignite, low-caking hard coal, biomass, petroleum coke, petroleum coal; into briquettes, with a device for pressing the feedstock.
  • a furnace device 10 in particular a coke oven with several vertical chambers 11 is shown.
  • Feedstock 1 in the form of briquettes 5 is fed to a briquette dryer 15 by means of a feed unit 10.1 and preheated therein, which briquette dryer 15 is arranged above the furnace chambers 11.
  • the pre-dried feedstock 5 can then be coked by indirect heating via heating walls 12 of the furnace chambers 11, in particular according to an exactly pre-definable temperature profile, as explained in more detail below (in particular Fig. 4A, 4B ).
  • drying can take place.
  • a device for dry coke cooling 19 is coupled to the bottom of the respective furnace chamber 11.
  • the feedstock 1, 5, 6 can be fed in and removed in an elegant manner by means of an inlet system 16 and an outlet system 17, each comprising one or more locks 16.1, 17.1, in particular gravity-driven. Coked and dried briquettes 6 can be caught and temporarily stored in a collecting device 17.9.
  • the furnace device 10 has, for example, four to six vertically aligned, vertically loadable furnace chambers, each of which is separated laterally by two heating walls along the yz plane. (in the view of the Figure 1A i.e. from the right and left). The heat transfer takes place indirectly via the heating walls.
  • Fig. 1C It is shown schematically that the dryer 15 can be coupled to several chambers 11. Likewise, the device for dry coke cooling 19 can be coupled to several chambers 11.
  • a temperature curve T over the height z is indicated, with six phases being highlighted here.
  • phase I drying takes place in the briquette dryer, shown schematically here with a linear temperature curve, which temperature curve can optionally also be non-linear.
  • phase II the feed material is transferred to the respective furnace chamber and kept at least approximately at the final temperature of phase I.
  • the feed system can optionally be tempered or have a heating device.
  • phase III a first coking phase is indicated, with a comparatively low temperature increase or flat temperature ramp. This enables particularly gentle heating and gentle expulsion of foreign substances/gas components.
  • phase IV the temperature ramp can be steeper, particularly since the feed material has now already emitted a large proportion of emittable foreign substances.
  • phase V the maximum final temperature during coking has been reached and cooling can take place in the dry coke cooling system.
  • the temperature curve in phases IV and V is shown schematically as linear, and can optionally be set to 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 with a temperature ramp in the range of 0.8 K/min, in particular monotonically increasing without discontinuities up to a temperature in the range of 320°C or over a period of up to 6 hours (phase IV).
  • the gradient of the temperature ramp can then be increased significantly, in particular to 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 hours (phase V).
  • the transition can also be continuous and steady.
  • the upper (first in the direction of material flow) temperature zone (for example the upper, first 4m of the furnace chamber, viewed in the direction of material flow) can be realized with the more moderate temperature ramp using at least one meandering heating channel.
  • the lower (second in the direction of material flow) temperature zone (for example the lower 2m of the furnace chamber) can be realized with the steeper temperature ramp using at least three individually fired horizontal heating channels.
  • Fig.2 shows an overview of the relationship between individual system components of a furnace arrangement 50 or a coal utilization arrangement 80.
  • Feedstock/raw material 1 is fed to a system component for pressing/compacting (in particular two-stage agglomeration), and leaves this system component as pressed pieces or coal briquettes, in particular in disc or puck form. After coking, coke briquettes 6 are then present.
  • the coal utilization arrangement 80 comprises not only at least one previously described furnace device 10, but also a gas evacuation arrangement ( Fig.6 ) and/or the system component for compacting.
  • the individual system components can be cleverly connected to one another, in particular for the purpose of high energy efficiency.
  • a return system 18 with at least one return line from the (respective) furnace chamber back to the dryer 15 is provided, so that exhaust gas G2 from a respective furnace chamber 11 can also be used to temper the dryer 15.
  • Raw gas G1 on the other hand, can be extracted by means of a gas evacuation arrangement 30 and handled for further/reuse.
  • Fig.3 shows details of the dryer 15.
  • Heating elements 15.4, 15.5, in particular hot gas lines at different temperatures are provided in several drying levels or drying circuits 15.6, 15.7, 15.8.
  • the upper heating elements 15.5 are less hot than the lower heating elements 15.4 and can be formed, for example, by a return line of a circuit.
  • hot gas from a hot gas circuit 15a can be fed, for example, at 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 at least two levels.
  • the individual sensors can be components of a measuring device 14 coupled to a control device 20.
  • one or more temperature sensors 14.1, H2O sensors 14.2, and/or pressure sensors 14.3 can be provided, the position of which is only indicated schematically here.
  • 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 previously 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 downwards.
  • the drying circuits 15.7, 15.8 can each comprise two drying levels 15.6, the upper of the two drying levels 15.6 being the cooler level in which drying gas that has already given off heat energy can be extracted.
  • the arrangement thus has at least two inlet and two extraction levels, the temperature and amount of drying gas on the respective inlet levels being able to be individually specified.
  • Each drying circuit can be regulated at least with regard to the volume flow and inlet temperature of the hot gas.
  • the drying gases can be evenly distributed over the individual lines or roofs of a level, for example, using valves, manually adjustable perforated disks or the like.
  • the individual pipes or roofs can be arranged offset from one another.
  • the vertical or diagonal distance between the pipes 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 plane and each open into a vertical exhaust flue (extraction line) 12.3, and are each individually fired by a burner 13.
  • flue is used exclusively for a line aligned vertically in the conveying direction of the coal/coke briquettes, in particular for exhaust lines, i.e. not for horizontal heating channels.
  • a burner axis 13.1 coincides with a longitudinal axis of the respective channel 12.1, at least approximately.
  • a meandering heating channel 12.2 extends over the horizontal single-level channels over several height levels, and therefore also has a large number of reversals or reversal points 12.21.
  • the meandering heating channel 12.2 is also fired by a burner 13. This results in a temperature gradient that decreases towards the top. In other words: briquettes fed into the furnace chamber are initially very carefully tempered, and further down in the area of the horizontal single-level channels 12.1 are subjected to a continuously increasing energy supply.
  • At least one observation point 12.22 or measuring point for measuring sensors 14 can 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 can have one or more vertical passages 12.5.
