JP7053662B2 - Devices and methods for utilizing carbonaceous raw materials, and their use - Google Patents

Description

The present invention relates to an apparatus and a method for utilizing a carbonaceous feedstock, respectively, and also relates to a related use of the feedstock. More specifically, the present invention relates to an apparatus and method for producing coke from a feedstock, which is currently not possible or currently satisfactory for standard use. It has not yet been possible to obtain a successful final product. More specifically, the present invention relates to devices and methods according to the preambles of their respective independent claims. Further, the present invention relates to the use of individual components or devices specifically in connection with these alternative feedstocks.

Coke and carbonic / carbon-containing feedstocks are now, and will continue to be, representatives of materials that are essential basic materials for many national economies on the planet, or that are themselves valuable in their actual form. Will. So far, coking has been done primarily with highly viscous bituminous coal (known as fatty charcoal). However, some types of coke are likely to run short in the global market in the very near future. In particular, the availability of coking coals that are very suitable for coking will be reduced, and as a result, less viscous coals or considerable coking coals will be produced in the future, especially for blast furnace coking production. It must be predicted that there will probably be a need to use swelling coal, or other carbon sources. Due to not a little political pressure, alternatives to traditional bituminous coals will be needed in the future, especially in areas including Europe, especially the burning of raw materials as an energy source in the future. This is because it is likely to remain essential for a decade. In Europe, traditional coking coal has been regarded as an important raw material since 2014, but nevertheless continues to be recognized as of greatest economic importance compared to other important raw materials. .. Taken together, it is clear here that there is a contradiction on the one hand and an opportunity or motivation to favorably introduce further optimization measures from the traditional coking process on the other.

Energy conversion is currently progressing only in rich, highly industrialized countries, while developing countries are committed to burning traditional raw materials based on the latest technology years and decades ago. We will continue to rely on it for years to come. However, even in highly developed countries such as Australia, especially Queensland, so that they can continue to improve their raw materials domestically, even in the future, in response to the shift to more modern furnace technology. , Has a high level of investment activity. Thus, it enables the provision of new opportunities for the production or utilization of coke with defined properties or certain types of coke, or for expanding the range of feedstocks available for coke production. There is great interest and high technical demand for equipment and methods. Of course, these measures can also avoid the need for certain raw materials to be transported over long distances around the world.

A specific technical challenge is to produce high-grade coke from finely caking and non-caking coke raw materials, especially lignite. The wider use of such feedstocks may also be of interest in Europe, but this is especially possible with such feedstocks in a more acceptable cost scenario than, for example, bituminous coal. That is why. The present invention particularly relates to this issue, which has recently become more important than ever, making non-conventional feedstock available. Of considerable interest in this context is, for example, the use of feedstocks with high sulfur content, which reveals various applications in which the very resulting sulfur can be used as a by-product. Because it must be.

In many cases, the conversion of coal to high-grade coke is pre-compressed by the raw material or feedstock in a particular way (referring to the briquette / forming of the feedstock to form briquettes). It has already become clear that it can be achieved successfully only if it has been done. Briquettes must withstand high pressures, especially in the furnace chamber floor, which can be several meters high, especially in the case of large vertical ovens, as many briquettes as possible into small particles. It is intended to be crushed. Therefore, the reachable strength of the feedstock is also an important criterion in an advantageous processing design, especially for use in vertical furnaces. One of the interesting issues in the search for new alternative feedstocks and new methods is, therefore, the question of the form of processing in which the alternative feedstock should ideally be provided, and the method by which the associated processing takes place.

As mentioned, the coke oven for coke generation can take a form called a vertical oven. The vertical furnace is charged with raw material briquettes or briquettes from above. Vertical furnaces can range from considerable heights, for example in the range of 30-40 m. For example, using a crane, the briquette is placed above the furnace and slid through the coke shaft (furnace chamber), especially for several hours, especially for several hours, for example 12 or 15 hours, during which time the feedstock is supplied. Equivalent to the time required to convert to coke. In this process, briquettes are subject to temperature changes, especially from an initial temperature of less than 300 ° C to a final temperature of 900 to 1100 ° C. A coke oven typically comprises 2-10 furnace chamber assemblies, forming what is called a furnace bunches. The shaft of each furnace chamber may have a height of, in particular 3.5-10 m, and a width of particularly 150-600 mm. From this it is clear that the briquette is subject to high friction and pressure during coking. Therefore, the strength of the briquette is as high as possible. In addition, there can be intentional volume changes and "effective" mass transfer within the briquette. Therefore, certain porosity is also advantageous.

To provide briquettes, the raw material may be pre-milled, in particular with a hammer mill, more specifically to a particle size of 0 to 1 mm. Second, typically, briquettes are formed by pressing with particle compression, and currently often a briquette shape in the form of elongated blocks with alternating rounded corners or rounded ends is advantageous. It turns out that. Oval briquettes are also a common shape, especially produced by rolling.

Water may be added to increase the cohesiveness of the finely ground material (stickiness of the particles during and after compression). However, high water content can have adverse consequences for briquette strength immediately after coking, resulting in shattering of briquettes, especially in the lower region of the vertical furnace where the maximum force or load acts on the briquettes. , The coking process is compromised.

In fact, it has been shown that throughout the process at various operating steps, difficulties arise, especially when briquette strength is not sufficient, resulting in briquettes / coke briquettes being ground on the floor within the coke shaft. Therefore, in many cases, especially in the case of a large / high furnace chamber, a number exceeding 30 MPa is set as the lower limit of the compressive strength of the briquette. Therefore, sufficient compressive strength is one of the most important criteria when estimating the feasibility of coking the feedstock. Compressive strength can be affected by molding and / or compression, so this process is recognized as of great significance.

Further problems arise, especially when the specific water content of the raw material or briquette is not sufficiently accurate, resulting in high stress on the briquette during heat supply, especially explosion or other forms of disintegration. From the above observations, it can be seen that efficient operation of the furnace requires providing as much raw material or briquette as possible, within narrow tolerances, especially with respect to compressive strength and water content.

Considering these points, the following points should be particularly concerned when searching for new methods and devices. Definition of the heating curve in the furnace chamber specific to the feedstock, method parameters specific to the feedstock, especially during coking and during the processing of the feedstock into briquettes, especially with respect to the gas generated during coking. Definition of temperature, duration, pressure, utilization and disposal options, both between material and type and volume balance.

At present, coke production is carried out in either a gas furnace having a vertical chamber or a coke oven having a horizontal chamber. The latter are two types, namely (integrated) horizontal chamber furnaces, in which a narrow furnace chamber and a horizontal furnace with an indirect heating upright filling chamber (charge standing upgrade), and a so-called heat (non-heat). ) A recovery furnace, which is equipped with an arched furnace chamber and a horizontally long filling chamber (charge lying flat), and can be classified into a heat (non) recovery furnace that can be directly heated from above at least. Current assumptions are that these two types of coke ovens are unlikely to be optimized as desired for future work in raw material utilization. It seems that new concepts must be developed for the new era of coke ovens, especially in the face of the desire to utilize different types of different feedstocks in coke ovens. Therefore, the concept of a new furnace, which is particularly suitable for the use of the (coal) feedstock that has been commonly used to date, is presented below.

An object of the present invention is an apparatus and method initially having the described features, which are non-conventional feedstocks, more particularly sub-coal and / or slightly viscous bituminous coal and / or biomass and / or petroleum coal. Is also to provide equipment and methods that enable high efficiency and gentle coking, especially in vertical furnaces. It is desirable to provide high quality final products (more specifically coke briquettes) even from non-conventional feedstocks. The purpose is also to make the product obtained after coking available as much as possible in the same or similar manner as has been done in the case of conventional feedstocks such as conventional bituminous coal briquettes. It can also be seen as preparing, providing, and / or managing the feedstock of. The device and method are also intended to make coking from a very wide range of non-conventional feedstocks attractive.

One of the ways in which this objective can be achieved is, preferentially, the furnace equipment detailed below, in particular at least one from the group of sub-coal, microviscosity and blue charcoal, biomass, petroleum coke, petro-coal. With at least one vertical furnace chamber for producing coke from one solid feedstock, particularly at least one briquette dryer having a coke oven and installed to heat control briquettes made from the feedstock. Further, in particular, under the briquette dryer, a furnace device having at least one furnace chamber connected to the briquette dryer and having a heating wall, the briquette dryer is a heating facility and a briquette that can be heated by the heating equipment. With a storage, the briquette dryer rises continuously in the briquette storage, or gradually in the direction of transport of the briquette, especially at least two or three temperature levels in the range of 60-200 ° C. Depends on the furnace equipment installed to establish the temperature.

The furnace apparatus preferably further comprises a carry-in system with at least one locking facility, wherein the carry-in system is located between the briquette reservoir and the (respective) furnace chamber and from the briquette reservoir (each). ) It is installed to supply briquettes to the furnace chamber.

In connection with the feedstock described herein, it has been found useful to carry out temperature adjustments to the various rising temperature levels in a very reliable manner. In this way, in particular, it is possible to reduce the water content of the briquette to the desired value in a gentle manner. These preparatory measures have been identified as important for subsequent coking operations. Through controlled briquette processing, especially in combination with a controlled temperature control system in the furnace chamber, the quality of a particularly wide range of feedstock can be improved. Therefore, it will not be impossible for at least some of these feedstocks to be made from materials from the log or cement industry.

The temperature level may be raised constantly and / or even at a specific temperature level set specifically for the various height planes of the reservoir in which the briquette is carried in the direction of gravity. good. The desired temperature level may be adjusted individually for each operation or feed.

A continuous operation of coking may be established in each vertical furnace chamber. The briquette floor in this case moves through at least one temperature zone with elevated temperatures. The desired throughput in this case may be established and adjusted, among other things by the unloading system. Compared to batch operation under fixed temperature conditions, in this case, for example, coal to coke conversion / upgrade can occur continuously. There may be a temperature control system, the operation may be affected, and / or by-products may be discharged in individual temperature zones.

Continuous operation in a vertical furnace also has advantages with respect to temperature stresses, for example on the material of the furnace equipment, more specifically silica. The material can be kept primarily at temperatures above 600 ° C or even at 800 ° C, eliminating the need for repeated cooldowns to lower temperatures. As a result, there is less stress / cracking on the material.

The furnace device may be equipped with a supply unit for providing the briquette to the briquette dryer. The feed unit may also be installed, for example, to transport the generated briquette from the press to the briquette dryer. The feeding unit is installed at least to ensure that the briquette is fed to the dryer continuously or in batch.

Upstream of the dryer is a fuel depot where briquettes can be fed continuously or in batches and from which briquettes can be delivered continuously or in batches, especially to the briquette dryer by sliding the briquettes. ing.

The carry-in system may be located above the (respective) furnace chamber. This allows the supply to be gravity-based.

The furnace device is preferably designed as a whole as a vertical furnace with a vertical furnace chamber. A vertical furnace chamber is a furnace chamber in which briquettes are transported vertically through it, especially on a gravity basis.

Feeding materials may include, among other things, the entire range of soft charcoal, matte and glossy lignite, and long flame charcoal. Good results have already been achieved, especially with lignite from Rhein, Lusatian and Indonesia. It has also already been found that the devices and methods described herein are also suitable for the use of Russian lignite and long flame coal, as well as petroleum coal. Raw materials of supply may include, among other things, the following coal types and peat, based on classifications by DIN, ASTM, and the United Nations Economic Commission for Europe (UN-ECE), and the following are outlined herein. It was remade in. In the context of the present invention, the coals that have been found to be particularly suitable for use with reference to the German DIN include soft lignite, matte lignite, glossy lignite, and long lignite classified by the DIN. Lignite can be mentioned.

The above numbers in the table are% by weight with respect to the number of volatile components and the measurements were made under "waf" conditions, i.e., anhydrous and ashes-free.

The above objectives are particularly for at least one vertical furnace chamber for producing coke from at least one solid feedstock from the group of sub-coal, finely caking bituminous coke, biomass, petroleum coke, coke ovens, especially in coke ovens. At least one briquette dryer in the form and installed to heat control briquettes made from feedstock, and at least one furnace chamber connected to the briquette dryer, especially under the briquette dryer. A furnace apparatus comprising and having a heating wall, wherein at least one horizontal heating channel and at least one horizontal heating channel on at least one side of the furnace chamber in at least one of the heating walls in the lower half, particularly in the lower third. On top of that, there is also a heating channel at least in the upper half or at the beginning of the middle 1/3, which is meandering and extending in various height planes, each with at least one heating channel. Achieved according to the present invention by a furnace device, which can be individually heated by a burner. This type of heating can provide a number of advantages described herein, among other things, independently of any particular configuration or mode of operation of the briquette dryer. Bricket dryers offer advantages, especially for processing briquettes before they are supplied to the furnace chamber. The heating channel then acts on subsequent stages of operation on the briquettes in the furnace chamber. As mentioned, both measures relate to a very precisely regulated temperature control system or energy supply to the briquette. The more accurate the processing upstream of the furnace chamber, the more accurately or effectively the energy supply to the furnace chamber can lead to the desired effect.

According to an exemplary embodiment, there are a number of horizontal heating channels that can be heated by the burner on at least one side of the furnace chamber in at least one of the heating walls, in particular at least three horizontal heating channels each. Individually heated by at least one of the burners. According to an exemplary embodiment, there are at least three horizontal heating channels and one meandering heating channel above it on at least one side of the furnace chamber in at least one of the heating walls in the lower half. Each heating channel can be individually heated by at least one burner. This provides an advantageous arrangement, especially with respect to heat regulation, in each case.

According to an exemplary embodiment, the meandering heating channel comprises an inversion point having an observation site, the observation site having a sensor located on it, or making measurements there, the sensor particularly temperature. It is a sensor. According to an exemplary embodiment, the meandering heating channel comprises at least one inversion point, in which a closed observation site, particularly operable by an adjustment slide from the outside, is placed. According to one exemplary embodiment, at least one of the heating channels, especially at the inversion point, has adjustment slides (open, closed, intermediate) for sliding blocks and / or measurement sensor systems. At least one observation site is located. This makes it possible to optimize the type and method of heat regulation in each case.

According to an exemplary embodiment, the manually accessible access tube for the adjustment slide is connected to at least one of the heating channels, particularly the meandering heating channel. This also simplifies any adjustment.

According to one exemplary embodiment, the meandering heating channel comprises one or more vertical channels. This also opens up additional possibilities for heat regulation.

According to one exemplary embodiment, the meandering heating channels are installed in one or more horizontal or vertical positions so that they are short-circuited / short-circuited, especially by cleaning or blocking the vertical flow path. To. According to an exemplary embodiment, the meandering heating channel comprises one or more vertical channels, each of which is populated with at least one regulator, in particular an externally operable sliding block. This also allows, in each case, particularly fine adjustments, or adjustments at specific local focal points.

