JP2020518683A - Devices and methods for gas recovery during coking of carbon-containing feedstocks and uses - Google Patents

Abstract

The present invention relates to a gas emission arrangement (30) for recovering gas during coking of at least one solid feedstock from the group of lignite, finely sintered bituminous coal, biomass, petroleum coke, petroleum coal, gas emission arrangement (30). The assembly is designed to be coupled to at least one vertical furnace chamber (11) of the furnace device (10). The gas exhaust assembly has at least three gas extraction lines (31, 33) that can be arranged at at least three different heights of the furnace and is designed to be connected to the furnace chamber at these at least three heights. To be done. The gas exhaust assembly is designed to selectively handle at least three gas types that are selectively exhausted by each gas extraction line. The invention also relates to a method for recovering a gas using such a gas exhaust assembly, and the use of at least one recovered gas type. [Selection diagram] Fig. 6

Description

The present invention relates to an apparatus and method for utilizing a carbonaceous feedstock, respectively, and also to the associated use of the feedstock or the gas recovered therefrom. More particularly, the present invention relates to an apparatus and method for recovering (by)products utilized in the production of coke from a feedstock, which feedstock is currently not standardly used. It is not possible, or at present, to obtain a satisfactory end product. More particularly, the invention relates to a device and a method according to the preamble of each independent claim. Furthermore, the invention relates to the use of individual components or devices, particularly in connection with these alternative feedstocks.

Currently, coke and carbonaceous/carbon-containing feedstocks are essential basic materials for many national economies on Earth, or represent themselves as valuable materials in their actual form, and will continue to be in the future. Will. Coking has so far mainly been done with highly caking bituminous coals (known as fatty coals). However, some types of coke are likely to run short in the global market very soon. Among other things, the availability of coking coals that are highly suitable for coking will be reduced, and as a result, in the future, especially for blast furnace coke production, less cohesive coals or significant amounts of It must be foreseen that it will probably also be necessary to use swollen coal, or other carbon sources. Due in no small part to political pressure, in particular in areas including Europe, there will be a need in the future for alternatives to traditional bituminous coal, which is especially due to the burning of raw materials as energy sources in the coming years. It is likely that it will remain essential for decades. In Europe, traditional coking coal has been regarded as a key raw material since 2014, but nevertheless continues to be recognized as having the greatest economic importance compared to other key raw materials. .. Overall, it is clear here that on the one hand there is a contradiction and on the other hand the opportunity or motivation to advantageously introduce further optimizing measures starting from the conventional coking process.

While the energy transition is currently only progressing in rich, highly industrialized countries, developing countries have decided to burn traditional raw materials, based on state-of-the-art technology decades and decades ago. I will continue to rely on it for years to come. However, for example, even in highly developed countries such as Australia, and especially Queensland, in order to be able to continue to make advanced refinements of raw materials against the shift to more modern furnace technology, and even in the future. , Have a high level of investment activities. It therefore offers new opportunities for producing or utilizing coke or a certain type of coke with defined properties, or for expanding the range of feedstocks available for coke production. There is great interest and high technical demand for devices and methods. Of course, these measures can also avoid the need for certain raw materials to be transported long distances around the world.

A specific technical problem is to produce high-grade coke from coke raw materials that are slightly caking and non-caking, especially lignite. Wider use of such feedstocks may also be of interest in Europe, but this is especially because these feedstocks can be mined with more acceptable cost scenarios than for example bituminous coal. That's why. The present invention relates, inter alia, to this problem, which has recently become more important than ever, also making it possible to utilize non-conventional feedstocks. Of considerable interest in this context is, for example, also the use of feedstocks having a high sulfur content, which in particular reveals various applications in which exactly this obtained sulfur can be used as a by-product. Because it must be.

In many cases, the conversion of coal to high-grade coke involves pre-compacting the raw material or feedstock in a specific way (referring to the formation of a coal briquette by briquetting/forming the feedstock). It has already become clear that only if it is done, it can be achieved successfully. Briquettes, inter alia, have to withstand high pressures in the hearth floor, which can be several meters high, especially in the case of large vertical furnaces, where as many briquettes as possible can be made into small particles. It is intended to be ground. 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 processes is therefore the question of the form of processing in which the alternative feedstock should ideally be provided, and the way in which its associated processing takes place.

The coke oven for coke production, as mentioned, can take the form called a vertical oven. A vertical furnace is charged with raw material briquettes or briquettes from above. Vertical furnaces can extend to a considerable height, for example in the range of 30-40 m. The briquettes are placed above the furnace, for example using a crane, and slid through the coke shaft (furnace chamber), especially by gravity, over a period of several hours, eg 12 or 15 hours, during which the feedstock is fed. Corresponds to the time required to convert to coke. In this process, the briquettes undergo a temperature change, especially from an initial temperature of less than 300°C to a final temperature of 900-1100°C. A coking oven typically comprises an assembly of 2 to 10 furnace chambers, forming what is referred to as a furnace bank. The shaft of each furnace chamber may have a height of, in particular, 3.5 to 10 m, and a width of, in particular, 150 to 600 mm. From this it is clear that briquettes are subject to high frictional forces and pressure during coking. Therefore, the strength of the briquette is as high as possible. Further, there may be intentionally volume changes and "effective" mass transport within the briquette. Therefore, certain porosities are also advantageous.

To provide briquettes, the raw materials may be milled beforehand, in particular with a hammer mill, and more particularly with a grain size of 0 to 1 mm. Briquettes are then typically formed by pressing by particle compression, and at present it is often advantageous to have briquette shapes in the form of elongated blocks with alternating rounded corners or rounded ends. It turns out. Elliptical briquettes are also commonly produced, especially by rolling.

Water may be added to increase the caking properties of the comminuted raw material (tackiness of the particles during and after compression). However, high water content can have a negative effect on briquette strength shortly after coking, resulting in shreds of briquettes, especially in the lower region of the vertical furnace where maximum force or load is applied to the briquettes. , The coking process is impaired.

In fact, it has been found that difficulties arise during the entire process at various operating steps, especially if the briquette strength is not sufficient, so that the briquettes/coke briquettes are ground in the bed inside the coke shaft. Therefore, in many cases, especially in the case of large/high furnace chambers, a number above 30 MPa will be the lower limit of the briquette compressive strength. Therefore, sufficient compressive strength is one of the most important criteria when estimating the feasibility of coking a feedstock. This process is found to be of great significance because compressive strength can be affected by molding and/or compression.

A further problem arises, in particular, if the specific water content of the raw material or briquettes is not obtained with sufficient accuracy, so that the briquettes are highly stressed during the heat supply, in particular blasting or other forms of collapse. From the above observations it can be seen that efficient operation of the furnace requires providing as many raw materials or briquettes as possible, within narrow tolerances, especially with respect to compressive strength and water content.

Considering these points, the following points should be of particular concern in the search for new methods and devices. The definition of the heating curve in the furnace chamber specific to the feedstock, the process parameters specific to the feedstock, in particular the stream relating to the gases evolved during coking and during the processing of the feedstock into briquettes, in particular during the coking process. Temperature, duration, pressure definitions, utilization and disposal options both during material and type and volume balancing.

Currently, coke making is carried out either in gas furnaces with vertical chambers or in coke ovens with horizontal chambers. The latter are of two types, namely (integrated) horizontal chamber furnaces, with a narrow furnace chamber and an indirectly heated upright charging chamber, and a so-called heat (non-heat) furnace. ) A recovery furnace, which is provided with an arcuate furnace chamber and a horizontally long charging chamber, and can be classified into a heat (non-)recovery furnace that can directly heat at least from above. Current assumptions are that these two types of coke ovens may no longer be able to be optimized as desired for future work in raw material utilization. A new concept seems to have to be developed for a new era of coke ovens, especially in the face of the desire to utilize different types of feedstocks in coke ovens. Therefore, a new furnace concept is presented below, which is particularly adaptable to the use of (coal) feedstocks that have been commonly used to date.

In connection with the object of the invention as defined below below, even non-traditional feedstocks, more particularly lignite and/or slightly caking bituminous coals and/or biomass and/or petroleum coals, especially vertical furnaces It is advantageous to provide an apparatus and method that allows coking in. Non-traditional feedstocks are used so that the product obtained after coking is available as much as possible in the same or similar manner as has been done so far with conventional feedstocks, such as conventional bituminous briquettes. It may be advantageous to prepare, provide, and/or manage.

In this context, it has at least one vertical furnace chamber, in particular a coke oven, for producing coke, in particular from at least one solid feedstock from the group of lignite, slightly caking bituminous coal, biomass, petroleum coke, petroleum coal Providing at least one briquette dryer installed for thermal conditioning of briquettes made from a feedstock, and further below the briquette dryer, among other things, at least one furnace chamber connected to the briquette dryer , And a furnace apparatus having a heating wall, the briquette dryer includes a heating facility and a briquette storage capable of being heated by the heating equipment, and the briquette dryer continuously raises or briquettes in the briquette storage. A furnace arrangement is provided which is installed in stages in the conveying direction of, in particular, to establish an increasing temperature at at least two or three temperature levels in the range of 60 to 200°C.

The furnace apparatus preferably further comprises a loading system comprising at least one locking device, said loading system being located between the briquette reservoir and the (respective) furnace chamber and from the briquette reservoir (respectively). ) It is installed to supply briquettes to the furnace room.

In connection with the feedstocks described herein, it has been found useful to carry out temperature adjustments to various increasing temperature levels in a very reliable manner. In this way, it is possible, among other things, to reduce the water content of the briquette in a gentle manner to the desired value. These preparatory measures have been identified as important for subsequent coking operations. Through controlled briquetting, especially in combination with a controlled temperature regime in the furnace chamber, a particularly wide range of feedstock quality can be achieved. Thus, it would not be impossible for at least some of these feedstocks to be made from logs or materials from the cement industry.

The temperature level may be constant and/or may be a specific temperature level set specifically for different height planes of the reservoir in which the briquettes are conveyed 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 having an elevated temperature. The desired throughput in this case may be established and adjusted, inter alia, by the export system. Compared to batch operation at fixed temperature conditions, for example, coal/coke conversion/upgrade may occur continuously in this case. There may be temperature regimes, operation may be affected, and/or byproducts may be discharged in individual temperature zones.

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

The furnace apparatus may include a feeding unit for providing briquettes to the briquette dryer. The feeding unit may also be installed, for example, to convey the produced briquettes from the press to the briquette dryer. The feeding unit is at least installed to ensure that the briquettes are fed to the dryer continuously or batchwise.

Located upstream of the dryer is a fuel depot from which briquettes can be fed continuously or batchwise and from which the briquettes can be continuously or batchwise discharged to the briquette dryer, especially by sliding the briquettes. ing.

The loading system may be located above the (respective) furnace chamber. This allows the feed to be gravity based.

The furnace apparatus is preferably entirely designed as a vertical furnace with a vertical furnace chamber. A vertical furnace chamber is a furnace chamber through which briquettes are conveyed vertically, especially on a gravity basis.

Feedstocks may include the full range of soft coal, matte and glossy lignite, and long-flame charcoal, among others. Good results have already been achieved above all with lignite from the Rhine, the Russian region and Indonesia. It has also been found that the devices and methods described herein are also suitable for utilization of Russian lignite and long-flame coals, as well as petroleum coals. Feedstocks may include, among other things, the following coal types and peats, based on DIN, ASTM, and UN European Economic Commission (UN-ECE) classifications, which are outlined herein: It was remanufactured to. In the context of the present invention, coals which have been found to be particularly suitable for use with reference to DIN of Germany include soft brown coals, dull brown coals, glossy brown coals and long browns classified under said DIN. Examples include flame charcoal.

The above numbers in the table are mass% with respect to the numbers of volatile constituents and the measurements were made under "waf" conditions, ie anhydrous and simultaneously ashless.

In connection with the object of the invention, which will be defined hereafter, the furnace arrangement described herein has at least one of the furnace chambers in at least one of the heating walls in the lower half, in particular in the lower third. On the side, there is at least one horizontal heating channel, above which, in particular, also at least at the beginning of the upper half or in the middle ⅓, the heating channel extends meandering in various height planes. It is advantageous that each heating channel can be individually heated by at least one burner. This type of heating may provide a number of advantages described herein, among others, independently of any particular configuration or mode of operation of the briquette dryer. Briquette dryers offer advantages, inter alia, for processing briquettes prior to feeding into the furnace chamber. Thereafter, the heating channels act at a later stage of operation on the briquettes in the furnace chamber. As mentioned, both measures relate to a very precisely regulated temperature management system or energy supply to the briquettes. 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 one exemplary embodiment, the briquette reservoir for briquette drying is in a coordinated manner measurable and at least below the temperature, moisture content, in particular 60-105° C., in particular A group comprising a first temperature level of 95°C or less, a second temperature level of 105 to 200°C, and optionally at least one further temperature level comprising a temperature level of 95 to 105°C. It is possible to heat up to at least two different temperature levels as a function of the measurement of, in particular at least two different height positions of the briquette reservoir. The upper limit of the last temperature level may be specifically established so that there is still no devolatilization. The upper limit of each temperature level may be selected from pre-determined temperature values for the particular feedstock and temperature values stored, for example, in data memory, or during operation, especially on/in the briquette dryer. Of at least one pressure sensor and/or gas sensor and/or moisture sensor of This allows the briquettes to be continuously and more strongly dried in a gentle manner without excessive temperature or material stress.