  • the vertical passages 12.5 allow a short-circuit in terms of energy supply and vertical or horizontal energy distribution in a certain sense.
  • the vertical passages 12.5 can be switched (open, closed, intermediate positions) using slide blocks 12.9, for example. This allows the coking process to be monitored and the temperature profile in the chamber 11 to be specifically influenced.
  • Measuring sensors 14.4 can also be provided specifically in the observation point.
  • an access channel which can also be accessed manually, can be provided within the heating wall.
  • the vertical exhaust ducts arranged in front of the front sides of the heating walls can have connections to each heating channel section of the fourth heating channel, in particular to enable additional heating control as a function of the feedstock used.
  • a meander channel 12.2 can thus 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 pre-definable temperature profile, be it in a vertical or horizontal direction.
  • critical temperature ranges for example 350 to 410°C or 410° to 470°C, can be deliberately avoided or at least limited to a short, locally small temperature zone.
  • the positioning of the slide stones can be done, for example, via regulating slides on observation openings 12.22.
  • the vertical passages 12.5 can be distributed in a matrix-like manner over the heating channels, so that a variety of options can be realized when adjusting/regulating the energy input into the furnace chamber.
  • a control device can communicate not only with all burners, but also with valves or flaps for supplying air and/or with valves or flaps on the respective vertical passage or with a device for moving stones to open and close a respective vertical passage.
  • observation points 12.22 each equipped with sensors 14.4, it is possible to monitor the temperature of the furnace chamber and to optimize/regulate it in a comparatively precise manner.
  • FIG. 4B A top view of the xy plane is shown.
  • Fig. 4C an xz side view is shown.
  • Gas outlets 12.6, 12.7, 12.8 are already indicated in three different height positions, which in Fig.6 is explained in more detail.
  • An optimal heating regime is ensured in particular by at least four external burners 13 per heating wall, 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.
  • the three lower heating channels 12.1 each extend in (only) one height position/height level and are each heated separately by an individual burner. Exhaust gas from the three lower heating channels is fed directly into the exhaust flue 12.3, which extends in a vertical direction.
  • the horizontal heating ducts 12.1 are in particular aligned parallel to each other and perpendicular to the corresponding vertical exhaust duct 12.3.
  • the lower part of the oven is preferably no longer heated and is intended for the cooking of the coke and the pre-cooling of the coke (approx. 1m).
  • This part can be described as a standing zone, which can support complete cooking and complete outgassing, which has a positive influence on the coke quality.
  • the briquette dryer is located above the furnace chambers and can be fed with exhaust gas from the respective burners via the (vertical) exhaust ducts.
  • This exhaust gas can be used as a drying medium in two separate drying circuits within the briquette dryer, which are referred to here as the dryer pre-stage and the dryer main stage.
  • Two drying circuits can be provided, in particular each fed by thermal energy from burners of the furnace device. Both circuits can optionally be equipped with additional, external burners, in particular for the purpose of redundancy or more flexible setting options.
  • Hot exhaust gas from a primary heat generation can be provided by at least three external burners, which are connected in particular to three horizontal heating channels arranged at the bottom of the respective furnace chamber.
  • Hot exhaust gas from a secondary heat generation can be provided by at least one external burner, which is connected to a meandering heating channel located above the horizontal heating channels.
  • Fig.5 shows individual components of a dry cooling device 19 arranged below the furnace chamber 11.
  • a pump 19.1 and a heat exchanger 19.3 operate a gas circuit 19.5 in which the coked briquettes 6 are cooled in countercurrent in a cavity 19.7, the gas being fed into the cavity through at least one inlet 19.9 and being evacuated again through at least one outlet 19.8.
  • the outlet is arranged just below the furnace chamber 11 and is sealed off from it by baffles or protruding walls. This arrangement has the advantage that the briquettes from the furnace chamber 11 are first surrounded by cooling gas that is already quite hot.
  • At least one flow-inhibiting roof or gas diversion unit 19.6 is arranged centrally within the cavity 19.7. This allows the flow profile to be adjusted. In particular, it can be avoided that a main energy or mass transport forms in the center of the cavity 19.7.
  • a special feature of the vertical chamber furnace is that the dry coke cooling system is arranged "precisely" under the furnace chamber.
  • the cavity of the dry cooling device can therefore have the same cross-sectional profile as the furnace chamber. This facilitates direct, gravity-driven conveying of the briquettes and can simplify continuous operation.
  • the transition is particularly seamless because there is no physical separation between the furnace chamber and the dry cooling device.
  • At least one roof or gas diversion unit 19.6 arranged in the radial direction, in particular centrally, can ensure that the cooling gas is distributed homogeneously in the radial direction and, in particular, is also guided to the outlets 19.8 in a homogeneous manner.
  • Fig.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. Furthermore, 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, each also comprising a coupling 33.1. Furthermore, several mixers 35.1 and at least one pump 35.2 are provided for further handling of the evacuated gases. Corresponding gas outlets or connections 12.6, 12.7, 12.8 are provided on the respective furnace chamber 11, each in the corresponding height position.
  • the raw gas can be extracted at at least three height levels, each individually for each furnace chamber: via a riser pipe in the furnace ceiling (topmost height position), through one or more connections arranged at a predefined height position in the furnace chamber and further by one or more vertical exhaust ducts, in particular within the respective heating wall (middle height position), and further by one or more connections arranged at a predefined height position of the furnace chamber and further by one or more vertical exhaust ducts, in particular within the heating wall (lowest height position).
  • the extracted raw gas can be cooled and collected via separate raw gas collection lines and then brought together in one or more raw gas collection lines. It has been shown that with direct raw gas extraction (especially immediately downstream of a lock device in the briquette feed system), the risk of raw gas passing from the furnace chamber into the pre-dryer can be reduced, particularly due to the negative pressure that is created here. This can further increase the quality.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Vertical, Hearth, Or Arc Furnaces (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • Coke Industry (AREA)
  • Drying Of Solid Materials (AREA)
EP18716579.0A 2017-04-13 2018-04-04 Ofenvorrichtung und verfahren zur herstellung von koks Active EP3609981B1 (de)