According to one exemplary embodiment, the briquette reservoir for briquette drying is measurable and at least less than or equal to the temperature, moisture content, especially 60-105 ° C., in a briquette reservoir in a coordinated manner. A group that includes a first temperature level of 95 ° C. or lower and a second temperature level of 105-200 ° C., and may include at least one additional temperature level including a temperature level of 95-105 ° C. It is possible to heat up to at least two different temperature levels as a function of the measurements consisting of, especially at at least two different height positions in the briquette reservoir. The upper limit of the final temperature level may be specifically established so that there is no volatile component removal yet. The upper limit of each temperature level may be selected from temperature values previously known for a particular feedstock and, for example, temperature values stored in a data memory, or during operation, especially on / in a briquette dryer. It may be specified by at least one pressure sensor and / or gas sensor and / or moisture sensor. This allows the briquette to be continuously and more strongly dried in a gentle manner without excessive temperature stress or material stress.

According to one exemplary embodiment, the briquette reservoir as a function of the measured values for adjusted drying of the briquette is at the outlet of the briquette dryer with a minimum moisture content of 1-5% by weight, especially 2-4% by weight or less. It can be heated up to the point of value. This allows the briquette to have a moisture value of less than 5% by weight from the starting moisture content in the range of 10-15% by weight in a gentle manner, which is advantageous for subsequent coking. In this case, a moisture sensor and / or a temperature sensor may be present in the briquette dryer, particularly at each height position. It may be sufficient that the temperature adjustment is carried out exclusively as a function of the water content, provided that the measurement accuracy is sufficient. Moisture content can be measured, for example, using volumetric or spectroscopic methods. However, preferably there is surplus measuring equipment, especially for pressure, volume and / or temperature measurement. The adjustment is preferably made, among other things, via temperature measurement, or may be done only through temperature measurement.

Especially for lignite, drying has been found to be particularly useful in the temperature range of 60-200 ° C, especially 100-200 ° C. Drying is preferably carried out up to an upper limit temperature, from which it is known that each feedstock begins to remove volatile components (gas discharge). This upper limit temperature may be preset for each feedstock, and in the case of adjustment of the drying process, such an upper limit may be called from the data memory and used as a target numerical value.

With this type of briquette storage, the drying process has also been found to be uniquely adaptable to each feed. The above temperature and moisture content may be further limited to, for example, lignite or bituminous coal. The feedstocks have different _H2O contents, and the mass transfer process during drying is unique to each feedstock, especially due to the structural differences of the materials (micropores / mesopores / macropores).

As far as lignite is concerned, it has been found that an upper limit of 200 ° C. can find a good compromise for effective prevention of removal of volatile components of _H2S , for example, although it is effective drying. Avoiding the removal of volatile components of _H2S may be desirable, especially when used to heat control the recycled flue gas in a briquette dryer.

The furnace device may have control equipment and measurement equipment connected to it, which are installed to control / regulate the drying or coking of briquettes. The control equipment here may be installed or specifically intended to control / adjust the drying process based on the measured values. The control equipment here may also be installed or provided for a single step of any of the method steps described herein, in each case communicating with the corresponding sensor of the measurement equipment.

According to an exemplary embodiment, the briquette dryer comprises at least one dryer unit, in particular a roof dryer unit, which is a thermal gas circuit, for the purpose of introducing thermal energy into the briquette. In particular, it is equipped with a partition from the briquette. The separation between the hot gas and the briquette can be accomplished by a partitioned hot gas circuit. The heat gas in this case can flow in the lines covered by the roof or otherwise in the inclined pipes, and on these lines, and the briquette passes through without staying on the lines.

The dryer unit here may be installed for the continuous transport (continuous operation) of the briquette based on gravity, in which case the briquette reservoir is particularly separated from the heat gas circuit and integrated into the dryer unit. .. Other types of drying, such as fluidized bed drying, have been found to be feasible, or at least not a good idea, especially because they cannot pretreat briquettes in the same gentle manner. The dryer units described herein are capable of effectively adjusting the heat energy introduced and, moreover, allow gentle drying in a unit whose structure is inexpensive and sturdy. The number / density of heating lines may be increased towards the bottom to allow continuous introduction of additional thermal energy without the need for particularly complex adjustments.

The briquette dryer here can also serve as a shock absorber. Preferably, above the highest / top dry level, there will always be multiple planes of the buffered briquette, especially to prevent short-circuit flow of dry gas. This multi-layer shock absorber of the supplied briquette is also capable of extracting dry gas under suction with a uniform distribution.

The shape and arrangement of the individual roofs of one height plane in the briquette dryer, especially the angles and spacing, as well as the height spacing of the drying planes, such that no solid bridges are formed, and the gravitational motion of the briquette. It may be something that can be done without interference. Vertical or diagonal spacing of at least 6 times the diameter of the briquette has been found to be an effective compromise between the temperature profile and the degree of freedom of transport or movement of the briquette (especially exclusively gravity driven).

Each drying circuit may carry a blower, as well as fresh dry waste gas (from the heat of the briquette in the coking chamber) and / or an externally generated dry flue from the burner. Gas (especially for the dryer exclusively to ensure a surplus) may be provided.

According to an exemplary embodiment, the briquette dryer comprises a dryer unit having a plurality of drying circuits, each of which comprises at least two dryer planes. This makes it possible to make particularly specific adjustments for each temperature level.

According to one exemplary embodiment, the briquette dryer comprises a dryer unit having a plurality of drying circuits, each of which comprises at least two drying planes. This provides maximum possible flexibility in establishing the desired temperature profile within the briquette reservoir.

According to one exemplary embodiment, the dryer unit defines a plurality of drying planes, in particular at least four drying planes, in which heat gas lines are respectively arranged, each drying plane adjusted to an individual temperature level. If possible, the dry planes are preferably located at least 60 cm apart from each other. This provides an effective compromise between facility complexity and fine temperature controllability.

According to an exemplary embodiment, the briquette dryer or briquette reservoir comprises a height of at least about 2 m, preferably at least 2.5 m or 3 m. This makes it possible to establish an advantageous temperature profile in the height direction, especially in the case of dry planes with wide individual spacing set in advance. Preferably, a temperature difference of at least 25-30 ° C and 35-45 ° C or less is established between the drying planes. In this way, advantageous drying processes have been found to be feasible, especially when briquettes are transported on a gravity basis.

According to one exemplary embodiment, the dryer unit defines a plurality of drying planes, particularly at least four drying planes, where hot gas lines are respectively arranged, each drying plane, particularly at different height positions. Can be adjusted to individual temperature levels, such as with sliders, valves, and / or flow control valves. This allows for continuous and gentle drying of briquettes, especially to higher drying temperatures. The dry plane may require a separate temperature value. The briquettes in the briquette dryer can be transported or transferred to individual drying planes, especially since this can be done continuously, so that drying can also be done under relatively uniform and constant temperature stress.

According to one exemplary embodiment, the briquette dryer or carry-in system is connected to at least two of the furnace chambers, in particular two to six furnace chambers. In this way, briquette supply can be easier and cheaper. The carry-in system can accommodate at least two furnace chambers. In particular, the carry-in system is equipped with a distributor for this purpose. The briquette can be evenly distributed to the individual furnace chambers (especially 4 to 6 furnace chambers), which is preferably a distributor suitable for the movement of gravity-driven mass material by hoppers, pipes, suction ports, etc. Supported by shape. Again, the locking equipment can prevent the generation of gas. Distribution of briquettes throughout the furnace chamber may be feasible, preferably without mechanically movable parts (switches), especially with what is called a mandrel. Mandrels located within or in front of or behind each locking facility can ensure uniform gravity-driven distribution of briquettes. In this context, it is also possible to implement a transverse offset configuration of the locking equipment with a carry-in system having an outlet wider than half the width of the furnace chamber.

Very uniform distribution of briquettes throughout each furnace chamber is also advantageous in that constant operating parameters can be ensured. The operation of the furnace chamber is a subtle interaction between many different agents. For example, if the furnace chamber is not fully filled, the type of heat transfer is not only associated with the extraction of raw gas under suction, but also with the indirect supply of thermal energy to the feedstock. Will be done. If the furnace chamber is not fully filled, there can be an increase in heat input, especially mass-specific.

According to one exemplary embodiment, the locking equipment (each) is equipped with a double flap system, which allows at least two furnace chambers to be connected to a briquette dryer or coke drycooling equipment. Airtightness can be ensured between the individual components by a suitable sealant, especially at each interface, and the interface may be static, so conventional sealants such as gaskets are also used. It is possible.

In this case, the internal volume of the lock, surrounded by a double flap system, can be made available, for example, by a pump that provides discharge to additional components of the furnace equipment or gas flow. The shape of each flap or lock slider can be particularly square.

The furnace equipment may feature a double lock system below at least two furnace chambers, thereby bringing briquettes / coke briquettes or coke brecture from at least two adjacent furnace chambers forward, especially in dry cooling equipment. Can be transported to.

According to one exemplary embodiment, the furnace device is further equipped with a unloading system equipped with at least one locking facility, from the furnace chamber, respectively, of briquettes or briquettes converted to coke briquettes, especially in a gravity driven process. Or installed for pick-up from coke dry cooling operation.

The respective locking equipment of the carry-in / carry-out system is preferably designed as a structure of heat-resistant material having slip-promoting property, for example by Teflon coating. The locking equipment comprises, for example, a slide tilt with an angle of 5 to 35 ° (relative to a horizontal plane). The locking equipment can be driven under motor control and can be operated manually (with manual switches, pushbuttons) or automatically (under time or coke temperature control). The corresponding motor control can interact with, for example, hydraulic, pneumatic, or electric drives.

The unloading system is preferably located below the (respectively) furnace chamber or below the coke-dry cooling operation. The carry-in and / or carry-out systems can be configured as rockers, flaps, levers, taps, sliders, or pendulum structures, respectively. In addition, a switch or distributor or at least one mandrel can be provided, especially on the base of the briquette dryer, or downstream of the furnace chamber, in the form of a triangular shunt, whereby the briquette is uniformly and by gravity. It can be driven and distributed within the lock.

According to an exemplary embodiment, the furnace equipment can be operated downstream of the furnace chamber (each) without water and for gas cooling, especially for inert gas cooling, at least one inlet and at least one outlet. Equipped with coke dry cooling equipment. Coke drywall allows for efficient yet gentle cooling. Since this cooling can be done in a countercurrent across the floor, a continuous temperature profile that can be adjusted as a function of the amount of purge gas used can be established, in particular. Coke drywall equipment can be described as an integrated heat exchanger with a continuous temperature profile.

According to an exemplary embodiment, the coke dry cooling equipment is for gas cooling that flows countercurrently across the briquette floor, and in particular sets up a cooling gas circuit with at least one heat exchanger. Drycooling equipment is preferably equipped with a heat exchanger installed to generate water vapor. The cooling gas circuit can thus achieve a relatively homogeneous temperature profile or temperature gradient on the briquette floor while simultaneously ensuring high energy efficiency. High energy efficiency is of interest at the latest until the economic condition of the entire operation becomes an issue. Therefore, high energy efficiency also directly affects, for example, potential / feasible measures associated with briquette drying.

Downstream of the furnace chamber, the coke drycooling equipment may be connected to at least one of the furnace chambers, in particular by the unloading system of the furnace equipment. The coke drycooling equipment may be connected to 1 to 6 furnace chambers.

According to an exemplary embodiment, the coke drycooling equipment comprises or sets up a cooling gas circuit, particularly with at least one heat exchanger. As a result, the recovered energy can be efficiently used.

According to one exemplary embodiment, in the furnace chamber (each), there are multiple temperature zones with elevated temperatures in the direction of transport of the briquette, with the temperature zone at the first temperature level of 60-95 ° C. , At least a temperature zone at a second temperature level of 95-125 ° C. and a temperature zone at a third temperature level of 125-200 ° C., with one or two additional temperature zones having the same temperature difference between them. It may be included. This makes it possible to control heating not a little in the evaporation region.

The dry cooling equipment may include a cooling gas circuit having a heat exchanger, and the heat exchanger is connected to a water supply line. The heat exchanger may consist of a bundle of tubes and a steam drum, and heat transfer for water supply from the cooling gas heated in the dry cooling facility occurs in a countercurrent, parallel or cross current. obtain.

Dry cooling equipment may include multiple cooling gas inlets and cooling gas outlets, each of which has a flow profile in the flow-crossing briquette floor that regulates the volume flow supplied or removed. Can be established.

According to one exemplary embodiment, the plurality of horizontal heating channels are configured on at least one side of the (each) furnace chamber in at least one of the heating walls, preferably at least one vertical waste. It is connected to a gas flue and can be heated by a burner, in particular at least three horizontal heating channels individually by at least one of the burners. This allows the temperature profile to be established relatively accurately in the furnace chamber. A horizontal heating channel in this context is a channel that is not stretched vertically or significantly. In contrast to meandering heating channels, horizontal heating channels extend into a substantially single height position or horizontal plane.

Regeneration preheating of the gas generated externally in the generator was realized in the 1960s, and the flow direction is reversed every 10 to 30 minutes, so that the cold gas is poured into the checker brick that has been heated in advance. As a result, I was able to heat up. This type of heating channel management system within the wall located on the side of the furnace chamber can be referred to as a "checker brick regenerator". According to the present invention, and in contrast, heating can be done individually in different height planes, without inversion. Each heating channel can be individually supplied with thermal energy.

This antique structure or composition of the heating channel has proven to be quite inflexible and can only be optimized for one source / coal (soft lignite in the Lusatian region) at best. This structure cannot provide an accurate response to different coal / feedstocks.

Indirect heat transfer to each furnace chamber can be achieved by individually heatable horizontal heating channels. Indirect heat transfer in this case refers to the transfer of heat through at least one dividing wall and thus includes heat transfer through the material of the furnace, particularly transfer based on heat transfer within the silica stone brick.

"Indirect" heat transfer ensures that there is no contact between the heating wall and the briquette, especially in between, by providing a temperature change stable, high temperature resistant silica material separation layer. To. Unwanted product contamination of briquettes can be prevented.

Horizontal heating channels that can be individually burned may have a volatile component removal chamber or a volatile component removal zone, where the volatile component removal can be substantially performed in the lower part of the furnace chamber. It provides a relatively high temperature stress and / or a relatively high energy supply to the pre-dried briquette. This can also prevent coking of the purge gas, especially in the upper region of the furnace chamber, and the briquette remains particularly susceptible to temperature stress.

Each of the horizontal heating channels (especially independently of each other) may lead to a vertical waste gas flue, in which the gas can be taken up.

According to one exemplary embodiment, the drying circuit of the briquette dryer is connected to at least one heating channel in the (each) furnace chamber. This makes it possible to utilize the heat generated by the furnace chamber for the purpose of controlling the heat of the briquette dryer. The flue gas from the heating of the furnace chamber can be used to supply as much "dry" flue gas as possible to the circuit of the briquette dryer. The temperature level of the flue gas taken in has been found to be still high enough to operate the dryer circuit. As a result, in addition to simplifying the facility configuration, there is a considerable possibility that energy efficiency will increase. Waste gas (or flue gas) from heating will have a very low O ₂ content, which can be ensured, especially by chemical quantitative combustion. This can prevent any risk of briquette burning.