According to an exemplary embodiment, the briquette reservoir as a function of the measured values for adjusted drying of briquettes has a minimum water content at the outlet of the briquette dryer of from 1 to 5% by weight, in particular from 2 to 4% by weight or less. It is possible to heat to the point of value. This makes it possible in a gentle manner for the briquette to have a starting moisture content in the range from 10 to 15% by weight and a moisture value of less than 5% by weight, which moisture value is advantageous for the subsequent coking. In this case, a moisture sensor and/or a temperature sensor may be present in the briquette dryer, especially at the respective height positions. It may be sufficient that the temperature adjustment is carried out exclusively as a function of the water content, subject to sufficient measurement accuracy. Water content can be measured using, for example, volumetric or spectroscopic methods. However, preferably excess measuring equipment is present, especially for pressure, volume and/or temperature measurements. The adjustment is preferably effected, inter alia, via temperature measurement, or even via temperature measurement alone.

Especially for lignite, drying has been found to be particularly useful in the temperature range 60 to 200°C, especially 100 to 200°C. It is known that the drying is preferably performed up to the upper limit temperature, and from this upper limit temperature, each feed material begins to remove volatile components (gas discharge). This upper temperature limit may be preset for each feed, and in the case of adjusting the drying process, such upper temperature limit may be retrieved from the data memory and used as a target value.

With this type of briquette reservoir, it has been found that the drying process is also uniquely adaptable to each feedstock. The above temperature and moisture content may be further limited, eg for lignite or bituminous coal. The feedstocks have different H ₂ O contents and the mass transport process during drying is unique to each feedstock, especially due to the structural differences of the materials (micropore/mesopore/macropore).

As far as lignite is concerned, it has been found that an upper limit of 200° C. may be a good compromise for effective prevention of, for example, H ₂ S volatile removal, although effective drying is possible. Avoidance of H ₂ S devolatilization may be desirable, especially when the recycled flue gas is used for thermal conditioning in a briquette dryer.

The furnace apparatus may have a control facility and a measurement facility coupled thereto installed to control/coordinate the drying or coking of the briquettes. The control equipment here may be installed or specifically intended to control/tune the drying process based on the measured values. The control facility here may also be installed or provided for the sole step of any of the method steps described herein, in each case communicating with the corresponding sensor of the measuring facility.

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

The dryer unit here may be installed for gravity-based continuous transport of briquettes (continuous operation), in which case the briquette reservoir is specially separated from the hot gas circuit and integrated into the dryer unit. .. Other types of drying, such as fluidized bed drying, have proven to be not feasible or at least not a good idea, especially because they cannot pretreat briquettes in the same gentle manner. The dryer unit described herein is capable of effectively adjusting the thermal energy introduced and, in addition, allows for gentle drying in a unit that is inexpensive and robust in construction. The number/density of heating lines may be increased towards the bottom so as to allow the continuous introduction of further thermal energy without the need for particularly complicated adjustments.

The briquette dryer here can also fulfill the role of a shock absorber. Preferably, above the highest/top drying level there is always a plurality of planes of buffered briquettes, inter alia to prevent short circuit flow of drying gas. This multilayer shock absorber of the supplied briquettes is also capable of extracting dry gas under suction with a uniform distribution.

Regarding the shape and arrangement of the individual roofs in one height plane in the briquette dryer, in particular the angle and spacing, and also the height spacing of the drying plane, such that no solid bridges are formed and the gravitational movement of the briquettes It may be performed without interruption. It has been found that a vertical or diagonal spacing of at least six times the briquette diameter can effectively compromise between the temperature profile and the (particularly exclusively gravity driven) transport or movement degrees of freedom of the briquette.

Each drying circuit may carry a blower, and also fresh dry waste gas (from the heat of the briquettes in the coking chamber) and/or an externally generated dry flue from the burner. Gas may be provided, especially to the dryer, so that excess can be assured.

According to one exemplary embodiment, a briquette dryer comprises a dryer unit having a plurality of dryer circuits, each dryer circuit comprising at least two dryer planes. This allows a particularly specific adjustment for each temperature level.

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

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

According to one exemplary embodiment, the briquette dryer or briquette reservoir comprises a height of at least 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, in particular in the case of dry planes in which the individual distances have been set wide 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, an advantageous drying process has been found to be feasible, especially when the briquettes are transported on a gravity basis.

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

According to an exemplary embodiment, the briquette dryer or loading system is connected to at least two, especially 2 to 6 of the furnace chambers. In this way, briquette supply can be easier and cheaper. The loading system can accommodate at least two furnace chambers. In particular, the loading system comprises a distributor for this purpose. The briquettes may be evenly distributed in the individual furnace chambers (especially 4-6 furnace chambers), which is preferably of a distributor adapted to the movement of the gravity driven bulk material, such as by hoppers, pipes, inlets and the like. Supported by shape. Here again, the locking facility prevents the generation of gas. The distribution of briquettes throughout the furnace chamber may preferably be feasible without mechanically displaceable parts (switches), especially by what is called a mandrel. A mandrel located in or on the front or back of the respective locking facility can ensure a uniform and gravity driven distribution of the briquettes. In this context, it is also possible to realize a transverse offset configuration of the lock installation with a loading system having an outlet wider than half the width of the furnace chamber.

A very even distribution of briquettes throughout the respective furnace chambers is also advantageous in that certain operating parameters can be ensured. The operation of the furnace chamber is a delicate interaction between many different agents. For example, if the furnace chamber is not completely filled, the type of heat transfer is not only associated with the extraction of raw gas under suction, but also with respect to the indirect supply of thermal energy to the feedstock. To be done. If the furnace chamber is not completely filled, there can be, inter alia, an increase in the mass-specific heat input.

According to an exemplary embodiment, the (respective) locking facility comprises a double flap system whereby at least two furnace chambers may be connected to a briquette dryer or coke dry cooling facility. A suitable sealant may be ensured between the individual components, in particular at each interface, and the interface may be static, so that conventional sealants, such as gaskets, are also used. It is possible.

In this case, the internal volume of the lock, which is surrounded by the double flap system, may allow evacuation, for example by means of evacuation to further components of the furnace arrangement or pumps which provide gas flow. The shape of each flap or locking slider can be square, among others.

The furnace apparatus may be characterized in that it has a dual locking system below at least two furnace chambers, whereby briquettes/coke briquettes or agglomerates from at least two adjacent furnace chambers are forward, especially in dry cooling installations. It becomes possible to transport it to.

According to an exemplary embodiment, the furnace device further comprises an unloading system comprising at least one locking arrangement, in particular in a gravity driven process, of briquettes or briquettes to be converted into coke briquettes, respectively from the furnace chamber. Alternatively, it will be installed to pick up from the coke dry cooling operation.

The respective locking facility of the loading/unloading system is preferably designed as a structure of refractory material with a slip-promoting property, eg by Teflon coating. The locking installation comprises a slide tilt, for example having an angle (relative to the horizontal) of 5 to 35°. The locking equipment can be driven under motor control and can be operated manually (with a manual switch, pushbutton) or automatically (under time control or coke temperature control). Corresponding motor controls can interact with hydraulic, pneumatic or electric drives, for example.

The unloading system is preferably located below the (respective) furnace chamber or below the coke dry cooling operation. The loading and/or unloading system can be configured as rockers, flaps, levers, taps, sliders or pendulum structures, respectively. Furthermore, the switch or distributor or at least one mandrel may be provided, inter alia, on the base of the briquette dryer or downstream of the furnace chamber, in the form of a triangular shunt so that the briquettes are even and gravity-dependent. It can be driven and distributed within the lock.

According to an exemplary embodiment, the furnace arrangement is downstream of the (respective) furnace chamber and is waterless operable and has at least one inlet and at least one outlet for gas cooling, in particular for inert gas cooling. Equipped with coke dry cooling equipment. Coke dry cooling allows efficient yet gentle cooling. This cooling can take place countercurrently over the bed, so that in particular a continuous temperature profile that can be adjusted as a function of the amount of purge gas used can be established. The coke dry cooling facility may be described as an integral heat exchanger with a continuous temperature profile.

According to one exemplary embodiment, the coke dry cooling installation is for cooling gas flowing countercurrently across the briquette bed, in particular establishing a cooling gas circuit with at least one heat exchanger. The dry cooling facility preferably comprises a heat exchanger installed to generate steam. The cooling gas circuit thus makes it possible to achieve a relatively homogeneous temperature profile or temperature gradient in the briquette bed while simultaneously ensuring high energy efficiency. High energy efficiency is of concern until at least when the economics of the overall operation are at issue. Thus, high energy efficiency also directly impacts potential/feasible measures associated with, for example, briquette drying.

Downstream of the furnace chamber, a coke dry cooling installation may be connected to at least one of the furnace chambers, in particular by means of a discharge system of the furnace equipment. The coke dry cooling equipment may be connected to 1 to 6 furnace chambers.

According to an exemplary embodiment, the coke dry cooling installation comprises or sets up a cooling gas circuit, which comprises in particular at least one heat exchanger. Thereby, the recovered energy can be efficiently used.

According to one exemplary embodiment, in the (respective) furnace chamber, in the conveying direction of the briquettes, there are a plurality of temperature zones having an increasing temperature, the temperature zones at a 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., between which one or two additional temperature zones are respectively provided with the same temperature difference. May be included. As a result, it becomes possible to control heating in the evaporation region to some extent.

The dry cooling installation may comprise a cooling gas circuit with a heat exchanger, said heat exchanger being connected to the water supply line. The heat exchanger may consist of a bundle of tubes and a steam drum, and the heat transfer for the feed water from the cooling gas heated in the dry cooling installation takes place countercurrently, cocurrently or in crossflow. obtain.

The facility for dry cooling may be provided with multiple cooling gas inlets and cooling gas outlets by means of which the flow profile in the cross-flow briquette bed adjusts the supplied or removed volumetric flow, respectively. Can be established.

According to an exemplary embodiment, a plurality of horizontal heating channels are configured on at least one side of the (respective) furnace chamber in at least one of the heating walls, preferably at least one vertical waste channel. Connected to the gas flue, the burners, in particular at least three horizontal heating channels, can each be heated 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 does not or does not stretch significantly in the vertical direction. In contrast to serpentine heating channels, horizontal heating channels extend to a substantially single elevation or horizontal plane.

Regeneration preheating of the gas generated externally in the generator was retroactively realized in the 1960s, and the flow direction was reversed every 10 to 30 minutes, allowing cold gas to flow to the checker brick that had been heated in advance. As a result, I was able to heat up. This type of heating channel management within the walls flanking the furnace chamber may be referred to as a "checker brick regenerator". By virtue of the arrangement described here, in contrast, heating can be carried out individually in different height planes without inversion. Each heating channel may be individually supplied with thermal energy.

This antiquated structure or configuration of heating channels has proven to be quite inflexible and can be optimized at most for only one feedstock/coal (soft brown coal from the Lusatian region). This structure is not able to respond accurately to different coals/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, especially based on heat transfer in silica bricks.

"Indirect" heat transfer ensures that there is no contact between the heating wall and the briquette, especially between them by providing a temperature sensitive and high temperature resistant silica material separation layer. To It is possible to prevent unwanted product contamination of briquettes.

The horizontal heating channels capable of burning individually may set a devolatilization chamber or devolatilization zone, where the devolatilization can be substantially performed in the lower part of the furnace chamber. , Give the briquettes, which have been considerably dried beforehand, a relatively high temperature stress and/or a relatively high energy supply. This too can prevent coking of the purge gas, especially in the upper region of the furnace chamber, and the briquettes remain particularly susceptible to thermal stress.

Each of the horizontal heating channels (in particular independently of one another) may lead to a vertical exhaust gas flue, in which the gas can be withdrawn.

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

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

The recovery system makes it possible to process the raw gas and to use the processed gas further, in particular as fuel for heating.

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

According to an exemplary embodiment, at least one of the plurality of horizontal heating channels is arranged external to the furnace chamber and comprises a flame monitor, and in more detail by said 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, a temperature of at least 1000° C. is feasible on each heating channel. With multiple horizontal heating channels, a very hot devolatilization zone can be established in a targeted manner in the lower region of the furnace chamber.