Applications Claiming Priority (2)

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DE102017206450.1A DE102017206450A1 (de) 2017-04-13 2017-04-13 Vorrichtung und Verfahren zur Nutzung von kohlehaltigem Einsatzstoff sowie Verwendung
PCT/EP2018/058525 WO2018188996A1 (de) 2017-04-13 2018-04-04 Vorrichtung und verfahren zur nutzung von kohlehaltigem einsatzstoff sowie verwendung

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CN111996024B (zh) * 2020-08-05 2021-11-30 北京科技大学 冶金粉尘与高硫煤复合制备高反应性焦炭协同脱锌固硫方法
CZ202162A3 (cs) * 2021-02-10 2022-06-29 THEODOR DESIGN, s.r.o. Způsob provádění termického rozkladu a zařízení pro termický rozklad
CN114249548B (zh) * 2021-12-15 2022-11-08 广西柳州钢铁集团有限公司 燃气双膛窑稳定掺配燃料方法
CN115259700A (zh) * 2022-08-03 2022-11-01 河北天峰碳酸钙有限公司 间隔加热式焙烧石灰窑

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JP2020516842A (ja) 2020-06-11
EP3609981A1 (de) 2020-02-19
CN110520507B (zh) 2021-12-17
JP7053662B2 (ja) 2022-04-12
DE102017206450A1 (de) 2018-10-18
WO2018188996A1 (de) 2018-10-18
UA125351C2 (uk) 2022-02-23

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