According to an exemplary embodiment, the furnace appliance comprises at least one return line for gas generated in at least one of the heating channels, said line connecting the (each) heating channel to a briquette dryer. do. This can provide a very energy efficient configuration. The gas generated from the burner can pass through a waste gas recovery pipe or in a hot gas flue, from which it can be guided to a briquette dryer via a connecting line.

The recovery system allows the raw gas to be processed and the processed gas to be used further, especially as a fuel for heating.

According to one exemplary embodiment, the drying circuit of the briquette dryer is connected to at least one heating channel in the furnace chamber. This also has achievable energy benefits.

According to one exemplary embodiment, at least one of the plurality of horizontal heating channels is located outside the furnace chamber and has a flame monitor provided in more detail by the burner connected to each heating channel. Can be heated by a burner operated using natural gas. This allows the energy input to be adjusted relatively accurately. In particular, temperatures of at least 1000 ° C. are feasible on each heating channel. With multiple horizontal heating channels, a very hot volatile component removal zone can be established in the lower region of the furnace chamber in a targeted manner.

Burners with flame monitoring, especially those operated using natural gas, offer the advantages of high flexibility and accuracy for heat regulation (heat input). In contrast, previously, gas generation was done in a separate gas generator located in front of the furnace chamber, with corresponding conduits feeding the furnace chamber. In these gas generators, heating gas was generated by the combustion of coal, which was harmful to the environment.

According to one exemplary embodiment, horizontal heating channels that are placed on top of each other and in contact with each other can be heated by burners placed facing each other. This allows for heat input that is relatively homogeneous with respect to the overall volume of the furnace chamber.

Horizontal heating channels that are in vertical contact with each other preferably lead to vertical waste gas flues at opposite ends. This offset configuration of the burner allows for particularly homogeneous heat input.

According to one exemplary embodiment, the heating channels located opposite each other at the same height position can be heated by burners placed facing each other. This allows for heat input that is relatively homogeneous with respect to the overall volume of the furnace chamber.

The burners can be placed diagonally opposite and at the same height in the furnace chamber. At the height position of the furnace chambers in contact with each other, the burners may be placed on one opposite edge / corner of the sides of the furnace chamber. This allows bi-rotation asymmetry to be generated, i.e., within each height plane and with respect to adjacent height planes.

According to one exemplary embodiment, on at least one side of the (each) furnace chamber, there are heating channels that meander and extend across multiple height planes, which are at least two or three horizontal heating channels. It is placed higher and can be heated by at least one burner. This makes it possible to easily establish a temperature profile that descends upward in the height direction.

According to an exemplary embodiment, there is a meandering heating channel with inversion on at least one side of the (each) furnace chamber, on which at least one measuring point, particularly at least one temperature measuring point and /. Alternatively, the pressure measurement point is located at at least one of the inversions. This allows measurements, especially in temperature profiles.

According to an exemplary embodiment, there is a meandering heating channel with at least one inversion on at least one side of the furnace chamber, on which at least one of the inversions an observation point is placed and more. In particular, the observation point is a closed observation point that can be operated from the outside. This provides a number of options for monitoring and establishing operating parameters in the furnace chamber, especially the temperature profile.

According to one exemplary embodiment, the observation point is located in at least one of the heating channels. Observation points allow for this optical control or otherwise visual insight. This provides options for monitoring and establishing operational parameters.

According to one exemplary embodiment, multiple horizontal heating channels are provided in the heating walls on the sides of the furnace chamber, especially in the facing heating walls, each of which is the fourth heating channel from the bottom to meander in the loops. At least one burner is connected to the fourth horizontal heating channel in the lower region of the furnace chamber, and in the upper region of the furnace chamber the line equipment leading to the briquette dryer is connected. This makes it possible to easily establish a temperature gradient that decreases upward.

According to an exemplary embodiment, there is a meandering heating channel with at least one inversion on at least one aspect of the (each) furnace chamber, and on at least one of the inversions on it the observation point. Arranged and, more specifically, the observation point is a closed observation point that can be operated from the outside. As a result, the target influence can be further exerted on the temperature control system in the furnace chamber. In particular, temperature detection and temperature monitoring may also be performed. The plurality of observation points may be provided at multiple height positions in order to detect not a little temperature gradient. At the observation point, the condition of the attached block can be inspected from the outside. The surface temperature of the block is also measurable and provides information, such as information about the radiant heat generated.

According to one embodiment, there is at least one observation point located in at least one of the heating channels. There you can operate the adjustment slider for the sliding block and / or check if the material of the furnace chamber wall remains intact. There can also be one or more sensors attached. It is accessible from each observation point, for example, from the outside through the skeleton.

According to one exemplary embodiment, multiple horizontal heating channels are provided in the heating walls on the sides of the furnace chamber, especially in the facing heating walls, each of which is the fourth heating channel from the bottom to meander in the loops. At least one burner is connected on the fourth horizontal heating channel in the lower region of the furnace chamber, and in the upper region of the furnace chamber a line arrangement leading to the briquette dryer is connected. This makes it possible to establish a temperature profile that falls uniformly upward over a wide height portion.

This configuration of the heating channel makes it possible to establish the temperature profile in the furnace chamber relatively accurately. Very high temperatures can be flexibly realized in the lower region of the furnace chamber, especially to bring the volatile components in the briquette to the desired level of less than 1% by weight and to end the coking process.

The number of three horizontal channels that can be individually heated has proven to be advantageous on the one hand for individual heating to a high degree and on the other hand for the high thermal energy that can be introduced as a result (eg, about). Desired final briquette temperature of 1050 ° C.).

It has been found that this type of heat input can be carried out over a relatively short distance (in the vertical transport direction of the briquette) by achieving a furnace chamber temperature well above 1000 ° C. It has been found that this heat input is ensured in the lower region of each furnace chamber (on the substrate) by a large number of burners and a large number of individual heating channels in a particularly useful manner. This configuration also allows a flexible response to the required final temperature on an individual basis, depending on the feedstock / coal type. According to our own research, the combination of three horizontal heating channels and one meandering heating channel is particularly numerous for the achievable, highly homogeneous temperature profile and structural cost and complexity. Provide benefits.

Meandering heating channels refer to channels that extend across multiple height planes, which are connected to each other by channel profiles in the form of loops or meandering curves. The channel may in this case continuously increase in height. At the inversion point of the channel, the angle is, among other things, 90 ° or less. The meandering heating channel can provide some kind of spiral heat exchanger.

In previous furnace chambers, in contrast, frequent observations did not allow the heat in the lower region of the furnace chamber to be properly used for coking, resulting in residual coal or coke, especially in the middle of the furnace chamber. Useless coke zones with high fractions of volatile components and low temperatures below 950 ° C. were formed.

According to an exemplary embodiment, at least three horizontal heating channels and above, among others, on at least one aspect of the furnace chamber in at least one of the heating walls in the lower half, particularly in the lower third. There is also a meandering heating channel at least in the upper half, especially at the beginning of the middle 1/3, each of which can be individually heated by at least one burner, and the meandering heating channel is preferably equipped with a sensor. Or it has an inversion point with an observation point to perform the measurement. This makes it possible to combine many of the above advantages. The vertical flow path is preferably formed on the meandering heating channel.

Heating channels equipped with regulators such as sliding block elements have been found to offer a variety of benefits, for example. Through the observation point, the adjusting member can be adjusted / positioned, especially from the outside, using suitable auxiliary structures such as metal hooks, whereby the volume flow flowing into the heating channel is an operating requirement (eg, setting). It will be possible to adjust according to (lowering the flow so that combustion takes place within the meandering channel at the height level). This allows the desired temperature gradient to be accurately established in the vertical direction. In addition, the heating channel may also further include an opening and especially a vertical flow path, which allows partial volume flow to flow from the bottom to the top horizontal channel in the form of a short circuit or bypass. As well as these bypass flows, not only the overall pressure drop of the system but also any temperature that occurs to the maximum can be minimized, especially at each reversal site.

According to one exemplary embodiment, at least three different height positions on the (each) furnace chamber are each located at least one gas outlet for a gas take-up line, the height position is particularly the furnace. It has a height position that is at least approximately centered at half the height of the chamber. This makes it possible to influence the propagation of gas into the furnace chamber and the temperature distribution relatively easily and very effectively. In addition to more homogeneous temperature distribution (avoid coking of purge gas), valuable gas has also been found to be able to be extracted for reuse, especially in the central position. If the feedstock contains lignite, hydrogen _H2 can be emitted, especially at this point. Apart from the reusability of hydrogen (eg, methanol synthesis), controlling the withdrawal of hydrogen by suction makes it possible to optimize temperature distribution very effectively. Hydrogen has high thermal conductivity.

The (each) furnace chamber may have at least three gas outlets located at at least three different height positions in the furnace chamber, through which at least three gas outlets can be ejected from the furnace chamber. Gases / gas types (first gas and at least one additional gas) can be provided.

According to one exemplary embodiment, the (each) furnace chamber comprises a plurality of gas outlets that can be specifically circulated and placed at a plurality of sites at at least one of the height positions. This allows the gas to be taken up with little mass transfer in the vertical or horizontal (or radial) direction. As a result, the coking process can be made more harmless and more selective.

According to one exemplary embodiment, the gas outlet extends to at least half the height of the furnace chamber, in particular at least 50% or more of the height of the furnace chamber. This allows the gas to be taken up so that there is little mass transfer in the vertical direction. This also allows for a wide range of emissions of different gases.

According to one exemplary embodiment, the first height position is located in the lower third of the furnace chamber, the second height position is located in the middle third of the furnace chamber, and the third height. The position is located in the upper 1/3 of the furnace chamber. This distribution along the height of the furnace chamber provides a particularly large number of options for the establishment of coking processes, or otherwise the emission of available gas types.

According to one exemplary embodiment, the first height position is located at a distance of 1-3 m, especially 1.5-2.5 m, from the second height position when viewed from the base of the furnace chamber. To. This allows selective discharge in the main degassing zones, especially in the horizontally heated channel regions where they are individually burned.

According to one exemplary embodiment, the first height position is located at a distance of 3-6 m, particularly 4-5 m, from the third height position. According to one exemplary embodiment, the second height position is located at a distance of 1-3 m, in particular 1.5-2.5 m, from the third height position. Each of these distances is often very appropriate in preventing coking or unwanted temperature anomalies in the purge gas. In practice the distance may be shorter, especially if there are more than three height positions, but this distance between facility / process processing costs and complexity and the simplicity of the facility's structure. It has been found to bring effective compromises.

According to one exemplary embodiment, the first height position is located at a distance of 0-2 m, particularly 1 m from the base of the furnace chamber, and / or the second height position is in the center of the furnace chamber. It is located at a distance of 0 to 0.5 m with respect to and / or the third height position is located at a distance of 0 to 2 m, especially 1 m, from the top of the furnace chamber. This distribution has the advantage that each furnace chamber can be fully taken into account in the process processing conditions and the height position of relatively small numbers can be taken into account virtually completely.

According to one exemplary embodiment, at least three height positions are set, located in the upper half of the furnace chamber. Especially in the upper region of the furnace chamber, this provides high operational reliability with relatively fine adjustments in the releasable gas or the desired temperature profile.

According to one exemplary embodiment, the height positions are each located at a distance of at least 20-25% of the total height of the furnace chamber from each other. This makes it possible to cover a high altitude range.

According to one exemplary embodiment, one of the height positions is provided at the top of the top of the furnace chamber and the top gas generated in the upper region of the furnace chamber is fired by the corresponding gas outlet. Can be discharged from. This allows the temperature profile to be established as accurately as possible, especially in the lower temperature sensitive regions of the furnace chamber. The top height position here does not have to correspond to the top edge of the furnace chamber, but may instead be located at a slightly lower position, for example, depending on the feedstock and process control regime.

According to one exemplary embodiment, the feedstock or briquette that can be supplied to the briquette dryer has a volatile coal content of 45% by weight or more, and a water content of 40% by weight or more than 45% by weight, and / or. It contains or consists of slightly viscous bituminous coal having a volatile component in the range of 28 to 45% by mass, or 12 to 22% by mass. This type of feedstock makes it possible to obtain briquettes that have been upgraded to a particularly high quality.

According to one exemplary embodiment, the furnace device is configured as a vertical furnace, where the briquette dryer is located above the (respective) furnace chamber. In this way, the supply of briquettes can be promoted. In particular, the entire material flow can be regulated using the unloading system. In this case, the temperature profile in the briquette dryer is the temperature profile in the furnace chamber so that when the desired material flow (amount / hour of briquette) in the furnace chamber is established, the desired temperature profile in the briquette dryer is also established. You may try to match with. For this purpose, it is advantageous if the briquette dryer has or is configurable with at least four drying planes or temperature planes. This allows for a response that is particularly sensitive to changes in the material flow.

According to one exemplary embodiment, the coke drycooling equipment is located below the (respective) furnace chamber. This makes it possible to continue the transportation method based on gravity. Due to the small overall layout, the material flow can be easily adjusted.

According to an exemplary embodiment, the furnace apparatus is equipped with measuring equipment and further coupled to it to control briquette drying in a temperature range of 60-200 ° C. and / or a moisture range of 1-5% by mass. Equipped with control equipment installed for coordination, and / or where the furnace equipment is equipped with measuring equipment and further coupled to it, particularly throughput or briquette material by the unloading system connected to the control equipment. Equipped with control equipment installed to request flow. With the same control equipment, both the temperature control regime and material flow during drying and coking can be coordinated, especially as a function of each other.

The (respective) furnace chamber or the heating wall of the furnace chamber may be made of a refractory silica material.

The bulk density of the briquettes in the furnace chamber may be in the range of 650 to 850 kg / m ³ based on the density of 1350 kg / m ³ for each briquette.

According to the present invention, the above furnace device may also achieve at least one of the above objectives, where the individual heating channels are arranged for at least two different temperature gradients / zones. The higher temperature zone is achieved with a moderate temperature gradient by at least one serpentine heating channel, and / or the lower temperature zone with a steeper temperature gradient is numerous, especially at least. It is realized by three individually burned horizontal heating channels.

The above object is also a method of producing coke from at least one solid feedstock from the group of sub-coal, finely caking bituminous coal, biomass, petroleum coke, petro-coal, which is described in detail below, wherein the feedstock is Supplied in the form of briquettes, and especially fed to the vertical furnace chamber of a coke oven, especially to the above-mentioned furnace equipment, briquettes are first fed to a briquette dryer, in which a preset temperature curve. According to the method, it is also preferably dried continuously at the rate of progression of the briquette, especially to at least two or three temperature levels in the range of 60-200 ° C. and then fed to the furnace chamber. Can be achieved. This allows the briquette to be pre-dried and pre-processed and at the same time gently processed, as may be requested very accurately. Here, the briquettes in the furnace chamber may be continuously heat-controlled over a wider range according to the traveling speed of the briquettes. An efficient method is possible by providing an energy supply that gradually and violently increases in the route. The energy supply can be particularly increased as a function of residual moisture, for example by supplying air at individual heating levels with a heat gas that is disproportionate to the temperature gradient between previous heating levels.