Burners with flame monitoring, especially burners operated using natural gas, offer the advantage of high flexibility and accuracy for heat regulation (heat input). In contrast, in the past, gas generation was done in a separate gas generator located in front of the furnace chamber and a corresponding conduit feeding the furnace chamber. In these gas generators, heated gas was generated by the combustion of coal, which damages the environment.

According to an exemplary embodiment, the horizontal heating channels arranged above one another and in contact with one another can be heated by burners arranged opposite one another. This allows relatively uniform heat input to the overall volume of the furnace chamber.

Horizontal heating channels which are vertically adjacent to each other preferably lead to vertical exhaust gas flues at their opposite ends. This offset configuration of the burner allows a particularly homogeneous heat input.

According to an exemplary embodiment, the heating channels arranged at the same height and opposite each other can be heated by burners arranged opposite each other. This allows relatively uniform heat input to the overall volume of the furnace chamber.

The burners can be placed diagonally opposite each other and at the same height in the furnace chamber. At the height of the furnace chambers which are in contact with each other, the burners can be arranged at one opposite edge/corner on the side of the furnace chamber. This allows bi-rotational asymmetry to be created, ie within each height plane and for adjacent height planes.

According to an exemplary embodiment, on at least one side of the (respective) furnace chamber, there are heating channels that meander and extend in a plurality of height planes, which have at least two or three horizontal heating channels. It may be located higher and heated by at least one burner. This makes it possible to easily establish a temperature profile that goes down in the height direction.

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

According to an exemplary embodiment, on at least one side of the furnace chamber, there is a meandering heating channel with at least one inversion, on which at least one of the inversions an observation or measurement point is located. And, more specifically, the observation point is a closed observation point operable from the outside. This provides numerous options in monitoring and establishing operating parameters within the furnace chamber, especially temperature profiles.

According to an exemplary embodiment, the observation point is located in at least one of the heating channels. The point of view allows this optical control or otherwise other visual insight. This provides options in monitoring and establishing operating parameters.

According to one exemplary embodiment, a plurality of horizontal heating channels are provided in the lateral heating walls of the furnace chamber, in particular in the opposite heating walls, each fourth heating channel from the bottom being meandering in a plurality of loops. The fourth horizontal heating channel in the lower region of the furnace chamber is connected with at least one burner, and the upper region of the furnace chamber is connected with the line equipment leading to the briquette dryer. This makes it possible to easily establish an upwardly decreasing temperature gradient.

According to one exemplary embodiment, on at least one side of the (respective) furnace chamber, there is a serpentine heating channel with at least one inversion, in at least one of which the observation point is Arranged, and more particularly, the observation point is a closed observation point operable from the outside. As a result, the target influence can be further exerted on the temperature control system in the furnace chamber. There may be temperature detection and temperature monitoring, among others. Multiple observation points may be provided at multiple elevation positions to detect, not less than, the temperature gradient. At the observation point, the condition of the attached block can be inspected from the outside. The surface temperature of the block can also be measured and provides information, eg about radiant heat generated.

According to one embodiment, there is at least one observation point located in at least one of the heating channels. There, it is possible to operate the adjusting slider for the sliding block and/or to see if the material of the furnace chamber wall remains intact. There, too, one or more sensors can be attached. It is accessible via the skeleton from the respective observation point, eg from the outside.

According to one exemplary embodiment, a plurality of horizontal heating channels are provided in the lateral heating walls of the furnace chamber, in particular in the opposite heating walls, each fourth heating channel from the bottom being meandering in a plurality of loops. And at least one burner is connected on the fourth horizontal heating channel in the lower region of the furnace chamber and a line arrangement is connected in the upper region of the furnace chamber leading to the briquette dryer. This makes it possible to establish a temperature profile that drops homogeneously upwards over a large height.

This configuration of the heating channel makes it possible to establish the temperature profile in the furnace chamber with relative accuracy. In the lower region of the furnace chamber, very high temperatures can be flexibly achieved, especially for the desired level of volatile constituents in the briquette of less than 1% by weight and for terminating the coking process.

The number of three individually heatable horizontal channels has proved to be advantageous on the one hand for a high degree of individual heating 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 kind of heat input can be effected over a relatively short distance (in the vertical conveying direction of the briquettes) by the realization of furnace chamber temperatures well above 1000°C. It has been found that this heat input is ensured in the lower region of the respective furnace chamber (on the substrate) in a particularly useful manner by means of a large number of burners and a large number of individual heating channels. This configuration also allows a flexible response to the required final temperature on an individual basis depending on the feed/coal type. From our own investigation, the combination of three horizontal heating channels and one serpentine heating channel is particularly high in terms of the achievable and very homogeneous temperature profile and the structural cost and complexity. Provide benefits.

A serpentine heating channel refers to a channel that extends across a plurality of height planes, the height planes being connected together by a channel profile in the form of loops or serpentine curves. The channels may in this case continuously rise in height. At the reversal point of the channel, the angle will notably be below 90°. The serpentine heating channel can provide some type of helical 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 residuals in the coal or coke, especially in the middle of the furnace chamber. Useless coke zones with a high fraction of volatiles and low temperatures below 950°C were formed.

According to an exemplary embodiment, on at least one side of the furnace chamber in at least one of the heating walls in the lower half, in particular in the lower 1/3, at least 3 horizontal heating channels and above it, in particular Also at least in the upper half, or in the beginning of the middle 1/3, there is a meandering heating channel, each said heating channel being individually heatable by at least one burner, the meandering heating channel preferably being provided with a sensor Alternatively, it comprises a reversal point with an observation point for performing the measurement. This allows many of the above advantages to be combined. Vertical channels are preferably formed on the serpentine heating channels.

According to one exemplary embodiment, the serpentine heating channel comprises a reversal point with an observation site, which has a sensor arranged thereon, or carries out the measurement there, the sensor notably at a temperature. It is a sensor.

According to an exemplary embodiment, the serpentine heating channel comprises at least one inversion point, in which a closed observation site is arranged, which is in particular operable from the outside by means of an adjusting slide.

According to an exemplary embodiment, at least one of the heating channels, in particular at the reversal point, has an adjusting slide (open position, closed position, intermediate position) for the sliding block and/or a measuring sensor system. At least one observation site is arranged.

According to an exemplary embodiment, a manually accessible access tube for the adjusting slide is connected to at least one of the heating channels, in particular the meandering heating channel.

According to one exemplary embodiment, the serpentine heating channel comprises one or more vertical channels. At least one adjusting element, in particular an externally actuable sliding block, is arranged in each flow path.

According to an exemplary embodiment, the serpentine heating channels are installed in one or more horizontal or vertical positions, in particular short circuited/short circuited by eliminating or blocking vertical flow paths. It

According to an exemplary embodiment, at least three different height positions on the (respective) furnace chamber are respectively arranged at least one gas outlet for the gas take-up line, the height position being notably the furnace There is a height position located at least approximately centrally at half the height of the chamber. This allows the gas propagation into the furnace chamber and the temperature distribution to be influenced relatively easily and very effectively. In addition to a more homogeneous temperature distribution (avoiding coking of the purge gas), it has been found that valuable gas can also be withdrawn, especially for recycling in the central position. If the feedstock contains lignite, it can be discharged hydrogen H ₂ Especially at this point. Apart from the reusability of hydrogen (eg methanol synthesis), the controlled extraction of hydrogen by suction makes it possible to optimize the temperature distribution very effectively. Hydrogen has high thermal conductivity.

The (respective) furnace chamber may be provided with at least three gas outlets arranged at at least three different height positions of the furnace chamber, by means of which at least three gas outlets capable of being discharged from the furnace chamber are provided. Gases/gas types (first gas and at least one additional gas) can be provided.

According to an exemplary embodiment, the (respective) furnace chamber comprises a plurality of gas outlets, which can be arranged in a circulating manner at a plurality of sites at at least one of the height positions. This allows the gas to be withdrawn with very little mass transport in the vertical or horizontal (or radial) direction. As a result, the coking process can be made more harmless and more selective.

According to an exemplary embodiment, the gas outlet extends to a height corresponding 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 drawn off with very little mass transport in the vertical direction. This also allows the emission of different gases over a wide range.

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

According to an exemplary embodiment, the first height position is arranged at a distance of 1 to 3 m, in particular 1.5 to 2.5 m from the second height position when viewed from the base of the furnace chamber. It This allows for selective evacuation in the main degassing zone, especially in the horizontally heated channel areas that are burned individually.

According to an exemplary embodiment, the first height position is arranged at a distance of 3-6 m, in particular 4-5 m, from the third height position. According to an exemplary embodiment, the second height position is arranged at a distance of 1-3 m, in particular 1.5-2.5 m, from the third height position. This respective distance is often very suitable in preventing coking of the purge gas or unwanted temperature deviations. In practice the distance may be shorter, especially if there are more than three height positions, but this distance allows for a balance between facility/process processing costs and complexity and the simplicity of the facility's structure. It turns out that it provides a valid compromise.

According to an exemplary embodiment, the first height position is arranged at a distance of 0-2 m, in particular 1 m from the base of the furnace chamber, and/or the second height position is in the middle of the furnace chamber. Is located at a distance of 0 to 0.5 m and/or the third height position is located at a distance of 0 to 2 m, in particular 1 m from the top of the furnace chamber. This distribution offers the advantage that the respective furnace chambers can be fully taken into account in the process processing conditions and virtually completely taken into account for relatively small numerical height positions.

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

According to an exemplary embodiment, the respective height positions are arranged at a distance from each other of at least 20-25% of the total height of the furnace chamber. This can cover the high altitude range.

According to one exemplary embodiment, one of the height positions is provided at the upper end of the top of the furnace chamber, and the top gas generated in the upper region of the furnace chamber is supplied by the corresponding gas outlet to the furnace chamber. Can be discharged from. This makes it possible to establish the temperature profile as accurately as possible, especially in regions of the furnace chamber that are more sensitive to lower temperatures. Here, the topmost height position need not correspond to the top end of the furnace chamber, but may instead be located at a slightly lower position, eg, according to feedstock and process controls.

According to an exemplary embodiment, the feedstock or briquette that can be fed to the briquette dryer has a volatile carbon content of 45% by weight or greater, and a water content of 40% by weight, or greater than 45% by weight, and/or It contains or consists of a slightly caking bituminous coal having a volatile component in the range of 28 to 45% by mass, or 12 to 22% by mass. Feedstocks of this kind make it possible to obtain briquettes which are upgraded to a particularly high quality.

According to an exemplary embodiment, the furnace arrangement is configured as a vertical furnace, where the briquette dryer is located above the (respective) furnace chamber. In this way, the briquette supply can be promoted. Among other things, the overall material flow can be regulated using a delivery system. In this case, the temperature profile in the briquette dryer is set to the temperature profile in the furnace chamber such that once the desired material flow (quantity of briquettes/hour) in the furnace chamber is established, the desired temperature profile in the briquette dryer is also established. May be combined with. For this purpose, it is advantageous if the briquette dryer comprises or can be set with at least four drying or temperature planes. This allows a response that is particularly sensitive to changes in the material flow.

According to one exemplary embodiment, the coke dry cooling equipment is located below the (respective) furnace chamber. This makes it possible to continue the transportation method based on gravity. Due to the compact overall arrangement, the material flow is easily adjustable.

According to an exemplary embodiment, the furnace device comprises a measuring facility and is further coupled to it to control the drying of briquettes in the temperature range of 60-200° C. and/or in the moisture range of 1-5% by weight. Equipped with control equipment installed for adjusting and/or where the furnace device comprises measuring equipment and is further connected to it, in particular by throughput system or briquette material by means of an unloading system connected to the control equipment. With control equipment installed to request flow. The same control facility makes it possible to adjust both the temperature regime and the material flow during drying and coking, in particular as a function of each other.

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

The bulk density of the furnace chamber of the briquette, based on the density of 1350 kg / ^{m 3} for each briquette may range from 650~850kg / ^{m 3.}

In this context, in particular a process for producing coke from at least one solid feedstock from the group of lignite, lightly bituminous coal, biomass, petroleum coke, petroleum coal, the feedstock being provided in the form of briquettes, and Especially fed to the vertical furnace chamber of the coke oven, in particular to the furnace equipment described above, the briquettes are first fed to the briquette dryer, in which the briquette's speed of advance is followed according to a preset temperature curve. There is also provided a method of continuous drying, in particular drying to at least two or three temperature levels in the range 60 to 200° C., and then feeding to the furnace chamber. This allows the briquettes to be pre-dried and pre-processed and at the same time gently processed so that they may be requested with great precision. Here, the briquettes in the furnace chamber may be continuously heat-controlled to a wider range according to the traveling speed of the briquettes. By gradually increasing the energy supply along the route, an efficient method becomes possible. The energy supply can be increased especially as a function of the residual water content, for example by supplying individual heating levels with hot gas which is disproportionate to the temperature gradient between the previous heating levels.

Coking of lignite, slightly caking bituminous coal, or biomass is an operation that should be controlled very accurately, especially so that softening (and collapse) of briquettes can be avoided. Coking in the temperature range called the "plastic zone" (for certain lignites, especially about 350-410°C), where the feedstock softens should be avoided. This can be done by establishing temperature regimes and/or heating curves.

For many feedstocks, the major volatile component removal is done in the "plastic zone". Therefore, it is within the "plastic zone" that the structural composition of the briquette comes closest to the risk of modification. The methods and apparatus described herein allow a "plastic zone" to be specifically assigned to a height position within the furnace chamber, particularly the height of the serpentine heating channel. This makes it possible to monitor the operation and/or adjust it to particularly good results and to coke the feedstock particularly gently.

Outgassing is also targeted in the area of the "plastic zone", especially in combination with preset temperature control systems in the furnace chamber and/or in combination with preset indirect heating via individually operable heating channels. It turns out that you can do it in a specific way. For example, at least one height position of the gas withdrawal line, more particularly the second height position (detailed below), may be in the region of the "plastic zone", especially in the center of this region or Clearly placed at the top of this area. After that, at least one gas extraction line is connected to the furnace chamber at a height corresponding to the "plastic zone". This allows any convective heating by rising raw gas to be effectively offset.

From experience, it is recommended to resolidify the feedstock at temperatures above about 470-500°C, after which. Briquettes made from lignite briquettes and slightly cindered bituminous coal, among others, appear to be less able to withstand coking while passing through the "plastic zone". 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. Predrying in a briquette dryer can be interpreted in this respect as a preliminary step. Disproportionately high drainage over short periods of time, even in the temperature range below 350° C., can lead to briquette rupture as a result of water outflow and gas fractions.

Thus, the temperature profile can be established not only by extraction of the exhaust gas by suction at various height positions, but also by control/regulation of the energy supplied by the external burner. In particular, also in meandering heating channels, measures can be taken such as eliminating or blocking vertical channels, for example so that the energy input can also be established in the "plastic zone".

In connection with the method described herein, the briquettes after drying in a briquette dryer have a lower half, in particular a lower 1/3, and above that, in particular also at least an upper half, or the middle 1/3 of the beginning. In the at least one heating wall of the furnace chamber in a section, their progress by indirect heat regulation from outside in the furnace chamber by individual combustion of at least one horizontal heating channel, respectively by at least one burner, A method is also provided in which the heating is more intense according to the rate. It has been found that this configuration of the heating wall makes it possible to establish the desired temperature profile in the furnace chamber in a relatively accurate and homogeneous manner, even with indirect heat regulation from the outside. The continuous connection of the individual horizontal sections to form the serpentine heating channel allows the controlled cooling of the flue gas with a controlled decrease in heat flow density over the height of the heating wall, with continuous heat transfer. .. The heat transferred indirectly through the heating channels can be supplied to individually match the load. In particular, at least one stage of the coking operation has a gradient of elevated temperature in the briquette such that residual vaporizing water and further volatiles depletion are removed from the briquette at only moderate pressures. It can be adjusted appropriately. At least one subsequent step, especially when the devolatilization rate is slowed down, the temperature or indirect supply of thermal energy (as a function of height position) is particularly required to complete the devolatilization to a desired degree. , Increase more gently. Thanks to at least the first steps taken in advance, the risk of weakening the briquette agglomeration structure is no longer present. The conditions of how the rate of increase rate and the steepness of each temperature gradient can be chosen and how many intervals of different temperature gradients are established, preferably along the height of the furnace chamber, are Flexible as a function of the selected feedstock and temperature range, among other things, is adjustable by the device described herein.

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

According to an exemplary embodiment, the heating of the briquettes in the briquette dryer takes place with a temperature curve of 0.4-2 K/min, in particular 0.8 K/min. This allows very gentle drying. Thermal energy is preferably introduced in two or more stages (hot at the bottom and less 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.

A temperature increase of 0.8 K/min has been found to be very advantageous, especially for lignite briquettes. Particularly advantages arise when the operation is carried out in this case in the temperature range from 60 to 200° C., in particular from 100 to 200° C. Furthermore, it has been found to be very advantageous for the quality of briquettes obtained if this temperature gradient is established in the furnace chamber and more particularly in the upper half or the upper 2/3. It has been found that this can be achieved by meandering heating channels, especially in combination with outgassing, especially at multiple elevations.

According to one exemplary embodiment, the briquettes are dried in a briquette dryer to a water content of less than 5 wt% before the briquettes are fed into the furnace chamber. As a result, the briquettes can be treated particularly gently. By a preliminary step prior to the briquette dryer, the feedstock is first heated and dried to 20 wt% moisture, then before the briquettes are fed to the briquette dryer, and especially when the briquettes are less than 5 wt%. It has been found that the feedstock formed to form briquettes is heated and dried to 11 wt% moisture before being fed to the furnace chamber at a water content of.

According to one exemplary embodiment, the briquettes are dried in a briquette dryer to a water content of 1 to 5% by weight, in particular 3% by weight, at the same time or as a result of 120 to 180° C., in particular 150° C. Allow to temperature. This may ensure a particularly gentle treatment of the briquettes.

According to an exemplary embodiment, the heating of the briquettes in the furnace chamber is carried out by a temperature curve of 0.5-5 K/min, in particular 2-3 K/min, especially with respect to the conveying direction of the briquettes or with respect to the vertical direction. Sub-minute temperature curve and/or the briquettes are heated in the upper furnace chamber for 4 to 15 hours, in particular 6 to 9 hours, and/or the briquettes are especially oriented with respect to the conveying direction of the briquettes or perpendicular to it. On the other hand, it is heated in the furnace chamber from a starting temperature of 100-200°C, or 120-180°C, especially 150°C, to a final temperature of more than 900°C, especially 900-1100°C. These temperature conditions provide an efficient method that involves gentle treatment of briquettes.

A continuous process in a vertical furnace (continuous process) 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 rate.

It has been found that a coking process can also be used to further increase the (coke) compressive strength while having a targeted effect on the temperature profile in the furnace chamber. In particular, the compressive strength can be increased, for example, from 20 to 25 MPa by 30% to 50% to at least 35 MPa to 45 MPa. With the furnace arrangement described above, it is possible to influence the temperature profile in the furnace chamber in a targeted manner in a sufficiently precise manner, in particular also by virtue of the outgassing at a plurality of height positions.

According to one embodiment, the heating of the briquettes is carried out in a plurality of stages, depending on the water content, in particular a first stage with a water content of 15-10% by weight or less, in particular 11% by weight and a water content of 1-5% by weight. Or 2 to 4% by weight, especially 3% by weight in the second stage and in a second stage in a briquette dryer. This allows a particularly gentle drying.

According to one embodiment, the heating of the briquettes is carried out in the briquette dryer on drying planes at different height positions, each to a individually adjusted presettable temperature level, in particular one or more. Of the individually adjustable dry gas circuit. This makes it possible to have a targeted influence on the energy supply during drying, especially in a manner specific to each feedstock. The adjustment can be accomplished by volume flow, inter alia, for example by means of sliders or flow control valves.

It is also possible to subject the feedstock to predrying, in particular from 20% to 11% by weight water, before shaping. The heating of the feedstock can be carried out in several stages depending on the water content, in particular in two stages, a first stage to 20% by weight moisture and a second stage to 11% by weight moisture.

According to one embodiment, the shaped body is heated to 950 to 1100°C, in particular 1000 to 1050°C or less, preferably 1050°C or less, during the coking operation. In both coke strength and particle size, undesired reductions can occur at final temperatures above 1100°C, or even above 1050°C, depending on the feedstock, and the use of coke in the blast furnace I know I can be in jeopardy.

According to the present method, when these temperature ranges are observed, high strength briquettes can be provided from a feedstock that can be considered a replacement for existing blast furnace coke.

According to one embodiment, the heating of the shaped body during the coking operation is such that the shaped body shrinks by 40% to 60%, in particular 50% by volume, during the coking operation and/or during the coking operation. The molded product is reduced by 40% to 60%, especially 50% in terms of mass. It has been found that volume changes within this range are still tolerable in obtaining high strength values and good combustion properties in a portion of the coke briquette.

According to one embodiment, the shaped body is dried in a briquette dryer to a water content of 1 to 5% by weight, in particular 3% by weight, and at the same time or as a result, a temperature of 120 to 180° C., in particular 150° C. Let This allows a good balance between gentle and efficient/effective drying.

According to one embodiment, the briquettes of at least two adjacent coking chambers are transferred to the dry cooling installation via the discharge system or the component itself, in particular by means of a double lock, where the cooling gas, In particular, it is cooled to a temperature below 200° C. with nitrogen. First, it provides an efficient method, and secondly, it also makes it possible to recover energy immediately after coking, whether upstream of the operating step or for another facility/process. The formation of condensate can be avoided by keeping the entire installation at a controlled temperature above the dew point, although cooling is actually 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 dry cooling facility.

According to one embodiment, thermal energy is removed from the heated cooling gas (especially nitrogen) as a result of dry cooling on the briquette bed, especially in the heat exchanger. As a result, a configuration with high energy efficiency is possible even in the circulation of the cooling gas. The cooling gas can then be used, inter alia, to produce steam. In the case of steam generation, steam can be utilized to generate an electric current (expansion in a steam turbine). The electric current can then be used for the operation of electric consumers such as pumps, compressors, blowers, locks, valves, etc. All excess current can be sent to the local supply grid. A further potential utilization of steam is, for example, as associated heating for raw gas preparation on the blank side of the furnace installation. Steam can be further utilized as a reactant in chemical processes, one example being methanol synthesis (keywords: steam reforming/steam reforming, syngas, H20 (shift reaction) to boost hydrogen yield, primary reforming furnace). Is.

According to one embodiment, coke, in particular lignite coke, having a fixed carbon content Cfix of greater than 55% by weight is produced. This provides advantageous physical properties for many subsequent applications. Among other things, the briquettes produced can be utilized in a DRI (direct reduced iron) process.

According to one embodiment, coke is produced, especially lignite coke having a very low coke reactivity index (CRI) of less than 24 wt% and a very high post-reaction strength index or post-reaction strength (CSR) of greater than 65 wt %. To be done. With these values, widespread applicability of high-grade coke is expected. Especially when the briquettes produced are available for blast furnace processes.

CRI is determined by heating the feedstock to 1100° C., among others, under preset conditions, and determining mass loss through outgassing. The CSR can be determined, inter alia, by spinning the outgassed material sample in a drum under preset conditions and is also quantified as a mass loss value.

According to one embodiment, coke is passed downstream of the furnace chamber with a countercurrent, reactive inert cooling gas, in particular nitrogen, through a briquette bed formed in the dry cooling facility and from the dry cooling facility to the furnace. It is cooled to a temperature of less than 200° C. by discharging the gas by the discharge system of the device. This allows for a method that is relatively simple to control/adjust and that can also recover energy efficiently.

The dry refrigeration facility can be operated in circulation, in which case the cooling gas accumulates combustible constituents, such as H ₂ and CO, due to further degassing events in the coke bed. To prevent further accumulation of H ₂ /CO above a certain content, and thus avoid conditions presenting safety concerns, the cooling gas can be discharged from the bed and purified. Among other things, atmospheric oxygen is added to the stored cooling gas before the thermal energy stored in the cooling gas transfers to supply water to the heat exchanger to burn the combustible components.

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

According to one embodiment, the (respective) furnace chambers are operated in a continuous manner and the briquettes are continuously conveyed into the furnace chambers (especially downwards), in particular locking equipment for at least two furnace chambers (duplex). It is fed and discharged in batches via the lock). The bed can be moved continuously in the furnace chamber, and can be moved in and out in particular in batches 2 to 4× because the loading and unloading can be done in batches. The residence time on the floor in the furnace chamber can be adjusted by the delivery speed. It is also possible here to take into account the fact that the mass flow and the volume flow of the briquettes change during the coking operation, inter alia due to degassing and contraction. The loading or unloading can thus be set at a higher mass flow rate than the unloading.

According to one embodiment, the briquettes are fed vertically into and/or withdrawn from the furnace chamber via gravity. This provides various advantages, not least in terms of self-adjusting transport and positioning of briquettes within the device.

According to one embodiment, the feedstock or supplied briquette comprises 45 wt% (waf) or more volatile carbon components and lignite having a water content of 35 wt% or 40 wt% or greater than 45 wt%. , Or consist of this. According to one embodiment, the feedstock or briquette comprises or consists of a slightly caking bituminous coal having a volatile carbon content in the range of 28-45 wt% (waf) or 12-22 wt% (waf). Due to this respective composition, the above advantages can be achieved.