Coking of lignite, slightly viscous bituminous coal, or biomass is an operation that should be controlled very accurately, especially to avoid softening (and disintegration) of briquettes. Coke formation in a temperature range called the "plastic region" (especially about 350-410 ° C. for a particular lignite), where the feedstock softens, should be avoided. This can be done by establishing a temperature control regime and / or a heating curve.

In many feedstocks, the main volatile component removal is done in the "plastic region". Therefore, it is within the "plastic region" that the structural composition of the briquette is closest to the risk of modification. By the methods and devices described herein, the "plastic region" can be specifically assigned to a certain height position in the furnace chamber, in particular the height of the meandering heating channel. This makes it possible to monitor the operation and / or adjust to particularly good results to coke the feed material particularly gently.

From experience, it is recommended to resolidify the feedstock at temperatures above about 470-500 ° C. Briquettes made from lignite and slightly viscous bituminous coals appear to be less tolerant of coking, among other things, while passing through the "plastic region". In this regard, there appears to be a risk that briquettes made from these feedstocks will crumble or shatter. Therefore, a temperature profile that is particularly suitable for a particular feedstock should be precisely established. Pre-drying in a briquette dryer can be interpreted as a preliminary step in this regard. Disproportionately high drainage in a short period of time can cause briquette rupture as a result of water spills and gas distillates, even in the temperature range below 350 ° C.

Therefore, the temperature profile can be established not only by extracting the exhaust gas by suction at various height positions, but also by controlling / adjusting the energy supplied by the external burner. In particular, even in meandering heating channels, measures such as cleaning or blocking the vertical flow path can be taken, for example, so that the energy input can be established also in the "plastic region".

The above object is a method of producing coke from at least one solid feedstock according to the present invention, particularly from the group of sub-coal, finely caking bituminous coal, biomass, petroleum coke, petro-coal, wherein the feedstock is briquette. Provided in the form, and particularly fed to the vertical furnace chamber of a coke oven, and more specifically to the above-mentioned furnace apparatus, the briquettes after drying in a briquette dryer meander in a number of height planes. At least one in at least one heating wall of the furnace chamber, in the lower half of the heating channel extending through, especially the lower 1/3, and above it, especially at least the upper half, especially at the beginning of the middle 1/3. Achieved by a method in which the horizontal heating channels are heated more strongly and continuously according to their rate of travel by indirect heat regulation from the outside in the furnace chamber by individual combustion by at least one burner each. .. It has been found that this configuration of the heating wall allows relatively accurate and homogeneous establishment of the desired temperature profile in the furnace chamber, even with indirect heat regulation from the outside. The continuous connection of the individual horizontal sections to form a meandering heating channel allows controlled cooling of the flue gas with a controlled and reduced heat flow density over the height of the heating wall, with continuous heat transfer. .. The heat indirectly transferred through the heating channel can be supplied to suit the load individually. In particular, at least one step of the coking operation has a gradient of elevated temperature within the briquette such that evaporating residual water and further effluent volatile debris are gently removed from the briquette with only moderate pressure. Can be moderately adjusted. At least one later step, especially when the rate of volatile component removal is slow, the temperature or indirect supply of heat energy (as a function of height position) is to complete volatile component removal to a particularly desired degree. , Increases more gently. The risk of weakening the briquette agglomerate structure no longer exists, thanks to at least the first steps taken in advance. The conditions for how to select the rate of increase and the steepness of each temperature gradient, and how to establish many intervals of different temperature gradients, preferably along the height of the furnace chamber. Flexible as a function of the selected feedstock and temperature range, it is particularly adjustable by the apparatus of the present invention.

According to one exemplary embodiment, temperature gradients of different steepness are established in the furnace chamber, in particular using a serpentine heating channel on the one hand and at least one horizontal heating channel on the other, exclusively indirect. By thermally adjusting to, especially after 5-7 hours, especially at the boundary temperature between gradients in the range of 300-350 degrees, the first temperature gradient has a gradient in the range of 0.7-1 K / min. The second temperature gradient has a gradient in the range of 2.5 to 3.5 K / min. This makes it possible to easily optimize the coking process. Here, the transition between the temperature gradients may be continuous or discontinuous. It has been found that continuous transition is only feasible if it is based on the continuous advance (downward slide) of the briquette.

According to one exemplary embodiment, heating of the briquette in the briquette dryer is carried out on a temperature curve of 0.4-2 K / min, particularly 0.8 K / min. This makes it possible to dry very gently. Thermal energy is preferably introduced in two or more stages (hot at the bottom and not very hot at the top) in the heating line of the briquette dryer. This can be done using exhaust gas from the furnace chamber and / or waste gas generated externally by the burner.

Especially for lignite briquettes, a temperature increase of 0.8 K / min has been found to be very advantageous. Particularly advantages arise when the operation is carried out in this case in the temperature range of 60-200 ° C, especially 100-200 ° C. Moreover, it has been found to be very advantageous for the quality of the briquettes obtained if this temperature gradient is established in the furnace chamber and, more specifically, in the upper half or upper two-thirds. It has been found that this can be achieved by meandering heating channels, especially in combination with gas emissions, especially at multiple height positions.

According to one exemplary embodiment, measurements, especially temperature measurements, are made at inversion points with observation sites within the meandering heating channel. According to one exemplary embodiment, the adjustment is performed at at least one inversion point within the meandering heating channel, especially by an adjustment slide from the outside. According to an exemplary embodiment, at least one measurement and / or at least one adjustment with a sliding block is performed on at least one of the heating channels, especially at the inversion point. According to one exemplary embodiment, the short circuit or bypass occurs in one or more vertical channels of the meandering heating channel, especially by cleaning or shutting off the vertical channels. According to an exemplary embodiment, at least one adjusting member for adjustment, particularly a sliding block operable from the outside, is located in each of one or more vertical channels of the meandering heating channel. This provides the advantages already described for each.

According to an exemplary embodiment, the briquette is first fed to a briquette dryer in which, according to a preset temperature curve, as the briquette progresses, in particular at least in the range of 60-200 ° C. It is continuously dried to two or three temperature levels, then fed into the furnace chamber and dried in the briquette dryer to a moisture content of less than 5% by weight before being fed into the furnace chamber. As a result, briquettes can be treated particularly gently. By a preliminary step prior to the briquette dryer, the feedstock is first heated and dried to 20% by weight moisture, then before the briquette is fed to the briquette dryer, and the briquette is particularly less than 5% by weight. It has been found that the feedstock formed to form briquettes is heated and dried to 11% by weight before being fed to the furnace chamber with the water content of.

According to an exemplary embodiment, the briquette is dried in a briquette dryer to a moisture content of 1-5% by weight, especially 3% by weight, at the same time or as a result, at 120-180 ° C, especially 150 ° C. Let it heat up. This can ensure a particularly gentle treatment of briquettes.

According to one exemplary embodiment, the heating of the briquettes in the furnace chamber is a temperature curve of 0.5-5 K / min, particularly 2-3 K / min, especially with respect to the briquette transport direction or in the vertical direction. Performed on a temperature curve of minutes or less, and / or the briquette is heated in the upper furnace chamber for 4-15 hours, particularly 6-9 hours, and / or the briquette is particularly directed or perpendicular to the briquette transport direction. On the other hand, it is heated in the furnace chamber from a starting temperature of 100 to 200 ° C. or 120 to 180 ° C., particularly 150 ° C., to a final temperature exceeding 900 ° C., particularly 900 to 1100 ° C. These temperature conditions provide an efficient method that involves gentle treatment of briquettes.

A continuous process in a vertical furnace allows, for example, a temperature gradient of 100-150 ° C. per vertical meter. For example, a temperature gradient of 2-3 ° C. can be manipulated depending on the vertical material flow / transport speed.

It has been found that coking processes can also be used to further increase the (coking) compressive strength while having a targeted effect on the temperature profile in the furnace chamber. In particular, the compressive strength can be increased from 20 to 25 MPa by 30% to 50% to at least 35 MPa to 45 MPa. The above-mentioned furnace equipment can affect the temperature profile in the furnace chamber in a sufficiently accurate and targeted manner, especially also thanks to gas emissions at multiple height positions.

According to one embodiment, the heating of the briquette is carried out in a plurality of steps depending on the water content, particularly in the first step of 15 to 10% by mass or less, particularly 11% by mass of water, and 1 to 5% by mass of water. It is carried out in a briquette dryer in two steps of the following or a second step of 2-4% by weight or less, particularly 3% by weight. This allows for particularly gentle drying.

According to one embodiment, the heating of the briquette is particularly one or more in the briquette dryers on multiple drying planes at different height positions, until each individually adjusted and preset temperature level is reached. This is done by an individually adjustable dry gas circuit. This makes it possible to have a targeted effect on the energy supply during drying, especially in a manner specific to each feedstock. Adjustments can be completed, especially by volume flow, using, for example, a slider or flow control valve.

It can also be pre-dried, especially from 20% to 11% by weight, before molding the feedstock. Heating of the feed material can be carried out in a plurality of steps depending on the water content, particularly in two steps, a first step to 20% by weight water content and a second step to 11% by weight water content.

According to one embodiment, the compact is heated to 950 to 1100 ° C., particularly 1000 to 1050 ° C. or lower, preferably 1050 ° C. or lower during the coking operation. Undesirable reductions in both the strength and particle size of coke can occur at final temperatures above 1100 ° C, or even above 1050 ° C, depending on the feedstock, and the use of coke in a blast furnace. I know it can be jeopardized.

According to the method, high-strength briquettes can be provided from feedstocks that can be considered alternatives to existing blast furnace coke when these temperature ranges are observed.

According to one embodiment, heating of the compact during the coking operation causes the compact to shrink 40% to 60% by volume, especially 50%, during the coking operation and / or during the coking operation. It is such that the molded product is reduced by 40% to 60% in terms of mass, particularly 50%. Volume changes within this range have been found to be still tolerable for obtaining high intensity values and good combustion properties in some of the coke briquettes.

According to one embodiment, the compact is dried in a briquette dryer to a water content of 1-5% by weight, especially 3% by weight, and at the same time or as a result, to a temperature of 120-180 ° C, especially 150 ° C. Let me. This makes it possible to achieve both gentle and efficient / effective drying.

According to one embodiment, the briquettes of at least two adjacent coking chambers are moved through the unloading system or the components themselves, especially by a double lock, to a dry cooling facility where the cooling gas, In particular, it is cooled to a temperature of less than 200 ° C. with nitrogen. First, it provides an effective method, and second, it also allows energy to be recovered immediately after coking, whether for upstream of the operating step or for other facilities / processes. Condensation formation can be avoided, especially by keeping the entire equipment at a controlled temperature above the dew point, although cooling is actually done below 200 ° C. For this purpose, one or more dew point sensors may be provided. It is also possible to remove the unloading system from the drywall equipment.

According to one embodiment, thermal energy is removed from the heated cooling gas (particularly nitrogen) as a result of dry cooling on the briquette floor, especially in the heat exchanger. This enables a highly energy-efficient configuration, especially in the circulation of cooling gas. The cooling gas can then be used specifically to produce water vapor. In the case of steam generation, steam can be used to generate an electric current (expansion in a steam turbine). The current can then be used for the operation of electric consumers such as pumps, compressors, blowers, locks, valves and the like. All excess current can be sent to the local supply network. Further potential utilization of steam is, for example, as concomitant heating for raw gas preparation on the blank side of the furnace appliance. Steam can be further utilized as a reactant in a chemical process, one example of which is methanol synthesis (keywords: steam reforming / steam reforming, syngas, H20 (shift reaction) to boost hydrogen yield, primary reforming furnace). Is.

According to one embodiment, coke, especially lignite coke with a fixed carbon content Cfix greater than 55% by weight, is produced. This provides favorable physical characteristics for many subsequent applications. In particular, the produced briquettes can be utilized in the DRI (Direct Reduced Iron) process.

According to one embodiment, coke, particularly lignite coke with a very low coke reactivity index (CRI) of less than 24% by weight and a very high post-reaction intensity index or post-reaction strength (CSR) of more than 65% by weight is produced. Will be done. With these values, widespread availability of high-quality coke is expected. Especially when the briquettes produced are available in the blast furnace process.

CRI is determined by heating the feedstock specifically to 1100 ° C. under preset conditions and determining mass loss through outgassing. The CSR can be determined, among other things, by rotating the outgassed material sample in a drum under preset conditions and is similarly quantified as a mass loss value.

According to one embodiment, the coke is allowed to pass countercurrently reactive cooling gas, especially nitrogen, through the briquette floor formed in the dry cooling facility downstream of the furnace chamber, and from the dry cooling facility to the furnace. The device is cooled to a temperature below 200 ° C. by discharging the gas through the carry-out system. This enables a method that is relatively easy to control / adjust and can efficiently recover energy.

_Drycooling equipment is circular and operable, in which case the cooling gas accumulates combustible components such as H2 and CO, due to further degassing events within the coke bed. Cooling gas can be discharged from the _floor and purified to prevent further accumulation of H2 / CO above a certain content and thus to avoid conditions that present safety issues. In particular, in order to burn the combustible components, air oxygen is added to the stored cooling gas before the thermal energy stored in the cooling gas is transferred to supply water to the heat exchanger.

According to one embodiment, briquettes are converted to coke briquettes within 4-15 hours, particularly within 6-9 hours, on the haul path from the briquette dryer to the (respective) furnace chamber.

According to one embodiment, (each) furnace chambers are operated continuously, briquettes are continuously transported (especially downward) into the furnace chamber, and locking equipment (double) for at least two furnace chambers in particular. It is supplied and discharged in batches via a lock). The floor can move continuously in the furnace chamber, and can move in and out in batches, especially at 2-4x / h. The residence time on the floor in the furnace chamber can be adjusted by the unloading speed. Here we can also take into account the fact that the mass and volume flow of the briquette changes during the coking operation, especially based on degassing and shrinkage. The carry-in or supply can therefore be set at a higher mass flow rate than the carry-out.

According to one embodiment, the briquette is vertically fed to and / or taken from the furnace chamber through gravity. This provides various advantages in terms of self-adjusting transport and positioning of briquettes within the device, not a little.

According to one embodiment, the feedstock or briquette supplied comprises 45% by weight (waf) or more of volatile coal components and lignite with a water content of 35% by weight or 40% by weight or more than 45% by weight. , Or from now on. According to one embodiment, the feedstock or briquette comprises or consists of slightly viscous bituminous coal with a volatile coal component in the range of 28-45% by weight (waf) or 12-22% by weight (waf). With each of these compositions, the above advantages can be achieved.

According to one embodiment, the feedstock material flow through the (each) furnace chamber is located below the (each) furnace chamber and is controlled or regulated, among other things by a gravity-based, gravity-driven unloading system. To. This allows for easy control / adjustment of material flow in the furnace chamber, i.e., only via the unloading system (if desired). Each of the effects on material flow is a great advantage here, but it allows the (possible) utilization of additional variables to allow influence on the temperature profile and / or energy input. Because it becomes.