According to one embodiment, the feedstock material flow through the (respective) furnace chamber is controlled or regulated by a unloading system located below the (respective) furnace chamber and, in particular, exclusively gravity-based gravity drive. It This makes it possible to easily control/adjust the material flow in the furnace chamber, ie (if desired) only via the unloading system. Each of the influences on the material flow is of great advantage here, but it allows the use of additional (optional) variables in order to be able to influence on the temperature profile and/or the energy input. It will be.

According to one embodiment, gas is drawn/exhausted from the furnace chamber at at least three different elevations. This makes it possible to more effectively establish or confirm the desired temperature profile.

The raw gas mixture of the outflowing gas components produced in the floor in the furnace chamber and flowing upwards has a high energy content (high temperature) in the undesired secondary coking of upstream briquettes (purge gas or raw gas coking). ) (Undesired accelerated convective heat transfer to the upper briquette) at present, with typical results. 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 created by the sidewalls by the targeted burner control. It has been found that by discharging raw gas at different vertical height positions, this result can be reduced or completely prevented, especially in at least three height positions, including one height position at the top of the furnace chamber.

The height positions located in the middle and lower areas of the furnace chamber very efficiently prevent high raw gas temperatures in the upper area of the furnace chamber. Especially hot gases in the lower region can be withdrawn before rising in the furnace chamber. The heat transfer in the vertical direction can be prevented. Among other things, hydrogen is discharged in a targeted manner, especially at the elevations where the feedstock produces hydrogen. Here, the energy supply may, in terms of technical regulation, be connected via a burner, in particular with respect to the volume flow to be discharged, to a suction withdrawal or exhaust system.

In this context, the use of feedstock from the group of lignite, slightly cindered bituminous coal, biomass, petroleum coke, petroleum coal, in a vertical furnace with at least one vertical furnace chamber, the following properties, 55% by weight: For use in coking feedstocks to coke having a solid carbon content of Cfix of greater than and/or a CRI of less than 24% by weight and a CSR of greater than 65% by weight, particularly in the above apparatus or in the above method. And the feedstock is preferably along the direction of travel along at least two temperature gradients including at least one temperature gradient in the briquette dryer located upstream of the furnace chamber and at least one temperature gradient in the furnace chamber. It is also advantageous to use the heat-regulated in a coordinated manner along at least three temperature gradients, including at least two temperature gradients of the rising gradient in the furnace chamber of These values are achievable thanks to the inherent heat regulation described herein, and especially for all bituminous coke, and also for the lignite coke, a relatively high Cfix of more than 55% by weight. I know it is achievable.

The object of the present invention is an apparatus and a method having the described characteristics from the beginning, whereby coking of non-conventional feedstocks, in particular lignite and/or slightly caking bituminous coal or biomass. Even so, it is to provide a method by which coking is possible, especially in vertical furnaces, with operating parameters that can be established with great accuracy. The objective is also to be non-conventional so that the overall operation can be adjusted very precisely in terms of energy, otherwise optimized and the energy or by-products of the operation can be used sustainably. Can be viewed as processing, providing, and/or handling the feedstock. It is contemplated here that the product obtained after coking is made available in the same or similar manner as possible with the current state of the art feedstocks, for example conventional bituminous briquettes.

According to the present invention, the above object is to provide at least one vertical feedstock during the coking of at least one solid feedstock from the group of lignite, slightly caking bituminous coal, biomass, petroleum coke, petroleum coal to obtain coke. A gas discharge arrangement for recovering available gas from a furnace apparatus having a furnace chamber, the gas discharge arrangement being set to connect to at least one of the vertical furnace chambers of the furnace apparatus, The exhaust arrangement may be arranged in at least three different height positions of each furnace chamber, and at least three gas draw lines installed for connecting to the (respective) furnace chamber at at least three height positions. A gas exhaust arrangement is provided for selectively handling at least three types of gas (first gas and at least one additional gas) selectively exhausted by the respective gas withdrawal line. Achieved by the discharge configuration. This allows, on the one hand, the utilization of the by-products obtained in the coking and, on the other hand, the precise temperature control/regulation and the control of the reaction taking place in the furnace chamber by avoiding the propagation of (purge) gases, especially in the vertical direction. It will be possible. Selective handling can also be accomplished by pumps, valves, and mixers in a gas evacuation configuration that is/can be connected to a gas draw line.

The gaseous substances can be withdrawn in a temperature-dependent manner in order to render the liquid and gaseous substances of high quality and, in particular, available from an environmental and/or economic point of view. The emission of gas emissions in the case of coal is carried out at different temperature levels, in a very defined manner, depending on the degree of coal coalification, and that the furnace chamber is maximally accurate and homogeneous at certain temperature levels. It has been found that this effect can be exploited if it can be heat regulated/managed. Not only the arrangement of the heating channels, but also the arrangement of the gas withdrawal flue/gas outlet has an effect here in terms of adjustability.

Thereby, for example, hydrogen can be collected. Methanol can be recovered. The gas emission mix thus contributes to a very efficient overall operation, including comprehensive, sustainable feedstock utilization, and especially coking. This also allows the briquettes in the upper region of the furnace chamber to be protected from the hot gases from the lower region. The briquettes can be guided more accurately along the desired temperature curve. Thermal stress is reduced. Coke of purge gas can be avoided. Furthermore, the condensation of tar vapors, which occurs for example in briquettes at different heights, is also 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 gases need not be selective, but the gases can be further processed or utilized individually. This option allows a flexible response, possibly to available developmental byproducts, according to the particular application.

The gas evacuation configurations can be further set individually at their respective height positions, in particular at a particular reduced pressure, for selectively adjusting the operating parameters. As a result, by-product emission and/or evolved gas flow paths within the furnace chamber can be adjusted in an even more targeted manner, even with a relatively small number of height positions (eg, only three). it can.

It has been found that there may be complementary effects between heating through the burner and suction removal of raw gas. Because of the degassing of individual gases over the height of the furnace chamber, the raw gas composition varies. As a result, the heat transfer coefficient also varies. By means of the method and the corresponding device, a direct heat exchanger (suction off) and an indirect heat exchanger (indirect heating of the furnace chamber via heating channels) can be thermotechnically linked to one another. The entire height of the suction extraction site (takeover) can influence the heat transfer and temperature profile in the furnace chamber.

Selective handling may also include the use of the exhaustable gas as a fuel/combustion gas, eg, for a burner of a furnace system, as well as methods of operating the furnace system 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 an exemplary embodiment, the gas evacuation arrangement comprises a plurality of gas withdrawal lines, which can be arranged in a particularly circular manner at at least one of the height positions and at a plurality of sites. This also makes it possible to establish and/or control the flow path of the evolved gas in the radial direction. Connections to the gas withdrawal line can be provided especially at the distribution in the periphery and between two circulation positions/sites, for example 6 or 8 circulation positions/sites.

According to the invention, the gas discharge arrangement extends over a height corresponding to at least half the height of the furnace chamber, in particular over at least 75% of the height of the furnace chamber. This makes it possible to prevent the generated gas from causing a secondary reaction or a modified temperature profile over a wide height range. For example, the outgassing arrangement extends over a height of at least 2-3 m when the height of the furnace chamber is 4 m, or over a height of at least 5 m-8 m when the height of the furnace chamber is 10 m.

According to an exemplary embodiment, the first height position is arranged at a distance of 1 to 3 m, in particular 1.5 to 2.5 m from the second height position when viewed from the base of the furnace chamber. It This allows for selective evacuation in the main degassing zone, especially in the horizontally heated channel areas that are burned individually.

According to an exemplary embodiment, the first height position is arranged at a distance of 3-6 m, in particular 4-5 m, from the third height position. This has a wide range of effects when there are relatively few height positions.

According to an exemplary embodiment, the second height position is arranged 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 an exemplary embodiment, the first height position is arranged at a distance of 0-2 m, in particular 1 m from the base of the furnace chamber, and/or the second height position is in the middle of the furnace chamber. Is located at a distance of 0 to 0.5 m and/or the third height position is located at a distance of 0 to 2 m, in particular 1 m from the top of the furnace chamber. This distribution provides a good compromise between equipment cost and complexity and selectivity or effectiveness for avoiding vertical gas flow. Among other things, it enables selective gas discharge in the main degassing zone.

According to the invention, the gas discharge arrangement sets at least three height positions for the gas withdrawal line, at least two of these heights being arranged in the upper half of the furnace chamber. This also provides an effective arrangement to prevent coking of the purge gas. Each gas draw line and/or associated gas valve or flange or seal may be specifically designed for the appropriate temperature range. In particular, the first gas withdrawal line and/or the first valve is temperature stable to at least 900° C., in particular up to 1000 or 1100° C., and the second gas withdrawal line and/or the second valve is It is temperature stable in the range of 300 to 600°C, and the third gas withdrawal line and/or the third valve is temperature stable in the range of at least 150 to 300°C. In other words, each gas withdrawal line and/or valve can be specifically designed for each gas type (including, inter alia, for corrosion resistance) and/or for a particular temperature regime. is there. For example, the material of the line can be appropriately selected. For example, the most ideal compromise between material, cost, and stability/resistance can be selected by one of ordinary skill in the art based on the particular type of gas to be controlled.

According to the invention, the respective height positions are arranged at a distance from each other of at least 20% to 45% of the overall height of the furnace chamber. This makes it possible to include a wide height section of the respective furnace chamber, especially in combination with pressure-dependent and/or volume-flow-dependent discharge regulation.

According to one exemplary embodiment, one of the height positions is provided at the top of the furnace chamber and the gas exhaust arrangement is arranged and connected to connect to a corresponding gas outlet at the top of the furnace chamber. At least one connection or at least one gas withdrawal line. With these, hot gases can be avoided, especially in the regions where the supplied briquettes remain very mildly and moderately acted upon by thermal energy.

According to an exemplary embodiment, the gas discharge arrangement is a separate raw gas cooling, tar shield/separation container, tar discharge device, dust, for handling the dischargeable gas from the (respective) furnace chamber. At least one component of an electronic filter and a desulfurization unit installed for reduction is provided. This allows the exhaust gas to be further processed in a gas-specific manner. The evacuation device makes it possible, for example, in the case of gases emanating from a certain height position, to prevent tar from condensing in the lines in the ambient atmosphere and causing blockages in these lines.

According to one exemplary embodiment, the gas discharge arrangement is provided in a parallel arrangement and comprises a plurality of gas withdrawal lines of the same function connectable to different furnace chambers at the same height position, the gas discharge arrangement comprising , A mixer to which gas discharge lines having the same function are connected. With this configuration, it is 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 structure and simplify its handling.

The above objective is also achieved by a furnace arrangement having at least one vertical furnace chamber, and in particular by the above vertical furnace arrangement having the gas discharge arrangement described above.

At least one of the above objects is also achieved according to the invention by a coke oven, in particular a vertical furnace, having the above-mentioned gas discharge arrangement. The coke oven preferably comprises vertically arranged furnace chambers which can be heat regulated in a clearly vertical direction for a particular height position.

The above objects are also in accordance with the invention from at least one vertical furnace of a furnace apparatus and from solid feedstocks for coking for the purpose of further handling of gases, in particular lignite, lightly caking bituminous coal, biomass, petroleum coke. A method for recovering gas from a furnace apparatus having at least one vertical furnace during coking of a feedstock from a group of petroleum coals, comprising at least three different gases (first gas and at least One additional gas) is selectively withdrawn/exhausted from the (respective) furnace chamber at at least three different height positions of the furnace chamber, and selectively downstream of the operating step, by virtue of the gas discharge arrangement described above. It is also achieved by methods that are handled and, more specifically, reused. This provides the above advantages.

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

The gas in question is more particularly a raw gas which forms in the furnace chamber under the influence of temperature during the coking operation and rises upwards through the bed. The gases/gas types that are discharged and handled include the following gases: C ₂ H ₆ , N ₂ , NH ₃ , CO, CH ₄ , H ₂ , H ₂ S, CO ₂ , SO ₂ , C ₂ H ₂ , _{C 2 H 4, C 3 H} 6, C 3 H 8, is formed from the particular BTX (benzene, toluene, xylene), and especially one or more gases from the group of other higher hydrocarbons.

It is possible to observe the desired temperature profile very accurately, as well as the absorption withdrawals at different height positions (ie also with specific exhaust gases). In corresponding conditions, eg, _{H 2} has about 6-7 times higher thermal conductivity than that of _{N 2.}

According to the invention, the discharge takes place over a height corresponding to at least half the height of the furnace chamber in at least three height positions, at least two of the at least three height positions being above the furnace chamber. Arranged in half and the respective height positions are at a distance from each other of at least 20% to 45% of the total height of the furnace chamber, and at least three different gases are taken from at least three different height positions. The lower one-third of the furnace chamber, the middle one-third, and the upper one-third, respectively. This provides the above advantages.

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

According to one embodiment, at least three different types of gas are withdrawn from at least three different height positions, in each case from a height section which extends over 20% to 30% of the height of the furnace chamber, or from the furnace. It is taken from the lower 1/3 of the chamber, the middle 1/3 and the upper 1/3. This makes it possible, in terms of technical equipment, to ensure that the impact is relatively wide and low in cost and complexity.

In this case, it is also possible to bridge or cross the temperature range, which is considered to be very important from experience, in particular the range from 350 to 470° C., as gently as possible, for example by time optimization. Experience has shown that feedstocks can be placed in this temperature zone/range so that adverse events such as "expansion" or "contraction/resolidification" that occur with a particular feedstock can thus be avoided or crossed. Can be transported through. Among other things, for example and/or in particular, certain types of gas can be aspirated/exhausted, for example at 450° C., which has proved to be of particular value, and the targeted emission based on height level. This makes it possible to promote this temperature range only in the small (height) zones in the respective furnace chambers.

According to one embodiment, the first gas is selectively withdrawn at a first height position within a range of 2 m or less below the top of the furnace chamber and additional gas is 35% of the height of the furnace chamber. ~ 65%, more particularly 45% to 55%, with additional heights selectively taken in at a further height position, another further gas is located at a further height position within a range of not more than 2 m above the bottom of the furnace chamber. The furnace chamber height is at least 4-6 m. This leads to an advantageous configuration and an effective influence at the relevant height position in each case and/or at the relevant temporal stage of the coking operation.

According to one embodiment, the at least three types of gas include individual adjustment of the volume flow discharged for each gas type, in particular to the volume discharged. This can affect not only the composition of the exhaust gas, but also the temperature profile in the briquette bed. For this purpose, at least one flow sensor can be provided, at least in each withdrawal line.

Modulation also allows for targeted effects of vertical gas flow that may not be completely prevented. For example, the gas withdrawal line disposed further below may have a pressure that is significantly reduced compared to the gas withdrawal line at a higher height position. The resulting effects are as follows. The vertically upward gas flows can be offset, or even the gas flows can be reversed and utilized to influence the temperature profile within the briquette bed. In this context, for each take-up line, more specifically, an individual measurement of the gas composition can be made by at least one gas sensor or at least one gas analysis system (for example spectroscopic or chromatographic analysis). Be wise.

According to one embodiment, further heating of at least three different gases/gas types taken from the (respective) furnace chamber includes, for example, methanol, dimethyl ether, olefins, humic acids, or synthetic natural gas. , The production of valuable chemicals. This allows for a considerable and sustainable overall economic process.

According to one embodiment, at least one of the at least three different gases/gas types withdrawn from the (respective) furnace chamber is fed as fuel to a burner that indirectly heats the furnace chamber. This makes it possible to save raw materials and energy. The gas withdrawn for the burner may consist in particular of at least 97% of the following constituents: C ₂ H ₆ , N ₂ , CO, CH ₄ , H ₂ , CO ₂ . The gas intended for the burner can be withdrawn at different height positions, in particular at three of the height positions. The gas may be purified, especially for BTX and higher hydrocarbons, before being fed to the respective burners. This improves the burner function.

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

According to one embodiment, the measurement, in particular the temperature measurement, is carried out in a meandering heating channel on at least one side of the furnace chamber at an inversion point with an observation site. According to one embodiment, the adjustment is carried out at least at one inversion point in the serpentine heating channel, in particular by an adjustment slide from the outside. According to one embodiment, at least one measurement and/or at least one adjustment by means of a sliding block comprises at least one heating channel, ie at least three horizontal heating channels and one meandering heating channel arranged thereon. From at least one heating channel, in particular at the inversion point. According to one embodiment, the short circuit or bypass occurs in one or more vertical channels of the serpentine heating channel of the furnace chamber, in particular by the elimination or interruption of the vertical channels. According to one embodiment, at least one adjusting member for adjustment, in particular a sliding block actuable from the outside, is arranged in each of the one or more vertical channels of the meandering heating channel. This provides each of the above advantages.

At least one of the above objects is in accordance with the invention at least one vertical furnace chamber for exhausting at least three gas types from the furnace chamber for the purpose of establishing a vertical temperature profile in the briquette bed of the furnace chamber. Can also be achieved by using the above-described gas exhaust arrangement.

According to the invention, at least one of the above objects is at least evacuated from a vertical furnace chamber for the purpose of providing fuel gas to at least one burner which indirectly heats the furnace chamber by means of the above gas evacuation arrangement. It is also achieved by the use of at least one of the three gas types.

At least one of the above objects is a furnace arrangement for producing coke briquettes according to the invention, comprising a gas discharge arrangement as described above and further a furnace arrangement, the lower half, more particularly the lower 1/ A furnace arrangement on at least one side of the furnace chamber in at least one heating wall at 3 is provided with at least one horizontal heating channel, and more particularly also at least at the beginning of the upper half or the middle third Heating channels are provided, which meanderingly extend in a plurality of height planes, each heating channel being individually heatable by at least one burner, in particular with the gas discharged from the furnace chamber. It can also be achieved by the furnace configuration.

At least one of the above objects is a method of producing briquettes from a carbonaceous solid feedstock according to the present invention, not only for drying briquettes made from the feedstock in a briquette dryer, but also for coke in a furnace chamber. Including coking of briquettes to form briquettes, the gas is exhausted at at least three height positions of the furnace chamber, the at least three height positions being distributed over at least half the height of the furnace chamber, The gas is also achieved by a method in which the gas is at least partially passed through a burner arranged in the furnace chamber for heating the furnace chamber. The method can be carried out with the furnace configuration described above.

Regarding the operating mode of each furnace chamber, the following may be mentioned. The raw material briquettes pass through their respective furnace chambers for 4 to 15 hours, especially 6 to 9 hours. In this procedure, the raw material briquettes are heated in a particularly multi-stage manner from an initial temperature of 100-200°C, in particular 150°C, to a final temperature of 900-1100°C. The required heat can be generated in two channels which are arranged transversely to each furnace chamber and can be heated by multiple external burners, this heat passing through the stone dividing wall into each furnace chamber. It is transmitted indirectly.

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

The types of coal of which the briquettes consist include lignite (hard and soft) containing, inter alia, a volatile carbon content (vc) of more than 45% by weight and a water content of more than 45% by weight. The raw material to be processed into briquettes contains 28% by mass to 45% by mass of volatile components (particularly, gas coal, gas long-flame charcoal, long-flame charcoal), or otherwise 22% by mass or less. It may include a slightly caking bituminous coal containing volatile components (especially blacksmith coal and poor coal). The slightly caking bituminous coal itself has a low caking property. In the preceding mixing operation, the slightly caking bituminous coal may be mixed with an adhesive, which increases the caking adhesion effect of the coal particles during the briquetting operation.

Due to the nature of the crucible coke, fatty coal is particularly representative of strongly coking coal (conventional "coke charcoal"). Furthermore, so-called blacksmith and gas coals are also strongly coking coals. All other types of coal are referred to herein as light coking coal.

Briquettes include anthracite (vc<12%), poor coal (12%<vc<19%), gas coal (28%<vc<35%), gas flame flame (35%<vc<45%), etc. Of bituminous coal types, or alternatively a mixture of these coal types, and high grade fat (coke) charcoal (19%<vc<28%) may also be used. I know. These percentages, and based on specifications for coal types, allow even more specific allocations.

The raw material may be comminuted in a perforated plate roll grinder, in particular into pellets having a particle size of 0-2 mm. It has been found that the pellets/particles produced by the perforated plate roll grinder are particularly easy to adhere (easily caking) and therefore the downstream briquetting operation (molding) is simple.

After milling, the raw material is shaped. This molding process (coagulation) is preferably carried out on a ram press in the forming channel. It has been found that a high pressure briquette can be produced by the shape of a channel die in the form of a Venturi tube with a narrow cross section and a wide cross section outward. Other types of presses have not been able to provide comparative quality results.

Furthermore, it has been found that very high briquette strength can be achieved when the feedstock is pressed through a narrowing cross section after it has been molded in a mold. Higher briquette strength may be achieved when the subsequent feedstock is guided along a diverging runout section. Advantageously, the narrowing portion is shorter than the runout portion or shorter than the widening cross section.

It has been found that flat cylindrical (disk-like, puck-like) briquettes provide particularly good strength values, both before and after coking. In particular, a ratio of briquette diameter to briquette height of 1-5, especially 2-3, gives good results for heating and coking operations. The diameter of the briquettes is preferably 20-100 mm. Briquettes are produced from coal particle sizes of 0-2 mm, among others.

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, platelets, mussels, cushions, balls or egg shapes. It will be clear that it is okay. In the experiments to date, the best experience has been achieved with the pack geometry.

The parameters of this method are as follows. Press pressure, press time, press temperature. The shaping is carried out, inter alia, at a pressure of 120 to 150 MPa, in particular 140 MPa. The shaping is carried out at a temperature of between 60 and 100° C., among others. Molding takes place in particular for a time of 15 seconds or less.

The types of coal described herein are mixed with coking assistants in upstream operating steps to make coking more efficient and to give coke products, for example, higher strength or more. It has been found that higher quality can be achieved, such as higher reactivity.

According to one embodiment, at least one coking aid is fed to the briquetting operation (during molding), in particular for improving the efficiency of the downstream coking process. The coking aids may be selected individually or in combination from the group of coking aids already proven to be particularly useful to date in conjunction with conventional feedstocks. Good.

Through the method described herein, when using lignite as a feedstock, the carbon content C(fix) of the coke produced may be increased to a value above 55%, i.e. It has been found that even direct smelting reduction processes (PRIMETALS COREX/FINEX processes) that produce steel can be used subsequently.

Prior to the pressing and coking operations, the raw material is preferably a binder in a single-stage or multi-stage mixing operation, especially to improve the quality of the coke produced or to accelerate the briquette pressing operation from the fine coking coal species. Mixed with (sticking) and coking systems. Such auxiliaries are preferably mixed at a temperature in the range 30 to 120° C. before briquetting.

Adjuvants include, among others, the following groups: molasses, sulfite waste liquor, sulfate pulp waste liquor, propane bitumen, cellulose fibers, HSC (heavy oil pyrolysis) residues from the petroleum industry, mixed HSC/ROSE (residual oil supercritical extraction ) It may be selected from the residues or may be selected in combination.

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

It has been found that for the coal species described herein, the addition of water tends to be unfavorable. Lignite, for example, traditionally has a water content of greater than 45%. It has been found to make 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 proven to be advantageous. Therefore, predrying may also be present.

Subsequent briquetting operations are carried out especially in the temperature range 40-90°C, in particular 55-65°C. Due to this agglomerate morphology, some of the briquettes produced have high compressive strength and wear strength, especially strengths above 30 MPa.

The briquettes can be installed using a crane above the main dryer and can slide through the main dryer, through the coke shaft, and into the coke dry chiller.

It has been found to be advantageous to gently dry the briquettes to a water content of 2-4% by weight during the main drying operation after coagulation.

The main operation of briquette drying is carried out, inter alia, by the roof dryer unit, which serves to further reduce the water content of the briquette from about 20% 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 shows that this can also lead to briquette crushing.

The main drying operation is carried out, inter alia, in two stages, but it can also be a single-stage or multistage operation. The drying medium used is preferably thermal waste gas/raw gas resulting from the combustion operation in the heating channel of the furnace chamber located below the dryer, which can enter upwards in the roof-mounted channel. it can.

The arrangement of these channels is especially cruciform for the cross flow management regime. In some parts, at least provision for counter-current or co-current may also be provided.

To improve the drying efficiency, the main drying unit installed for main drying may be connected to an external burner with flame monitoring, all or two or more, or so, depending on the flame monitoring. Otherwise, additional waste gas can be provided for only one drying stage. The main drying unit and the respective furnace chambers may be separated from each other by a hermetically sealable, in particular 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 management regime provides advantages. In the first stage, the briquettes are heated to a temperature range of 300 to 400° C. and operated at a temperature rise of 0.75 to 0.9 K/min, in particular for 0 to about 4 to 7 hours. In at least one further step, the briquettes are brought into the temperature range of 300-1100° C. and the heating is carried out at a heating rate of 2.6-3 K/min.

For certain feedstocks it may also be advantageous to carry out the heating only in one stage with a constant heating rate, which can likewise be associated with the desired high coke strength.