According to one embodiment, the gas is taken up / discharged from the furnace chamber at at least three different height positions. This makes it possible to more effectively establish or confirm the desired temperature profile.

The raw gas mixture of outflowing gas components produced on the floor of the furnace chamber and flowing upwards has a high energy content (high temperature) in the unwanted secondary coking (purge gas or raw gas coking) of the upstream briquette. ) (Undesired accelerated convective heat transfer to the upper briquette), which is currently a typical result. Such secondary coking is a significant disadvantage, especially in high volume vertical furnaces. There is a risk that this result will overlap or alter the temperature profile generated by the sidewalls by the targeted burner control. It has been found that discharging raw gas at different vertical height positions can reduce or completely prevent this result, especially at at least three height positions, including one height position at the top of the furnace chamber.

At height positions located in the middle and lower regions of the furnace chamber, high raw gas temperatures in the upper region of the furnace chamber are very efficiently prevented. Especially hot gas in the lower region can be taken up before rising in the furnace chamber. It can prevent heat transfer in the vertical direction. In particular, hydrogen is discharged in a targeted manner, especially at heights where the feedstock produces hydrogen. Here, the energy supply may be coupled to a suction take-out or discharge system through the burner, especially with respect to the volume flow discharged, in terms of technical regulations.

According to the present invention, in the use of feedstock from the group of sub-coal, finely caking bituminous coke, biomass, petro-coke, petro-coal, in a vertical furnace having at least one vertical furnace chamber, the following properties, 55% by mass: Use to coke feed feedstock into coke with a solid carbon content Cfix greater than or equal to Cfix and / or a CRI of less than 24% by mass and a CSR of greater than 65% by weight, especially in the above equipment or in the above method. The feedstock is tuned along at least two temperature gradients, including at least one temperature gradient in a briquette dryer located upstream of the furnace chamber and at least one temperature gradient in the furnace chamber. Thermally regulated in, the temperature gradient in the furnace chamber is preferably horizontal by meandering heating channels along at least three temperature gradients, including at least two temperature gradients of ascending in the furnace chamber in the direction of travel. At least one of the above objectives is achieved by use, which is also established by the heating channel. Thanks to the inherent thermal conditioning described herein, and especially for all bituminous coke, these values are feasible, and for lignite coke, there is also a relatively high Cfix of over 55% by weight. It turns out to be achievable.

Along with the object of the invention as described above, it is also advantageous to provide an apparatus and method having the described features from the beginning, whereby even in the case of coking non-conventional feedstocks, especially biomass and / or. Even coking of finely viscous bituminous coal or biomass can be coked, especially in vertical furnaces, using highly accurately establishable operating parameters. Here, it may be advantageous to process, provide, and / or handle non-conventional feedstocks so that the overall operation can also be optimized in terms of energy. Here, it is advantageous if the product obtained after coking can be used, for example, in the same or similar manner as possible with conventional bituminous coal briquettes at present.

Also, in this context, to recover the gas available during coking of at least one solid feedstock from the group of subcoal, finely caking bituminous, biomass, petroleum coke, coke to obtain coke. , Gas emission configurations are also provided, the gas emission configurations are set to connect to at least one vertical furnace chamber of the furnace equipment, and the gas discharge configurations can be located at at least three different height positions in the furnace chamber. It comprises at least three gas pick-up lines installed to connect to the (each) furnace chamber at at least three height positions, and the gas discharge configuration is at least three selectively discharged by each gas pick-up line. It is set up to selectively handle one type of gas (first gas and at least one additional gas). This, on the one hand, utilizes the by-products obtained from coking, and on the other hand, provides precise temperature control / regulation and control of the reaction taking place in the furnace chamber, especially by avoiding the propagation of (purge) gas in the vertical direction. It will be possible. Selective handling can also be performed by pumps, valves, and mixers with gas discharge configurations that are connected / connectable to the gas take-up line.

The gaseous material can be taken in a temperature-dependent manner to make the liquid and gaseous material of high quality and especially available from an environmental and / or economic point of view. The emission of gas emissions in the case of coal is carried out in a very clear manner at different temperature levels, depending on the degree of coalification of the coal, and the furnace chamber is maximally accurate and homogeneous at a particular temperature level. It has been found that this effect can be utilized when thermal control / control is possible. Not only the arrangement of the heating channels, but also the arrangement of the gas intake flue / gas outlet has an effect here in terms of adjustability.

This makes it possible to take in hydrogen, for example. Methanol can be recovered. Therefore, the gas emission composition contributes to a very efficient overall operation, including comprehensive and sustainable use of raw materials, and especially coking. This also protects the briquette in the upper region of the furnace chamber from the heat gas from the lower region. The briquette can be guided more accurately along the desired temperature curve. Thermal stress is reduced. It is possible to avoid coking of the purge gas. Further, for example, the condensation of tar vapor generated by briquettes at different height positions is avoided.

Here, the gas discharge configuration can be set for selective transmission or further processing of at least three gases that are selectively discharged. The handling of the gas does not have to be selective, but the gas can be further processed or utilized individually. This option allows for a flexible response to possibly available by-products of development, depending on the particular application.

Gas discharge configurations can be further configured to selectively adjust operating parameters individually at their respective height positions, especially at specific reduced pressures. As a result, the flow path of by-product emissions and / or generated gas in the furnace chamber can be adjusted in an even more targeted manner, even with a relatively small number of height positions (eg, only three). can.

It has been found that there may be complementary effects between heating through the burner and suction removal of raw gas. The raw gas composition varies as individual gases degas over the height of the furnace chamber. As a result, the heat transfer coefficient also varies. The method and corresponding devices allow direct heat exchangers (suction extraction) and indirect heat exchangers (indirect heating of the furnace chamber via a heating channel) to be thermally technically coupled to each other. The entire height portion of the suction extraction site can affect the heat transfer and temperature profile in the furnace chamber.

Selective handling may also include the use of effluxable gas, such as fuel / combustion gas for the burner of the furnace device, as well as the method of operating the furnace device described herein. The raw gas may be used as a fuel for a burner of a dryer, for example. In terms of energy, it is advantageous to provide a circuit for this purpose.

According to one exemplary embodiment, the gas emission configuration comprises a plurality of gas pick-up lines that can be specifically circulated and placed at at least one of the height positions and at the plurality of sites. This also makes it possible to establish and / or control the flow path of the generated gas in the radial direction. Connections to gas take-up lines can be specifically provided in the distribution around and between two circulation positions / sites and, for example, 6 or 8 circulation positions / sites.

According to one exemplary embodiment, the gas emission configuration extends over a height corresponding to at least half the height of the furnace chamber, especially over at least 75% of the height of the furnace chamber. This can prevent the generated gas from causing a secondary reaction or altered temperature profile over a wide range of heights. For example, the gas emission configuration extends over a height of at least 2 m to 3 m when the height of the furnace chamber is 4 m, or at least 5 m to 8 m when the height of the furnace chamber is 10 m.

According to one exemplary embodiment, the first height position is located at a distance of 1-3 m, especially 1.5-2.5 m, from the second height position when viewed from the base of the furnace chamber. To. This allows selective discharge in the main degassing zones, especially in the horizontally heated channel regions where they are individually burned.

According to one exemplary embodiment, the first height position is located at a distance of 3-6 m, particularly 4-5 m, from the third height position. This has a wide range of effects when there are only a relatively small number of height positions.

According to one exemplary embodiment, the second height position is located at a distance of 1-3 m, in particular 1.5-2.5 m, from the third height position. This improves the accuracy and selectivity of emissions for certain types of gas.

According to one exemplary embodiment, the first height position is located at a distance of 0-2 m, particularly 1 m from the base of the furnace chamber, and / or the second height position is in the middle of the furnace chamber. It is located at a distance of 0 to 0.5 m with respect to and / or the third height position is located at a distance of 0 to 2 m, especially 1 m, from the top of the furnace chamber. This distribution provides a good compromise between the cost and complexity of the equipment and the selectivity or effectiveness of avoiding vertical gas flow. In particular, it allows selective gas emission in the main degassing zones.

According to one exemplary embodiment, the gas discharge configuration sets at least three height positions for the gas take-up line, at least two of which are located in the upper half of the furnace chamber. To. This also provides an effective arrangement to prevent coking of the purge gas.

According to one exemplary embodiment, the height positions are each located at a distance of at least 20% to 45% of the total height of the furnace chamber to each other. This makes it possible to include a wide height portion of each furnace chamber, especially in combination with pressure-dependent and / or volume flow-dependent emission control.

According to one exemplary embodiment, one of the height positions is provided at the top of the furnace chamber and the gas emission configuration is arranged and installed to connect to the corresponding gas outlet at the top of the furnace chamber. It comprises at least one connection or at least one gas pick-up line to be made. These can avoid hot gases, especially in areas where the supplied briquette appears to remain very mildly and moderately actuated by thermal energy.

According to one exemplary embodiment, the gas discharge configuration is a separate raw gas cooling, tar shield / separation vessel, tar discharge device, dust for handling the gas that can be discharged from the (each) furnace chamber. It is equipped with at least one component of an electronic filter and desulfurization unit installed for reduction. This allows the exhaust gas to be further processed by the gas-specific individual methods. The discharge device, for example, especially in the case of gas discharged from a specific height position, can condense in the lines in the surrounding atmosphere and prevent tar that causes blockage in these lines.

According to one exemplary embodiment, the gas emission configuration is provided in a parallel arrangement, with multiple gas pick-up lines of the same function that can be connected to different furnace chambers at the same height position, and the gas emission configuration. , Equipped with a mixer to which gas discharge lines of the same function are connected. This configuration makes it possible to further handle the same type of gas from a plurality of furnace chambers. This makes it possible to further reduce the size of the configuration and make its handling easier.

In this context, a furnace device having at least one vertical furnace chamber is also provided, among other things, by the above-mentioned vertical furnace device having the above-mentioned gas emission configuration.

In this context, a method for obtaining gas by coking solid feedstocks for coking, especially sub-coal, finely caking bituminous coal, biomass, petroleum coke, coking feedstocks from the group of petroleum coals, furnace equipment. With at least one vertical furnace and a method for further handling of gas, at least three different gases (first gas and at least one additional gas) are furnaces, especially with the above gas emission configurations. Methods are also provided that are selectively picked up / discharged from the (each) furnace chamber at at least three different height positions in the chamber, selectively handled downstream of the operating step, and more specifically recycled. .. This provides the above advantages.

Here, the various gases may be treated separately. Valuable (single) material may be recycled from two gases / two gases taken at different height positions.

The gas in question is, more specifically, the raw gas that is formed in the furnace chamber under the influence of temperature during the coking operation and rises upward through the floor. The types of gases discharged and handled are: C ₂ H ₆ , N ₂ , NH ₃ , CO, CH ₄ , H ₂ , H ₂ S, CO ₂ , SO ₂ , C ₂ H ₂ , It is formed from C ₂ H ₄ , C ₃ H ₆ , C ₃ H ₈ , especially one or more gases from the group of BTX (benzene, toluene, xylene), and other higher hydrocarbons.

Absorption-removal at different height positions (ie, absorption-removal of a particular exhaust gas) can also be observed very accurately in the desired temperature profile. Under the corresponding conditions, for example, H ₂ has about 6-7 times higher thermal conductivity than that of N ₂ .

According to one embodiment, the first gas is selectively taken up in the temperature range of 150-300 ° C., the additional gas is selectively taken up in the temperature range of 300-600 ° C., and another further gas is taken. , 600-950 ° C or 700-900 ° C. This makes it possible to utilize at least three selectively taken-up gases on the one hand and very effectively prevent vertical convective heat transport in the furnace chamber on the other hand.

According to one embodiment, at least three different types of gas are taken from at least three different height positions, either from a height portion greater than 20% to 30% of the height of the furnace chamber, or in each case. It is taken from the lower 1/3, middle 1/3, and upper 1/3 of the furnace chamber. This ensures that, in terms of technical equipment, it has a wide height impact on relatively low cost and low complexity.

In this case, it is also possible to bridge or cross the temperature range, which is considered to be very important from experience, especially the range of 350-470 ° C., as gently as possible, for example by time optimization. Experience has shown that feedstocks have this temperature zone / temperature range so that adverse events such as "expansion" or "shrinkage / resolidification" that occur with a particular feedstock can be avoided or crossed in this way. Can be transported through. Among other things, for example and also specifically, certain types of gases can be aspirated / discharged at 450 ° C., which have proven to be particularly valuable, and targeted emissions based on height levels. This makes it possible to promote this temperature range only in the small (height) zones of the respective furnace chambers.

According to one embodiment, the first gas is selectively taken up at the first height position within a range of 2 m or less below the top of the furnace chamber, and the additional gas is 35% of the height of the furnace chamber. Selectively taken up at a higher height position within the range of ~ 65%, more specifically 45% ~ 55%, another additional gas is at a higher height position within 2 m above the bottom of the furnace chamber. The height of each furnace chamber is at least 4 to 6 m. This results in favorable configuration and effective impact at the relevant height position in each case and / or at the relevant temporal stage of the coking operation.

According to one embodiment, at least three types of gas include individual adjustments of the discharged volume flow for each type of gas, especially with respect to the discharged volume. This can affect not only the composition of the exhaust gas, but also the temperature profile within the briquette floor. For this purpose, at least one flow sensor may be provided at least on the pick-up line.

Adjustment also allows for targeted effects of vertical gas flow that are probably not completely preventable. For example, the gas pick-up line located further down may have a much lower pressure than the gas pick-up line at a higher height position. The resulting effects are as follows. Vertically upward gas flows can be offset, or gas flows can even be reversed and utilized to influence the temperature profile within the briquette floor. In this context, for each pick-up line, more specifically, individual measurements of gas composition may be made by at least one gas sensor or at least one gas analysis system (eg, spectroscopic or chromatographic analysis). Be wise.

According to one embodiment, further heating of at least three different gases / gas types taken from the (each) furnace chamber is a valuable chemical, such as methanol, dimethyl ether, or synthetic natural gas. Is included in the generation of. This enables a not a little sustainable and economical overall process.

According to one embodiment, at least one of at least three different gases / gas types taken from the (each) furnace chamber is supplied as fuel to a burner that indirectly heats the furnace chamber. This makes it possible to save raw materials and energy. The gas taken up for the burner may consist of at least 97% or less of the following components, C ₂ H ₆ , N ₂ , CO, CH ₄ , H ₂ and CO ₂ . The gas intended for the burner can be taken up at different height positions, especially at three of the height positions. The gas can be purified, especially with respect to BTX and higher hydrocarbons, before being fed to each burner. This improves the functionality of the burner.

According to one embodiment, lignite coke having a fixed carbon content (Cfix) of more than 55% by mass is produced. This method makes it possible to provide high-quality coke for widespread use. Here, the reference variable Cfix can also be defined as coke yield minus ash content.

Also in this context is the use of a gas emission configuration in at least one vertical furnace chamber to expel at least three gas types from the furnace chamber for the purpose of establishing a vertical temperature profile within the briquette floor of the furnace chamber. It is advantageous.

Also, in this context, at least one of the three gas types discharged from the vertical furnace chamber for the purpose of providing fuel gas to at least one burner that indirectly heats the furnace chamber. Use is also advantageous.

Also, in this context, a furnace configuration for producing coke briquettes, which also comprises the above gas emission configuration and furnace equipment, in a furnace at at least one heating wall in the lower half, more specifically in the lower third. The furnace device on at least one side of the chamber comprises at least one horizontal heating channel and, more particularly, a heating channel at the beginning of at least the upper half or middle 1/3, which is also more specifically. A furnace configuration is provided in which the heating channels meander and stretch in multiple height planes, each of which can be individually heated by at least one burner, particularly with the gas discharged from the furnace chamber.

Also, in this context, a method of producing a briquette from a carbonaceous solid feedstock, which is not only for drying briquettes made from feedstock in a briquette dryer, but also for forming coke briquettes in a furnace chamber. Including coking, the gas is discharged at at least three height positions in the furnace chamber, these at least three height positions are distributed over at least half the height of the furnace chamber, and the gas is used for heating the furnace chamber. For this purpose, a method is provided that at least partially passes through a burner placed in the furnace chamber. This method can be carried out by the above furnace configuration.

The raw material briquette passes through each furnace chamber for 4 to 15 hours, especially 6 to 9 hours. In this procedure, the raw material briquette is heated, especially in a multi-stage manner, from an initial temperature of 100-200 ° C, especially 150 ° C to a final temperature of 900-1100 ° C. The required heat can be generated in two channels, which are placed sideways to each furnace chamber and can be heated by multiple external burners, and this heat can be generated in each furnace chamber through a stone split wall. It is transmitted indirectly.

Usually 2-10, especially 4-6 shaft chambers are connected together to form a furnace cluster. The height of each shaft is 3.5 to 10 mm, particularly 5 to 8 m. The width of each shaft is 150-600 mm, particularly 200-400 mm.

Types of coal from which briquettes are made include, among other things, lignite (hard and soft) containing more than 45% by weight of volatile carbon components (vc) and more than 45% by weight of water content. Raw materials processed into briquettes contain 28% by mass or more to 45% by mass of volatile components (particularly gas coal, gas bituminous coal, bituminous coal), or 22% by mass or less otherwise. It may contain slightly viscous bituminous coal containing volatile components (particularly blackened coal and poor coal). Slightly viscous bituminous coal itself has low cohesiveness. In the preceding mixing operation, the slightly viscous bituminous coal may be mixed with an adhesive, thereby increasing the cohesive adhesive effect of the coal particles during the briquetting operation.

Due to the nature of its crucible coke, fatty charcoal in particular represents strong caking charcoal (conventional "coke charcoal"). Further, so-called blacksmith coal and gas coal are also strongly caking coal. All other types of coal are referred to herein as finely caking coal.

Briquettes include anthracite coal (vc <12%), poor coal (12% <vc <19%), gas coal (28% <vc <35%), gas bituminous coal (35% <vc <45%), etc. It may consist of a bituminous coal type, or instead a mixture of these coal types, and high grade fat (coke) charcoal (19% <vc <28%) may also be used. I know. More specific allocations are possible by these percentages and based on the standards for the type of coal.

The raw material may be finely pulverized with a perforated plate roll pulverizer, particularly into pellets having a particle size of 0 to 2 mm. Pellets / particles produced by the perforated plate roll grinder have been found to be particularly easy to bond (easily clot) and thus easy to perform downstream briquetting operations (molding).

After fine grinding, the raw material is molded. This forming process (agglomerates) is preferably carried out in a ram press machine for forming channels. It has been found that high pressure resistant briquettes can be produced by the shape of the channel die in the form of a Venturi tube with a narrow cross section and an outwardly wide cross section. Other types of presses have not been able to produce comparative quality results.

Furthermore, it has been found that very high briquette strength can be achieved when the feedstock is pressed through a narrowed cross section after molding in a mold. Higher briquette strength can be achieved by guiding subsequent feedstock along the expanding runout portion. Advantageously, the narrowing portion is shorter than the run-out portion or shorter than the expanding portion of the cross section.

Flat cylindrical (disk-like, pack-like) briquettes have been found to provide particularly good strength values before and after coking. In particular, when the ratio of briquette diameter to briquette height is 1-5, especially 2-3, good results are also obtained for heating and coking operations. The diameter of the briquette is preferably 20 to 100 mm. Briquettes are produced, among other things, from a coal particle size of 0-2 mm.

The required strength can also be achieved with different dies or different types of presses, and briquettes also have different shapes such as cubes, blocks, plaques, mussels, cushions, balls, or egg shapes. It will be clear that it may be. In the experiments to date, the best experience has been achieved in pack shape.

The parameters of this method are as follows. Press pressure, press time, press temperature. Molding is carried out at a pressure of 120 to 150 MPa, particularly 140 MPa. Molding is carried out, among other things, at a temperature of 60-100 ° C. Molding is performed in a time of 15 seconds or less, in particular.

The types of coal described herein are mixed with a coking assistant in an upstream operating step to make coking more efficient and coke products, for example higher strength or more. It is known that higher quality can be achieved, such as high reactivity.

According to one embodiment, at least one coking aid is supplied during the briquetting operation (during molding), especially to improve the efficiency of the downstream coking process. The coking aids may be selected individually or in combination, especially from the group of coking aids that have already been proven to be useful in conjunction with conventional feedstocks. good.

When lignite is used as a feedstock through the methods of the invention, the carbon content C (fix) of the coke produced may be increased to a value greater than 55%, i.e., the coke produced steel. It has been found that even in the direct melt-reduction process (PRIMETALS COREX / FINEX process), it can be used thereafter.

Prior to the pressing and coking operations, the raw materials are preferably caking in a one-stage or multi-stage mixing operation, especially for improving the quality of the coke produced or facilitating the briquette pressing operation from the finely caking coal species. It is mixed with the (adhesive) system and the coking system. Such an adjunct is preferably mixed at a temperature in the range of 30-120 ° C. prior to briquetting.

Auxiliaries include, among others, sugar honey, sulfite pulp effluent, sulfate pulp effluent, propane bitumen, cellulose fiber, HSC (heavy oil pyrolysis) residues from the petroleum industry, mixed HSC / ROSE (residual oil supercritical extraction). ) It may be selected from the residue or it may be selected in combination.

Usually, a distinction is made between coking aids and cohesive aids, but there may also be aids for certain feedstocks that can fulfill both functions.

It has been found that the addition of water tends to be unfavorable for the coal species described herein with respect to the methods of the invention. Lignite, for example, customarily has a water content of greater than 45%. It has been found that it makes sense to observe some (not too high) water content in order to ensure the high efficiency of the briquetting operation. In particular, a water content of about 20% has been found to be advantageous. Therefore, according to the present invention, pre-drying may also exist.

Subsequent briquetting operations are performed in the temperature range of 40-90 ° C, in particular 55-65 ° C. Due to this agglomerate morphology, a part of the produced briquettes has high compressive strength and wear strength, particularly strength of 30 MPa or more.

The briquette can be installed using a crane above the main dryer and can slide through the main dryer, through the coke shaft, and further to the coke dry cooling device.

During the main drying operation after agglomeration, it has been found advantageous to gently dry the briquette to a moisture content of 2-4% by weight.

The main operation of briquette drying is performed specifically by the roof dryer unit and helps to further reduce the moisture content of the briquette from about 20% by weight to about 3% by weight. In this way, the heat transferred to the furnace chamber is not dissipated to the higher percentage of water evaporation, and this experience has shown that it can also lead to briquette crushing.

The main drying operation is carried out in two stages in particular, but may be a one-stage operation or a multi-stage operation. The drying medium used is preferably thermal waste gas / raw gas resulting from a combustion operation in the heating channel of the furnace chamber located under the dryer, which can penetrate upward into the roof-mounted channel. can.

The arrangement of these channels is especially cruciform for cross-flow management regimes. In some parts, at least, preparations for countercurrent or parallel currents may be made.

For improved drying efficiency, the main drying unit installed for the main drying may be connected to an external burner with flame monitoring, all or two or more, or so by flame monitoring. Otherwise, additional waste gas can be provided for only one drying stage. The main drying unit and each furnace chamber may be separated from each other by a hermetically sealed, especially airtight locking system. The locking system may be connected to at least two furnace chambers, especially in the form of double flaps.

The raw material / feedstock (or briquette) is preferably heated in a coke shaft (or furnace chamber) located below the main dryer by applying a raw material specific temperature control regime. For example, the following temperature control regimes provide benefits. In the first step, the briquette is heated to a temperature range of 300-400 ° C. and operated at a temperature rise of 0.75-0.9 K / min, especially over 0-about 4-7 hours. In at least one further step, the briquette is brought to a temperature range of 300 to 1100 ° C. and heating is carried out at a heating rate of 2.6 to 3 K / min.

For certain feedstocks, it may be advantageous to heat only in one step with a constant heating rate, which can also be associated with the desired high coke intensity.

Thanks to one or more methods of the invention (especially in combination with a unique agglomeration technique for briquette delivery), it is possible to provide relatively high grade coke or coal to the feedstock, desired. The maintenance of the briquette shape, especially the cylindrical pack shape, can be ensured during coking. During the coking process, coal is reduced by 40% to 60%, especially 50%, both in terms of mass and volume, which further results in the desired high compressive strength and wear strength above 30 MPa (especially reaction (CSR)). ) Subsequent coke intensity), as well as low reactivity with a CRI (coke reactivity index) value of less than 55% is required. This upper limit of reactivity is necessary because otherwise the briquettes could start to burn themselves in the presence of air. The quality levels set by these limits are currently not achievable with the current low grade coals described. In particular, current methods and equipment result in cracks in the briquettes or even complete destruction of the briquette shape. Changes in mass and volume can occur at the same rate, among other things.

Thanks to the method of the present invention, the briquette shape (pack shape) can be maintained, so that pressure drop, heat transfer, flow profile, and other method parameters remain preset.

Each furnace chamber is made of refractory silica material in particular.

Aspects for optimizing the heat / energy balance will be described below.

On the sides of each furnace chamber, especially on both sides, there may be heating ducts built into the wall. The heating duct is burned by at least one, preferably four external burners. The burners are connected to the horizontal heating channels, among other things, overlapping. Here, the waste gas or fuel gas from the heating wall is also available for energy, and for this purpose the take-up amine may be supplemented by a flue gas blower.

According to one advantageous and exemplary embodiment, three burners are provided / coupled to the lower or bottom three horizontal channels. The lower three channels run horizontally on opposite sides of the furnace chamber, each of which is an upward induction vertical heating shaft. Centralized placement of the three burners in the lower region of the shaft / furnace has been shown to allow the formation of a strong heat source there, which is the 500 ° C required for coke formation. It means that the temperature exceeding the temperature is generated in the furnace chamber.

According to one advantageous and exemplary embodiment, above the lower or bottom horizontal channel meanders above, especially as the fourth channel (counting from the bottom) formed within the heating wall. There is a channel facing. Similarly, the burner can be linked to a meandering channel. It has been found that this meandering channel ensures a favorable distribution of heat, especially in the vertical direction. As it heads up, the waste gas produced by the corresponding (especially the fourth) burner slowly cools, thereby ensuring vertical briquette loading / gradual heat transfer to the floor. Can be done. This type of gradual heat transfer offers a variety of advantages, whether in terms of energy, or in terms of dimensional stability of briquettes, or in general with respect to mild coking procedures. Burners can be burned, among other things, with natural gas and / or coke oven gas from a coke shaft.

Thanks to the above configuration, it is not necessary to have the costly generator gas unit currently used to generate combustion gas from coal, which actually has some disadvantages in terms of generation, upstream of each furnace chamber. Can be done.

Aspects for sustained use of by-products formed during coking are described below. It is advantageous to extract by-products from different height positions in each furnace chamber, especially in connection with the feedstock described herein, thereby providing high selectivity and even effective temperature control regimes. It is known that various effects are possible.

According to one advantageous and exemplary embodiment, the high calorie gas formed in each furnace chamber during coking is taken out at 1-5 extraction sites at different height positions and thus in the furnace chamber. It is discharged from and used for further use. At each retrieval site, there may be ports with, among other things, preset angles.

At present, there is an unwanted phenomenon, usually in the upper part of the furnace chamber, called coking of purge gas. The purge gas produced by the gas released at the bottom rises in the furnace chamber and causes an unwanted reaction with the briquette placed at the top in an undesired or uncontrollable temperature range. From experience, in these upper regions of the furnace chamber, this is accompanied by unwanted convective heat transfer and coke quality degradation. At present, this means that in many arrangements or furnace configurations, controlling the temperature profile on the floor is not easy. Therefore, coking is done in a somewhat chaotic form.

It has been found that arrangements with extraction sites located at different heights can prevent coking of purge gas, which currently typically occurs in the upper part of the furnace chamber.

In addition, this measure involves fractional discharge of the released gas from the coking process at each stage of the coking operation, supplying them to the unique gas process facility and / or to valuable chemicals. And have the advantage of being able to convert them. In this context, fractional extraction means extraction at different height positions and extraction of different gas types or compositions. It has been found that presettable distances between extraction sites (according to the type of feedstock or coking procedure) also allow highly selective preselection of the composition of the gas to be extracted.

Advantageously, one, two or more of the extraction sites, or otherwise all, are located at least 50% vertically above the shaft / base outlet of each furnace chamber. This is not a little advantageous for the placement of the hold zone in front of the unloading system. As a result, the raw gas can be sucked from the upper region and returned to the shaft via the lower "suction removal" system. For this purpose, each lower gas take-up line may also be re-initiated as a gas supply line. Therefore, the gas can pass locally over the thermal briquette, thereby establishing a quality improving effect.

In downstream operating steps, these emissions can be used to produce high value substances such as methanol, synthetic natural gas, or dimethyl ether. It has been found that these gases can be produced substantially more efficiently if the gas fractions required for that purpose are taken from the coking operation at the location where they are formed.

The conventional equipment has the disadvantage that the gas formed in the furnace chamber can be discharged only in one stage at best. In this case, adverse heat transfer and chemical conversion events occurred not only in coking efficiency, but also in the quality of gas preparation, especially in the upper region of each furnace chamber.

Aspects of long-term use of energy spent or generated during coking are described below. In particular, flue gas from the heating system or from the coking unit can be used for the dryer circuit. In this case, there may be a regulated partial removal to humidify the circulating dry gas. In particular, steam generation may also be used for steam power plants for heating devices, conduits, valves. The steam may further be obtained and / or utilized in the form of process steam for the processing of crude gases. Supply to the waste heat recovery unit may and / or flue gas to the dry cooling facility at sufficiently high temperature levels (especially in the gas of waste gas from the bottom burner). You may.