Thanks to the sustainable method or methods described herein (especially in combination with the unique agglomeration technology), it is possible to provide relatively high quality coke or coal to the feedstock. Maintaining the desired briquette shape, especially the cylindrical pack shape, can be ensured during coking. In the course of the coking process, the coal is reduced by 40% to 60%, in particular 50% both in terms of mass and volume, which further leads to the desired high compressive strength and wear strength above 30 MPa (especially reaction (CSR ) After coke strength) as well as low reactivity with CRI (Coke Reactivity Index) values of less than 55%. This upper limit on reactivity is necessary because otherwise the briquettes could begin to burn themselves in the presence of air. The quality level set by these limits is not yet achievable with the current low grade coal described. Among other things, the current methods and devices result in cracking of the briquettes or even complete destruction of the briquette shape. Changes in mass and volume can occur in the same proportions, among others.

Thanks to the method described here, the briquette shape (pack shape) can be maintained, so that the pressure drop, heat transport, flow profile and other method parameters remain presettable.

Each furnace chamber is made of refractory silica material, among others.

Aspects relating to heat/energy balance optimization are described below.

On the sides of each furnace chamber, especially on both sides, there may be heating ducts integrated into the wall. The heating duct is combusted by at least one, preferably four external burners. The burners are connected to the horizontal heating channels, in particular overlapping. Here, waste gas or fuel gas from the heating wall is also available for energy, for which purpose take-off amines may be supplemented by flue gas blowers.

According to an advantageous and exemplary embodiment, three burners are provided/connected to the lower or the lower 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. It has been found that the centralized arrangement of the three burners in the lower region of the shaft/furnace makes it possible to form a strong heat source there, which is the 500°C required for coke formation. It means that over-temperature is generated in the furnace chamber.

According to an advantageous and exemplary embodiment, above the lower or bottom horizontal channel, meanderingly above as a fourth channel (counting from the bottom) formed in the heating wall. There is a channel facing. Similarly, burners can be connected to the serpentine channels. It has been found that this tortuous channel ensures a favorable distribution of heat, especially in the vertical direction. On going up, the waste gas produced by the corresponding burner (especially the fourth) is slowly cooled, thereby ensuring a vertical, gradual heat transfer to the loading/bed of briquettes. You can This type of gradual heat transfer provides various advantages, whether in terms of energy, or in terms of briquette dimensional stability, or in general of mild coking procedures. The burner may be burned with coke oven gas, especially from natural gas and/or coke shafts.

Thanks to the above configuration, one would not have to have the expensive generator gas units currently used to generate combustion gases from coal, which in fact have demerits in their generation upstream of their respective furnace chambers. You can

Aspects relating to the sustained use of by-products formed during coking are described below. Particularly in connection with the feedstocks described herein, it is advantageous to withdraw by-products from different elevations of the respective furnace chambers, in order to achieve high selectivity and even effective temperature control regimes. It is known that significant impacts are possible.

According to an advantageous and exemplary embodiment, the high-calorie gas formed in the respective furnace chambers during coking is taken off at one to five withdrawal sites at different height positions, thus It is discharged from the factory and sent for further use. There may be a port with a preset angle, among others, at each ejection site.

At present, there is an undesired phenomenon commonly referred to as coking of the purge gas in the upper part of the furnace chamber. The purge gas provided by the gas released at the bottom rises within the furnace chamber and undergoes unwanted reactions with briquettes placed at the top in an undesired or uncontrolled temperature range. Experience has shown that in these upper areas of the furnace chamber this is accompanied by unwanted convection heat transfer and coke degradation. At present, this means that in many arrangements or furnace configurations, controlling the temperature profile in the floor is not straightforward. Therefore, coking is done in a somewhat chaotic form.

It has been found that an arrangement with withdrawal sites located at different heights can prevent the coking of the purge gas that currently typically occurs at the top of the furnace chamber.

In addition, this measure involves the fractional discharge of the gas released from the coking process at the individual stages of the coking operation, feeding them to the native gas process facility, and/or to valuable chemicals. And the advantage is that you can convert them. Fractional withdrawal in this context means withdrawal at different height positions and withdrawal of different gas types or gas compositions. It has been found that the presettable distance (depending on the type of feedstock or coking procedure) between the take-off sites also allows a highly selective pre-selection for the composition of the gas taken out.

Advantageously, one, two or more, or otherwise all of the unloading sites are vertically located at least 50% above the shaft/basement outlet of the respective furnace chamber. This is in no way advantageous for the arrangement of the holding zone in front of the export system. As a result, raw gas may be sucked from the upper region and returned to the shaft via the lower "suction off" system. For this purpose, the respective lower gas withdrawal line can also be re-conceived as a gas supply line. Therefore, the gas can locally pass over the hot briquette, thereby establishing a quality improvement effect.

In the downstream operating steps, high value substances such as methanol, synthetic natural gas or dimethyl ether can be produced from these exhaust gases. 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 devices to date have the disadvantage that the gas formed in the furnace chamber can only be discharged at best in a single stage. In this case, adverse heat transfer and chemical conversion events occurred not only in the coking efficiency but also in the quality of the gas preparation, especially in the upper region of the respective furnace chambers.

Aspects of long-term use of energy spent or generated during coking are described below. Among other things, 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 controlled partial withdrawal to humidify the circulating dry gas. There may also be steam generation, especially for steam power plants for heating devices, conduits, valves. Steam may also be obtained and/or utilized in the form of process steam for the processing of crude gas. At a sufficiently high temperature level (especially in the gas of the waste gas from the bottom burner), the supply to the waste heat recovery unit may be carried out and/or the flue gas may be supplied to the dry cooling installation. May be.

According to an advantageous and exemplary embodiment, the gastight unloading system can be arranged below the (respective) furnace chamber to transfer the thermal coke to the dry cooling installation. The export system may be constructed in the form of a shaft. The unloading system may be installed to accommodate the total amount of coke from two adjacent furnace chambers.

According to one advantageous and exemplary embodiment, the coke is brought from a temperature level in the region above 900° C. to a temperature level below 200° C., in particular by introduction of cold inert gas, in particular from below without addition of water. To be cooled. It has been found that the cooling gas, which flows upwards through the cooling shaft coke bed to obtain heat in this way, can be supplied to heat exchangers, in particular heat exchangers for the production of steam, especially with an improved energy balance. There is. To provide the pressure difference, a reduced pressure system may be provided, in particular in the form of a blower, which reduced pressure system may be connected to a dry cooling installation and/or a heat exchanger.

With this type of arrangement, it is possible to achieve lower coke temperatures than dry cooling installations below 200°C. A rocker or pendulum structure may be embodied, for example, for picking up coke. Thus, cold cooling gas can be introduced into the dry cooling installation through the free bed area.

At least one of the above objects is a furnace configuration for briquette production, comprising the furnace apparatus described above and a gas discharge configuration, wherein the gas discharge configuration is provided in at least one furnace chamber of the furnace apparatus. It is also achieved by a furnace configuration, which is connected by at least three gas draw lines at three height positions. This provides the above advantages.

At least one of the above objectives is a method of producing briquettes from a carbonaceous solid feedstock, comprising drying briquettes produced from the feedstock in a briquette dryer along a presettable first temperature gradient, Further comprising coking briquettes for coking briquettes in the furnace chamber along at least one presettable second temperature value, the second temperature gradient being at least three heights of the furnace chamber. Established by outgassing in position, the at least three height positions are also achieved by the briquetting process, which is distributed over at least half the height of the furnace chamber. This provides the above advantages.

According to an advantageous embodiment, the method is carried out with the furnace arrangement described above.

According to an advantageous embodiment, the briquettes provided for the briquette dryer are in a pre-dried form with a water content of 10-12 wt. There is drying to less than wt%. This allows a particularly gentle treatment of the feedstock.

Further features and advantages of the invention will be apparent from the description of at least one exemplary embodiment using the drawings, and also from the drawings themselves. Reference numerals that are not explicitly stated with respect to the individual figures refer to other figures. What each drawing shows as a schematic representation is as follows.

FIG. 3 is a side view of a furnace apparatus and coal utilization configuration according to an exemplary embodiment. 4 is an exemplary adjustable temperature profile according to one embodiment across a height of a furnace apparatus according to one exemplary embodiment. FIG. 3 is a side view of a furnace apparatus and coal utilization configuration according to an exemplary embodiment. FIG. 3 is a diagram of individual components of a furnace apparatus in a coal utilization configuration that includes the furnace apparatus, according to an illustrative embodiment. FIG. 3 is a detailed view of individual components of a briquette dryer in a furnace system, according to an exemplary embodiment. FIG. 3 is a partial side view of a wall of a furnace chamber of a furnace apparatus, according to an exemplary embodiment. FIG. 5 is a basic diagrammatic representation of an indirect method of heat regulation in a furnace chamber, according to one embodiment. FIG. 3 illustrates individual components of a coke dry cooling installation of a furnace system, according to an exemplary embodiment. FIG. 3 is a schematic diagram illustrating individual components of a gas discharge configuration of a furnace system/furnace configuration or individual components of a coal utilization configuration comprising a furnace system, according to an exemplary embodiment.

FIG. 1A shows a furnace apparatus 10, in particular a coke oven having a plurality of vertical chambers 11. The feedstock 1 in the form of briquettes 5 is fed by a feed unit 10.1 to a briquette dryer 15 where it is preheated, said briquette dryer 15 being arranged above the furnace chamber 11. The pre-dried feedstock 5 is then coke by indirect heating via the heating wall 12 of the furnace chamber 11 according to an exactly presettable temperature profile, which will be described in more detail below (in particular FIGS. 4A, 4B). Can be Coking may be done before drying. For this purpose, a coke dry cooling installation 19 is connected at the bottom of the respective furnace chamber 11. Feeding and removal of feedstocks 1, 5, 6 may be accomplished vigorously by an import system 16 and an export system 17, each of which is driven, inter alia by gravity, to one or more locks 16.1, 17. .1 is provided. The coke-dried briquette 6 can be cut out and placed in a temporary storage in the sectioning facility 17.9.

The furnace apparatus 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). It is heated from the side by the wall. The heat transfer is performed indirectly via the heating wall.

FIG. 1C schematically illustrates how the dryer 15 may be connected to multiple furnace chambers 11. The coke dry cooling facility 19 may likewise be connected to a plurality of furnace chambers 11.

The temperature profile T over the height z is shown in FIG. 1B, here with six steps highlighted. In stage I, the drying takes place in a briquette dryer, which is schematically illustrated here as a linear temperature profile, which may also be non-linear. In Stage II, the feedstock is transferred to the respective upper furnace chamber and maintained at least about the Stage I final temperature. For this purpose, the loading system may feature thermal conditioning and/or may be equipped with heating equipment. In Stage III, the first coke stage is shown with a relatively low temperature rise or temperature gradient. This allows, among other things, mild heating and gentle elimination of external substances/gas components. In Stage IV, the temperature gradient can be steeper, especially since the feedstock has already discharged a large amount of immiscible external material here. The energy supply can be increased without over-stressing the feedstock. In stage V, the maximum final temperature during coking is reached and cooling may take place in the coke dry chiller. The temperature profiles at stage IV and stage V are each shown here schematically as linear, but may also be non-linear depending on the stage in progress. In stage VI, coked briquettes are available or accessible for further processing either at downstream operating steps.

The heating can be achieved, inter alia, very gently at first, with a temperature gradient in the region of 0.8 K/min, in particular in a continuous and monotonic increase, up to a temperature in the region of 320° C. and/or for up to 6 hours. (Step IV). After that, the slope of the temperature gradient is significantly higher, in particular in the region of 2.8 K/min, with a particularly continuous and monotonic increase, up to a temperature in the region of 1050° C. and/or for up to 5 or 6 hours. Can be (step V). The transition can be continuous or unchanged.

The upper temperature zone (the first temperature zone in the direction of material flow, eg the upper part of the furnace chamber when viewed in the direction of material flow, first 4 m) has a more moderate temperature due to 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 material flow direction, eg 2 m at the bottom of the furnace chamber) can be realized with a steeper temperature gradient by at least three individually burnt horizontal heating channels Good.

FIG. 2 generally illustrates the relationship between individual facility components of the furnace configuration 50 or coal utilization configuration 80. The feedstock/raw material 1 is fed to a facility component for molding/compression (in particular a two-stage agglomeration) and stays in this facility component in the form of compacts or briquettes, especially in the form of discs or packs. The product after coking takes the form of coke briquettes 6. The coal utilization configuration 18 comprises not only at least one furnace apparatus 10 already described above, but also a gas discharge configuration (FIG. 6) and/or compression facility components. Here, the individual facility components may be appropriately connected to one another for the purpose of not less than high energy efficiency. A recovery system 18 having at least one return line from the (respective) furnace chamber back to the dryer 15 is provided in particular, ie the waste gas G2 from the respective furnace chamber 11 is also used for heat regulation of the dryer 15. Can be used. In contrast, the raw gas G1 may be collected by the gas exhaust arrangement 30 and managed for further use/recycle.