According to one advantageous and exemplary embodiment, the gas smuggling system is located below the (respectively) furnace chamber and the hot coke can be transferred to a dry cooling facility. The unloading system may be constructed in the form of a shaft. The unloading system may be installed to accommodate the entire amount of coke from two adjacent furnace chambers.

According to one advantageous and exemplary embodiment, the coke is from a temperature level in the region above 900 ° C to a temperature level below 200 ° C, especially with the introduction of cold inert gas, especially from below without the addition of water. Be cooled. Cooling shafts It has been found that the cooling gas that flows upwards across the coke floor and obtains heat in this way can be supplied to heat exchangers, especially heat exchangers for steam generation, especially with improved energy balance. There is. To provide the pressure difference, the reduced pressure system may be provided specifically in the form of a blower, which may be coupled to a dry cooling facility and / or a heat exchanger.

This type of arrangement can achieve lower coke temperatures than drywall equipment below 200 ° C. The rocker, or pendulum structure, may be embodied, for example, for coke pick-up. In this way, cold cooling gas can be introduced into the drycooling equipment through the free floor area.

Also, in this context, a furnace configuration for briquette generation, comprising the above furnace apparatus and further a gas discharge configuration, the gas exhaust configuration is at least three height positions in at least one furnace chamber of the furnace apparatus. Also provided is a furnace configuration connected by at least three gas pick-up lines in. This brings the above advantages.

Also, in this context, a method of producing briquettes from a carbonaceous solid feedstock, the drying of briquettes produced from the feedstock in a briquette dryer along a presettable first temperature gradient, and at least one. Along two preset temperature gradients, including coking of briquettes for coking the briquettes in the furnace chamber, the second temperature gradient is due to a meandering heating channel and optionally a horizontal heating channel. A second temperature gradient is established by gas emissions at at least three height positions in the furnace chamber, the at least three height positions being at least half the height of the furnace chamber. A briquette generation method, which is distributed over, is also provided. This brings the above advantages.

According to one advantageous embodiment, the method is carried out by the above furnace configuration.

According to one advantageous embodiment, the briquette provided for the briquette dryer is a pre-drying form with a water content of 10-12% by weight, followed by 5 before the briquette is fed into the furnace chamber. There is drying to less than% by weight. This allows for particularly mild processing of feedstock.

In this context, solid feedstocks, in particular solid carbon-containing feedstocks, more specifically solid feedstocks from the following groups, sub-coal, microviscosity bituminous coal, biomass, petroleum coke, petroleum coal are molded into briquettes. A specific mold device for this purpose, which is equipped with equipment for molding a feedstock, can also be provided.

Further features and advantages of the invention are evident from the description of at least one exemplary embodiment using the drawings, and also from the drawings themselves. Reference codes not explicitly stated for individual drawings are referred to other drawings. What each drawing shows as a schematic display is as follows.

It is a side view of the furnace apparatus and coal utilization composition by an exemplary embodiment. As an example, an adjustable temperature profile according to an embodiment, spanning the height of the furnace apparatus according to an exemplary embodiment. It is a side view of the furnace apparatus and coal utilization composition by an exemplary embodiment. FIG. 3 is a diagram of individual components of a coal-based fire pot with a fire pot according to an exemplary embodiment. FIG. 3 is a detailed view of the individual components of a briquette dryer in a furnace appliance, according to an exemplary embodiment. It is a partial side view of the wall of the furnace chamber of a furnace apparatus according to an exemplary embodiment. It is a figure which shows the indirect heat control method in a furnace chamber by one Embodiment by a basic figure. It is a figure which shows the individual component of the coke dry type cooling equipment of a furnace apparatus by an exemplary embodiment. It is a schematic diagram which shows the individual component of the gas discharge composition of a furnace device / furnace composition, or the individual component of a coal utilization composition provided with a furnace device according to an exemplary embodiment.

FIG. 1A shows a coke oven having a furnace device 10, particularly a plurality of vertical chambers 11. The feedstock 1 in the form of the briquette 5 is supplied to the briquette dryer 15 by the supply unit 10.1 and preheated therein, and the briquette dryer 15 is arranged above the furnace chamber 11. The pre-dried feedstock 5 is then coked by indirect heating through the heating wall 12 of the furnace chamber 11 according to a temperature profile that can be accurately preset, among other things (particularly FIGS. 4A and 4B). Can be transformed into. Coking may be done before drying. For this purpose, coke drycooling equipment 19 is connected at the bottom of each furnace chamber 11. The supply and removal of feedstocks 1, 5 and 6 can be vividly accomplished by the carry-in system 16 and the carry-out system 17, each of which has one or more locks 16.1, 17 driven by gravity, among other things. It is equipped with 1. In the sectioning equipment 17.9, the coked and dried briquette 6 can be cut out and placed in a temporary storage.

The furnace device 10 comprises, for example, 4 to 6 vertically aligned, vertically fillable furnace chambers, each of which has two heatings along the yz plane (ie, viewed from right to left in FIG. 1A). Heated from the side by the wall. Heat transfer is done indirectly through the heating wall.

FIG. 1C schematically shows how the dryer 15 can be connected to a plurality of furnace chambers 11. The coke dry cooling equipment 19 may be similarly connected to a plurality of furnace chambers 11.

The temperature profile T over height z is shown in FIG. 1B in six steps highlighted here. In step I, drying takes place in a briquette dryer, which is schematically shown here with a linear temperature profile, but the temperature profile may also be non-linear. In stage II, the feedstock is moved to their respective upper furnace chambers and maintained at least approximately at the final temperature of stage I. For this purpose, the carry-in system may be characterized by thermal regulation and / or may be equipped with heating equipment. In stage III, the first coke stage is indicated by a relatively low temperature rise or low temperature gradient. This allows, among other things, gentle heating and gentle elimination of external substances / gas components. At stage IV, the temperature gradient can be steeper, especially because the feedstock has already discharged large amounts of immiscible external material here. The energy supply may increase without excessive stressing the feedstock. In step V, the maximum final temperature during coking can be reached and cooling can be performed in the coke drywall cooling facility. The temperature profiles at stage IV and stage V are shown schematically here as linear, respectively, but may also be non-linear, depending on the stage in progress. At stage VI, coking briquettes will be available or access to further processing at either downstream operating step.

Heating can be achieved, especially initially very gently, with a temperature gradient in the region of 0.8 K / min, especially with an uninterrupted and monotonous rise, up to temperatures in the region of 320 ° C. and / or over up to 6 hours. (Stage IV). After that, the gradient of the temperature gradient is significantly higher, especially up to the value in the 2.8 K / min region, especially with an uninterrupted monotonous rise, up to the temperature in the 1050 ° C region and / or over a maximum of 5 or 6 hours. Can be (stage V). The transition can be continuous and unchanging.

The upper temperature zone (the first temperature zone in the direction of material flow, eg, the upper part of the furnace chamber, the first 4 m in the direction of material flow) is more moderately temperatureed by at least one meandering heating channel. It may be realized by a gradient. Even if the lower temperature zone (the second temperature zone in the direction of material flow, eg, 2 m at the bottom of the furnace chamber) can be achieved with a steeper temperature gradient by at least three individually burned horizontal heating channels. good.

FIG. 2 shows the overall relationship between the individual facility components of the furnace configuration 50 or the coal utilization configuration 80. The feedstock / raw material 1 is fed to the facility component for molding / compression (particularly two-stage agglomeration) and remains in the facility component in the form of a compact or briquette, especially in the form of a disc or pack. This coke-ized product takes the form of coke briquette 6. The coal utilization configuration 18 includes not only the at least one furnace device 10 already described above, but also a gas emission configuration (FIG. 6) and / or a facility component for compression. Here, the individual facility components may be appropriately connected to each other for the purpose of not a little high energy efficiency. A recovery system 18 having at least one return line from the (each) furnace chamber back to the dryer 15 is specifically provided, i.e., even if the waste gas G2 from each furnace chamber 11 is used for heat control of the dryer 15. It will be available. In contrast, the raw gas G1 can be taken up by the gas discharge configuration 30 and managed for further use / regeneration use.

FIG. 3 shows the dryer 15 in detail. Within the plurality of drying planes or drying circuits 15.6, 15.7, 15.8, the heating elements 15.4, 15.5, in particular the hot gas lines, are present at different temperatures, respectively. The other heating element 15.5 is not warmer than the lower heating element 15.4 and may be formed, for example, by the return line of the circuit. At the lower heating element 15.4, the heat gas of the heat gas circuit 15a can be supplied, for example, at the lowest drying level 15.8, with a particularly high energy content. Within the briquette dryer, in particular, temperature and humidity sensors may be present at two or more levels in more detail.

Each sensor can be an element of measuring equipment 14 connected to control equipment 20. In particular, there may be one or more temperature sensors 14.1, H ₂ O sensors 14.2, and / or pressure sensors 14.3, but here they are only schematically shown their location.

The dryer 15 comprises at least one storage 15.1 particularly sized for gravity driven continuous operation. The storage heating equipment 15.2 may be formed by the lines 15.4, 15.5 described above, or may include additional heating elements. The line is preferably located below the roof element 15.3 and around the roof element the briquette can slide downwards.

The drying circuits 15.7 and 15.8 can each be particularly equipped with two drying planes 15.6, and the upper part of the two drying planes 15.6 where heat energy is already carried is a cooling plane, respectively. There, the dry gas can be extracted under suction. Thus, the configuration comprises at least two introduction planes and two suction and extraction planes, and the temperature and amount of dry gas can be individually requested in each introduction plane. Each drying circuit can be tuned at least with respect to the volume flow of hot gas and the inlet temperature. Uniform division of dry gas across individual lines and / or roofs in one plane can be done, for example, via valves, manually adjustable perforated plates, and the like.

Individual lines or roofs may have offset configurations with respect to each other. The vertical or diagonal distance between the lines is preferably at least 6 times the diameter of the briquette.

FIG. 4A shows the heating wall 12 as viewed from the side or in cross section yz. Each of the three horizontal heating channels 12.1 extends in a single height plane, leads to a vertical waste gas flue (take-up line) 12.3, and is individually burned by the burner 13. In the following text, the term "flue" is used only for lines oriented perpendicular to the briquette / coke briquette transport direction, especially for waste gas lines, and therefore not for horizontal heating channels. The burner axis 13.1 in each case coincides with at least the major axis of each channel 12.1. On a horizontal single plane channel, the meandering heating channel 12.2 extends over a number of height planes, i.e. also comprises a number of inversions or inversion points 12.21. The meandering heating channel 12.2 is also burned by the burner 13. The resulting temperature profile is one that decreases upwards. That is, the briquette supplied to the furnace chamber is initially very carefully heat regulated and further below in the region of the horizontal single plane channel 12.1 receives a continuously increasing energy supply.

On each channel 12.1, 12.2, at least one vibration point 12.22 and / or measurement point for the measurement sensor system 14, and in particular an inversion point 12.21, may also be provided. The meandering heating channel 12.2 may include one or more vertical channels 12.5. The vertical flow path 12.5, in a sense, allows for short circuits and vertical or horizontal energy distribution in the energy supply. The vertical flow path 12.5 can be switched by, for example, a sliding block 12.9 (open position, closed position, intermediate position). This allows the coking operation to be monitored and can have a targeted effect across the temperature profile in the furnace chamber 11. Here, the measurement sensor system 14.4 may also be provided specifically in the observation point. In order to make each observation point 12.22 easily accessible, an access tube, particularly a manually accessible access tube, can be provided therein within the heating wall.

A vertical waste gas flue located in front of the end face side of the heating wall allows further control of the connection of the fourth heating channel to each heating channel portion, in particular the heating as a function of the feedstock used. Can be prepared. Adjustments that may be placed within the heating channel, especially the sliding block 12.9, allow it to be hotter, especially in the waste gas flue or in a pre-configured horizontal position, starting from the fourth heating channel from the bottom. There is also the possibility of directing the form of waste gas upwards. As a result, the meandering channel 12.2 can be short-circuited in one or more horizontal or vertical positions. This allows individual heating channels to be heated either vertically or horizontally according to the desired temperature profile that can be individually preset. In particular, dangerous temperature ranges, such as 350-410 ° C or 410-470 ° C, can be avoided in a targeted manner, or at least short and locally limited to small temperature zones. The sliding block may be positioned by an adjustment slider, for example at the observation opening 12.22.

Since the vertical flow path 12.5 can be distributed in a matrix format over the heating channels, it is possible to embody a large number of options for adjusting / adjusting the input of energy into the furnace chamber.

Additional parameters that affect the temperature profile in the furnace chamber arise through the supply of air to each heating channel and / or through the drive / adjustment of individual burners as a function of other burners. That is, the control equipment not only communicates with all burners, but also places air supply valves or flaps and / or valves or flaps on each vertical flow path, or blocks for opening and closing each vertical flow path. It may also communicate with the equipment for doing so.

In particular, thanks to the observation points 12.22, each equipped with a sensor system 14.4, the heat regulation of the furnace chamber can be monitored and its optimization / adjustment can be carried out relatively accurately.

FIG. 4B shows a plan view of the xy plane. In FIG. 4C, an xz side view is shown. In FIG. 4C, the gas outlets 12.6, 12.7, and 12.8 are already shown at three different height positions, which will be described in detail with reference to FIG.

For optimal heating control regimes, in particular at least four external burners 13 are provided for each heating wall, oriented in the x-axis or y-axis direction, and alternately placed in front of and behind the furnace chamber 11 facing each other. To.

Each of the three lower heating channels 12.1 extends to one height position / height plane (only) and is heated separately in each individual burner. From the three lower heating channels, waste gas enters the vertically extending waste gas flue 12.3 directly. The fourth heating channel 12.2 counting from the bottom extends over multiple horizontal planes and is burned by a single or multiple burners 13 from which waste gas squeezes the rest of the fourth heating channel. It meanders, but the rest lies above the first part.

The horizontal heating channels 12.1 are particularly oriented parallel to each other and intersect the corresponding vertical waste gas flue 12.3 at right angles.

The lower part of the furnace is preferably no longer heated and full coking of coke and pre-coking of coke is intended (about 1 m). This portion may also be described as a reserved zone, which can support complete coke formation and complete deaeration with a positive impact on coke quality.

Regarding the recovery system 18, the following can also be mentioned. A briquette dryer is installed on the furnace chamber and can be fed waste gas from each burner via a (vertical) waste gas flue. This waste gas can be used as a drying medium in two separate drying circuits within the briquette dryer, which is defined here as a pre-dryer stage and a major dryer stage. In other words, it is possible to provide two drying circuits, each of which can be provided by thermal energy from the burner of the furnace device, among others. Both circuits may also be equipped with an additional external burner, especially for extra or more flexible adjustability.

Thermal waste gas from the primary heating system (first drying circuit) can be provided, among other things, by at least three external burners connected to three horizontal heating channels located at the bottom of each furnace chamber. The thermal waste gas from the secondary heating system (second drying circuit) can be provided by at least one external burner connected to a meandering heating channel lying across the horizontal heating channel.

FIG. 5 shows the individual components of the drywall cooling equipment 19 located below the furnace chamber 11. A pump 19.1 and a heat exchanger 19.3 operate a gas circuit 19.5, where the coked briquette 6 is cooled by a countercurrent in the cavity 19.7 and the gas is at least one inlet 19.9. It enters the cavity through and is ejected again through at least one outlet 19.8. The outlet is located just below the furnace chamber 11 and is separated from the furnace chamber by a warp plate or a protruding wall. The advantage of this configuration is that the briquette from the furnace chamber 11 is initially surrounded by a stream of cooling gas that has already been heated to a very high temperature. Therefore, this method provides gentle cooling. Similarly, the (temperature) stress on the briquette is minimized. Nevertheless, cooling can obviously be effective. At least one flow blocking roof or gas diversion unit 19.6 is centrally located within the cavity 19.7. This makes it possible to adjust the flow profile. In particular, it can prevent the main transport of energy and / or mass generated in the center of the cavity 19.7.

A specific feature of the vertical furnace is that the coke drywall is placed "exactly in line" with the underside of the furnace chamber. Therefore, the cavity of the drywall equipment may have the same cross section as the furnace chamber. This is an advantage of direct gravity driven transport of briquettes, which can simplify continuous operation. The transition is particularly uninterrupted, as there is no physical separation between the furnace chamber and the drywall equipment.

In particular, at least one roof and / or gas diversion unit 19.6 centrally located in the radial direction disperses the cooling gas homogeneously in the radial direction, and in particular in a similarly homogeneous manner, the outlet 19.8. Can be ensured to lead to.

FIG. 6 shows a furnace configuration 50 with a gas discharge configuration 30 having one or more gas pick-up lines 31 for a first height position, the gas pick-up line 31 connecting or connecting 31.1. It can be connected to each furnace chamber 11 via. At least one additional height position, here one or more gas take-up lines 33 for the second and third height positions, are also provided, the second and third height positions being similarly concatenated, respectively. It is equipped with 33.1. In addition, a plurality of mixers 35.1 and at least one pump 35.2 are provided for further control of emissions. Corresponding gas outlets or connections 12.6, 12.7, 12.8 are provided on the respective furnace chambers 11 for their respective height positions.

Here, the raw gas is in three or more height planes, each individually for each furnace chamber, via a riser pipe at the top of the furnace (the position of the top type), and the preset height of the furnace chamber. Through one or more connections placed in the up position, and above all through one or more vertical waste gas flues within each heating wall (intermediate height position), and even in the furnace chamber. By one or more connections arranged in a preset height position, and especially under suction, through one or more vertical waste gas flues within the heating wall (bottom height position). Can be extracted.

The harvested raw gas can be cooled and collected via separate / separated raw gas collection lines and then incorporated into one or more raw gas collection lines. It has been found that direct suction removal of raw gas (especially just downstream of the lock facility of the briquette loading system) can reduce the risk of raw gas moving from the furnace chamber to the pre-dryer, but this is not a small amount. It depends on the reduced pressure generated here. Thereby, the quality can be further improved.

1 Feeding material / raw material 1.1 Pellets, especially those produced using a perforated plate roll crusher 2 Coke auxiliaries 3 Adhesives 4 Bricket strands 5 Molded or wrought charcoal, especially disc or packed 6 Molded Or coke briquettes, especially disc or pack type 10 Reactor equipment, especially coke oven 10.1 Supply unit 11 furnace chamber 12 heating wall 12.1 Horizontal heating channel in a single plane 12.2 Serpentine heating channel over multiple planes 12. 21 Inversion or inversion point 12.22 Observation point or measurement point for measurement sensor system 12.3 Vertical waste gas flue (pick-up line)
12.5 Vertical flow path 12.6 Gas outlet or connection at first height position 12.7 Gas outlet or connection at additional (second) height position 12.8 Gas outlet or additional (third) ) Connection in height position 12.9 Sliding block 13 Burner 13.1 Burner shaft 14 Measuring equipment, especially 14.1 temperature sensor 14.2 H2 O sensor 14.3 pressure sensor with temperature sensor and / or _H2O sensor. 14.4 Observation point specific measurement sensor system 15 Briquette dryer, especially a dryer unit with a 15a heat gas circulation with a roof dryer unit, especially a roof dryer unit 15.1 storage, especially size 15 for continuous operation .2 Storage heating equipment 15.3 Roof element 15.4 Heating element, especially line / hot gas line at first temperature 15.5 Heating element, especially line / hot gas line at second temperature 15. 6 Drying plane 15.7 First drying circuit 15.8 Further (second) drying circuit 16 Carry-in system 16.1 Lock equipment 17 Carry-out system 17.1 Lock equipment 17.9 Section equipment 18 For gas from furnace chamber Recovery system with at least one return line 19 Coke dry cooling equipment, or dry cooling equipment 19.1 Pump 19.3 Heat exchanger 19.5 Line system, especially circuit 19.6 Roof or gas diversion unit 19.7 Cavity 19.8 Outlet 19.9 Inlet 20 Control equipment 30 Gas discharge configuration 31 Gas take-up line for first height position 31.1 Connection or connection 33 Gas take-up line for at least one additional height position 33 .1 Connection or connection 35.1 Mixer 35.2 Pump 50 Reactor configuration 80 Coal utilization configuration G1 Raw gas G2 Waste gas

Claims (21)

In a furnace apparatus (10) having at least one vertical coke oven chamber (11) for producing coke from at least one solid feedstock from the group of sub-coal, finely caking bituminous coke, biomass, petroleum coke, petroleum coal. There is at least one briquette dryer (15) installed to heat control the briquettes made from the feedstock, and at least one furnace chamber (11) connected to the briquette dryer. A furnace apparatus (10) comprising a heating wall (12) and a burner (13) disposed at least in the furnace chamber (11), wherein the heating wall is located in the lower half or the lower third. At least one horizontal heating channel (12.1) arranged as a horizontal single plane channel (12.1) and at least above it on at least one side of the furnace chamber in at least one of them. There is a serpentine heating channel (12.2) in half or the middle 1/3, which is meandering and extending in various height planes, each of which is the burner (13). A furnace apparatus (10), characterized in that it can be individually heated by at least one of the above and at least one of the horizontal single plane channels (12.1) leads to a vertical waste gas flue. Claim that there are at least three horizontal heating channels (12.1) that can be individually heated by the burner (13) on at least one side of the furnace chamber (11) in at least one of the heating walls. The furnace apparatus according to 1. The furnace apparatus according to any one of claims 1 to 2, wherein the vertical waste gas flue comprises a connection to each heating channel portion of the meandering heating channel (12.2). The meandering heating channel comprises an inversion point (12.21) with an observation site (12.22), the observation site (12.22) having a temperature sensor on it, or making measurements there, as well as / Or the meandering heating channel comprises at least one inversion point (12.21), on which a closed observation site (12.22) operable by an adjustment slide from the outside is placed and / or the heating channel. At least one of the observation sites is located at the inversion point (12.21), having an adjustment slide for the sliding block (12.9) and / or having a measurement sensor system (14). The furnace apparatus according to any one of claims 1 to 3, wherein a manually accessible access tube for and / or adjustment slide is connected to at least one of the meandering heating channels. The meandering heating channel comprises one or more vertical channels (12.5) and / or the meandering heating channel cleans or shuts off the vertical channels in one or more horizontal or vertical positions. Thereby being short-circuited / short-circuited and / or said meandering heating channel comprises one or more vertical channels (12.5), each of which can be operated from at least one external. The furnace apparatus according to any one of claims 1 to 4, wherein a sliding block (12.9) is arranged. The briquette dryer comprises a heating facility (15.2) and a briquette storage (15.1) capable of heating by the heating facility (15.2), and the briquette dryer is provided in the briquette storage in the direction of transporting briquettes. , Installed to establish a temperature that rises at at least two or three temperature levels in the range of 60-200 ° C., and / or said briquette dryer comprises at least one roof dryer unit (15a). The furnace device according to any one of claims 1 to 5, wherein this comprises a hot gas circuit for introducing thermal energy into the briquette. The briquette reservoir (15.1) for drying the briquette is a function of a measured value consisting of a group including temperature and moisture content, which is measurable in the briquette reservoir and at least below, in an adjusted manner. It is possible to heat up to a first temperature level of at least 60-105 ° C. and a second temperature level of 105-200 ° C. The furnace device according to claim 6 , which can heat up to a minimum water content of 1 to 5% by mass or less at the outlet. Any of claims 1 to 7, wherein a coke drywall cooling facility (19) having at least one inlet (19.9) and at least one outlet (19.8) for cooling the inert gas is provided downstream of the furnace chamber. The furnace device according to one item. At least one gas outlet (12.6, 12.7, 12.8) for a gas take-up line is arranged at at least three different height positions on the furnace chamber (11), respectively, at the height position. The furnace apparatus according to any one of claims 1 to 8, wherein the furnace apparatus comprises a height position located at least substantially in the center of half the height of the furnace chamber. The first height position is located at a distance of 1 to 3 m from a furnace chamber / the base of the furnace chamber to the second height position, and / or the first height position is the first. The second height position is located at a distance of 3 to 6 m to the height position of 3 and / or the second height position is located at a distance of 1 to 3 m to the third height position and / or the first. The height position of is located at a distance of 0 to 2 m from the base of the furnace chamber, and / or the second height position is located at a distance of 0 to 0.5 m with respect to the center of the furnace chamber. The furnace device according to claim 9 , wherein the furnace device is arranged and / or the third height position is arranged at a distance of 0 to 2 m from the top of the furnace chamber. A method of producing coke from at least one solid feedstock from a group of sub-coal, slightly viscous bituminous coal, biomass, petroleum coke, petroleum coal, wherein the feedstock is provided in the form of briquettes and from claim 1. It is supplied to the furnace apparatus (10) according to any one of 10.
After drying in the briquette dryer (15), the briquette is at least one arranged as a horizontal single plane channel (12.1) in at least one heating wall (12) of the furnace chamber in the lower half. At least one placed in the furnace chamber (11) of each of the horizontal heating channels (12.1) and of the meandering heating channels (12.2) that meander and extend in a number of height planes above it. By indirect heat regulation from the outside in the furnace chamber (11) by individual combustion by one burner (13), it is heated more strongly and continuously according to their traveling rate, and at least one of the horizontal single planes. A method characterized in that gas can be taken up in a vertical waste gas flue through which the channel (12.1) is open. Temperature gradients of different steepness, on the one hand, using the serpentine heating channel and, on the other hand, using at least one horizontal heating channel, exclusively indirectly heat-regulated, after 5-7 hours, 300- At the boundary temperature between the gradients in the range of 350 ° C., the temperature gradient established in the furnace chamber (11) and having different steepness is the first temperature gradient having a gradient in the range of 0.7-1 K / min. 11. The method of claim 11, wherein the second temperature gradient has a gradient in the range of 2.5 to 3.5 K / min. The briquette is dried in a briquette dryer (15) along a presettable first temperature gradient, and the briquette is placed in the furnace chamber (11) along at least one presettable second temperature gradient. Coking into a coke briquette, the second temperature gradient is established by the meandering heating channel (12.2) and, by alternative, by the horizontal heating channel (12.1), said second temperature gradient. The gas is discharged at at least three height positions in the furnace chamber (11), and the at least three height positions are distributed over at least half the height of the furnace chamber. Item 10. The method according to any one of Items 11 to 12. Temperature measurements are made at inversion points (12.21) with observation sites (12.22) in the meandering heating channel, and / or thermal energy adjustments are made at at least one inversion point in the meandering heating channel. At (12.21), at least one temperature measurement is made at the inversion point (12.21), and / or at least one of the heating channels, and / or by an adjustment slide from the outside. Alternatively, the method of any one of claims 11 to 13, wherein the adjustment of at least one thermal energy is performed using a sliding block (12.9). Short circuits or bypasses occur in one or more vertical channels (12.5) of the meandering heating channel by cleaning or shutting off the vertical channels and / or can be actuated from at least one external for adjustment. The method of any one of claims 11-14, wherein the sliding block (12.9) is located in each of one or more vertical channels (12.5) of the meandering heating channel. The briquette is first fed to a briquette dryer (15) in which at least two or three in the range of 60-200 ° C. according to the traveling speed of the briquette and according to a preset temperature curve. The briquettes are continuously dried to a temperature level and then fed to the furnace chamber (11), and the briquettes in the briquette dryer (15) are before the briquettes are fed to the furnace chamber (11). In addition, the briquettes are dried to a water content of less than 5% by mass and / or the briquettes in the briquette dryer (15) are heated on a temperature curve of 0.4 to 2 K / min and / or the furnace. The briquette in the chamber (11) is heated on a temperature curve of 0.5-5 K / min and / or the briquette in the furnace chamber is heated over 4-15 hours and / or the briquette. The method according to any one of claims 11 to 15, wherein the method is heated in the furnace chamber from a starting temperature of 100 to 200 ° C. or 120 to 180 ° C. to a final temperature exceeding 900 ° C. The briquette for the briquette dryer (15) is supplied in a pre-dried form with a moisture content of 10-12% by weight, where the briquette is reduced to less than 5% by weight before being supplied to the furnace chamber. The method according to any one of claims 11 to 16, wherein drying is performed. The feedstock or the fed briquette contains or comprises 45% by weight or more of volatile coal components and lignite having a water content of more than 35% by weight and / or the feedstock or the briquette. The method according to any one of claims 11 to 17, comprising or comprising slightly viscous bituminous coal having a volatile component in the range of 28 to 45% by mass, or 12 to 22% by mass. The method of any one of claims 11-18, wherein the gas is selectively withdrawn / discharged from the furnace chamber at at least three different height positions. The use of the furnace apparatus (10) according to any one of claims 1 to 10, wherein in a vertical furnace having at least one vertical furnace chamber (11), sub-charcoal, slightly viscous bituminous charcoal, biomass, petroleum coke. , The feedstock from the petroleum coal group to coke having the following properties, solid carbon content Cfix greater than 55% by mass, and / or CRI less than 24% by mass, and CSR greater than 65% by mass. To be coked, the feedstock is coked and the feedstock is at least one temperature gradient in a briquette dryer (15) located upstream of the furnace chamber and at least one in the furnace chamber (11). The temperature is regulated in a coordinated manner along at least two temperature gradients including the temperature gradient, and the temperature gradient in the furnace chamber is preferably at least 3 including at least two temperature gradients of the ascending slope in the furnace chamber. Use, established by a meandering heating channel (12.2) along one temperature gradient, and by an alternative horizontal heating channel (12.1). A furnace configuration (50) for generating briquettes, wherein the furnace apparatus (10) according to any one of claims 1 to 10 and a gas discharge configuration (30) are provided, and this gas discharge configuration (30) is provided. ) Is connected to at least one furnace chamber (11) of the furnace apparatus by at least three gas take-up lines (31, 33) at at least three height positions, the furnace configuration (50).

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