FIG. 3 shows the dryer 15 in detail. Within the plurality of drying planes or drying circuits 15.6, 15.7, 15.8, respectively heating elements 15.4, 15.5, in particular hot gas lines, are present at different temperatures. The other heating element 15.5 is less warm than the lower heating element 15.4 and may be formed, for example, by the return line of the circuit. In the lower heating element 15.4, the hot gas of the hot gas circuit 15a can be supplied, for example, at the lowest drying level 15.8, in particular with a high energy content. Within the briquette dryer, in particular, temperature and humidity sensors may be present, more particularly at more than one level.

The individual sensors can be elements of the measurement facility 14 that are coupled to the control facility 20. Notably, there may be one or more temperature sensors 14.1, H ₂ O sensors 14.2 and/or pressure sensors 14.3, but their position is only shown here schematically.

The dryer 15 comprises at least one storage 15.1 which is in particular sized for gravity-driven continuous operation. The heating facility 15.2 of the reservoir may be formed by the lines 15.4, 15.5 described above or may be equipped with additional heating elements. The line is preferably arranged below the roof element 15.3, around which the briquettes can slide downwards.

Each of the drying circuits 15.7, 15.8 can in particular comprise two drying planes 15.6, the tops of the two drying planes 15.6 already carrying heat energy being respectively cooling planes. , Where the dry gas can be drawn off under suction. The arrangement thus comprises at least two inlet planes and two suction extraction planes, the temperature and the amount of drying gas being required individually in each inlet plane. Each drying circuit can be adjusted at least with respect to the hot gas volume flow and the inlet temperature. The uniform division of the dry gas over the individual lines of one plane and/or the roof can be effected, for example, via valves, manually adjustable perforated plates and the like.

The 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 from the side or in cross section yz. The three horizontal heating channels 12.1 each extend in a single height plane and each lead to a vertical exhaust gas flue (take-off line) 12.3, which is in each case burned individually by a burner 13. In the text below, the term "flue" is used only for lines oriented perpendicular to the briquette/coke briquette transport direction, in particular the waste gas line, and therefore not for horizontal heating channels. The burner axis 13.1 in each case at least approximately coincides with the long axis of the respective channel 12.1. On a horizontal uniplanar channel, the serpentine heating channel 12.2 extends over a number of height planes, ie also comprises a number of inversions or inversion points 12.21. The serpentine heating channel 12.2 is also burned by the burner 13. The resulting temperature profile decreases upwards. That is, the briquettes fed to the furnace chamber are first very carefully heat-conditioned and, in the region of the horizontal single-plane channel 12.1 below, receive a continuously increasing energy supply.

On each channel 12.1, 12.2, at least one observation point 12.22 and/or measurement point for the measurement sensor system 14 may also be provided, in particular also an inversion point 12.21. The serpentine heating channel 12.2 may comprise one or more vertical channels 12.5. The vertical flow path 12.5 allows, in a sense, short circuits in the energy supply and vertical or horizontal energy distribution. 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 over the temperature profile within the furnace chamber 11. Here, the measurement sensor system 14.4 can also be provided, especially in the observation point. In order to allow easy access to each observation point 12.22, an access tube can be provided therein, in particular a manually accessible access tube, in the heating wall.

A vertical waste gas flue located on the end-side front of the heating wall allows further control of the connection of the fourth heating channel to each heating channel section, in particular heating as a function of the feedstock used. Can be prepared. Due to the sliding block 12.9, which may be arranged in the heating channel, the hot form of the exhaust gas, in particular starting from the fourth heating channel from the bottom, in the exhaust gas flue or in a preset horizontal position There is also the possibility of turning directly upward. As a result, the serpentine channel 12.2 can be short-circuited at one or more horizontal or vertical positions. This allows the individual heating channels to be heated either vertically or horizontally according to the individually presettable desired temperature profile. In particular, dangerous temperature ranges, for example 350-410° C. or 410-470° C., can be avoided in a targeted manner or at least restricted to short, locally small temperature zones. The sliding block can be positioned by means of an adjusting slider, for example in the observation opening 12.22.

The vertical channels 12.5 can be distributed in a matrix fashion over the heating channels, which makes it possible to implement a number of options for adjusting/adjusting the input of energy into the furnace chamber.

Further parameters affecting the temperature profile in the furnace chamber occur through the supply of air to the respective heating channel and/or through the drive/regulation of the individual burners as a function of other burners. That is, the control facility is not only in communication with all the burners, but also has a valve or flap for air supply and/or a valve or flap on each vertical channel or a block for opening and closing each vertical channel. It may be in communication with the equipment for doing.

Thanks to the observation point 12.22, each equipped with a sensor system 14.4, among others, the thermal 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 Figure 4C, a xz side view is shown. In FIG. 4C, the gas outlets 12.6, 12.7, 12.8 are already shown in three different height positions, which will be explained in detail in FIG.

For optimum heating management, among other things, at least four external burners 13 are provided per heating wall, oriented in the x-axis or y-axis direction and arranged alternately in front of and behind the furnace chamber 11. It

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

The horizontal heating channels 12.1 are particularly parallel in orientation to one another and intersect the corresponding vertical waste gas flues 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 contemplated (about 1 m). This part is sometimes described as a holding zone and can support full through coking and full degassing while positively impacting coke quality.

Regarding the collection system 18, the following may also be mentioned. The briquette dryer is mounted above the furnace chamber and can be provided with waste gas from the respective burner via the (vertical) waste gas flue. This waste gas is available as a drying medium in two separate drying circuits in the briquette dryer, defined here as a pre-dryer stage and a main dryer stage. In other words, it is possible to provide two drying circuits, each of which in particular can be provided by the thermal energy from the burner of the furnace unit. Both circuits may also be equipped with an additional external burner, which is, inter alia, for extra or more flexible adjustability.

The thermal waste gas from the primary exothermic system (first drying circuit) can be provided by at least three external burners, which are connected to three horizontal heating channels located in particular at the bottom of the respective furnace chambers. The thermal waste gas from the secondary heating system (second drying circuit) may be provided by at least one external burner connected to a serpentine heating channel lying over a horizontal heating channel.

FIG. 5 shows the individual components of the dry cooling installation 19 arranged below the furnace chamber 11. A gas circuit 19.5 is operated by a pump 19.1 and a heat exchanger 19.3, where the coked briquettes 6 are cooled countercurrently in the cavity 19.7 and the gas is at least one inlet 19.9. Through it into the cavity and is exhausted again through at least one outlet 19.8. The outlet is located immediately below the furnace chamber 11 and is separated from the furnace chamber by a baffle plate or a protruding wall. The advantage of this arrangement is that the briquettes from the furnace chamber 11 are first surrounded by a stream of cooling gas which has already been heated to very high temperatures. Therefore, in this way, gentle cooling is provided. Similarly, the (temperature) stress on the briquettes is minimized. Nevertheless, cooling can clearly be effective.

At least one flow barrier or gas shunt unit 19.6 is centrally located within the cavity 19.7. This makes it possible to adjust the flow profile. In particular, the main transport of energy and/or lumps occurring in the center of the cavity 19.7 can be prevented.

A particular feature of the vertical furnace is that the coke dry cooling is located in "fine alignment" with the underside of the furnace chamber. Therefore, the cavity of the dry cooling facility may have the same cross section as the furnace chamber. This is an advantage of direct gravity driven carriage of briquettes, thus simplifying continuous operation. The transition is particularly uninterrupted because there is no physical separation between the furnace chamber and the dry cooling equipment.

At least one roof and/or gas diverting unit 19.6, which is arranged diametrically centrally, in particular, diverts the cooling gas homogeneously diametrically, and in particular also in a homogeneous manner, the outlet 19.8. You can be sure to guide to.

FIG. 6 shows a furnace arrangement 50 comprising a gas discharge arrangement 30 having one or more gas extraction lines 31 for a first height position, the gas extraction line 31 comprising a connection or connection 31.1. It can be connected to each furnace chamber 11 via. One or more gas withdrawal lines 33 for at least one further height position, here the second and third height positions, are also provided, the second and third height positions being respectively connected in the same way. 33.1 is provided. Furthermore, a plurality of mixers 35.1 and at least one pump 35.2 are provided for further management of the exhaust gas. Corresponding gas outlets or connections 12.6, 12.7, 12.8 are provided on the respective furnace chamber 11 for the respective height positions.

Here, the raw gas is in three or more height planes, individually for each furnace chamber, via a riser pipe at the top of the furnace (the position of the topmost kind), and the preset height of the furnace chamber is set. Through one or more connections arranged in a vertical position, and in particular through one or more vertical exhaust gas flues in the respective heating wall (intermediate height position), and further the furnace chamber Under suction by means of one or more connections arranged in preset height positions of, and in particular through one or more vertical exhaust gas flues in the heating wall (bottom height position) Can be removed.

The raw gas withdrawn may be cooled and collected via a separate/separated raw gas collection line and then incorporated into one or more raw gas collection lines. It has been found that in the case of direct suction extraction of raw gas (especially immediately downstream of the lock installation of the briquette loading system), the risk of raw gas moving from the furnace chamber to the pre-dryer can be reduced, which is not small It depends on the reduced pressure generated here. This can further improve the quality.

1 Feedstock/Raw Material 1.1 Pellets, especially those produced by using a perforated plate roll grinder 2 Coking aids 3 Adhesives 4 Briquette strands 5 Compacts or briquettes, especially discs or packs 6 Compacts Or coke briquettes, especially in the form of discs or packs 10 furnace equipment, especially coke oven 10.1 supply unit 11 furnace chamber 12 heating wall 12.1 horizontal heating channels in a single plane 12.2 meandering heating channels in multiple planes 12. 21 Inversion or reversal point 12.22 Observation point or measurement point for measurement sensor system 12.3 Vertical waste gas flue (collection line)
12.5 Vertical flow path 12.6 Gas outlet or connection at first height position 12.7 Gas outlet or further (second) height position 12.8 Gas outlet or further (third position) ) connected 12.9 sliding block 13 burner 13.1 burner axis 14 measurement facility at the height position, in particular 14.1 temperature sensor 14.2 H ₂ O sensors 14.3 pressure sensor comprises a temperature sensor and / or H2O sensor 14.4 Observation point-specific measurement sensor system 15 Briquette dryer, in particular with roof dryer unit 15a Dryer unit with hot gas circulation, in particular roof dryer unit 15.1 Reservoir, especially size 15 for continuous operation .2 Reservoir heating equipment 15.3 Roof element 15.4 Heating element, especially line at first temperature/hot gas line 15.5 Heating element, especially line at second temperature/hot gas line 15. 6 Drying plane 15.7 First drying circuit 15.8 Further (second) drying circuit 16 Loading system 16.1 Locking facility 17 Unloading system 17.1 Locking facility 17.9 Sectioning facility 18 For gas from furnace chamber Recovery system 19 with at least one return line of coke dry cooling equipment or dry cooling equipment 19.1 pump 19.3 heat exchanger 19.5 line system, in particular circuit 19.6 roof or gas distribution unit 19.7 Cavity 19.8 Outlet 19.9 Inlet 20 Control equipment 30 Gas outlet arrangement 31 Gas take-up line for the first height position 31.1 Connection or connection 33 Gas take-off line 33 for at least one further height position 33 .1 Connection or connection 35.1 Mixer 35.2 Pump 50 Furnace configuration 80 Coal utilization configuration G1 Raw gas G2 Waste gas

Claims (19)

A furnace apparatus having at least one vertical furnace chamber during coking of at least one solid feedstock from the group consisting of lignite, slightly cindered bituminous coal, biomass, petroleum coke, petroleum coal to produce coke ( A gas discharge arrangement (30) for obtaining gas from 10), which is configured to connect to at least one of the vertical furnace chambers (11) of the furnace apparatus (10),
At least three gas draw lines (31, 33), which may be arranged at at least three different height positions of each of the furnace chambers and which are installed to connect to the furnace chambers at the at least three height positions. Installed to selectively manage at least three gas types selectively discharged by each said gas draw line, and/corresponding to at least half the height of said furnace chamber (11) Extending at a height that defines at least three height positions with respect to the gas draw lines (31, 33), at least two of which are located in the upper half of the furnace chamber (11) Gas evacuation arrangement (30), characterized in that the positions are respectively arranged at a distance from each other of at least 20% to 45% of the total height of the furnace chamber (11). The gas exhaust arrangement (30) according to claim 1, wherein the gas exhaust arrangement extends over a height corresponding to at least 75% of the height of the furnace chamber. The first height position is/is arranged at a distance of 1 to 3 m, in particular 1.5 to 2.5 m to the second height position as viewed from the base of the furnace chamber (11), and/or The first height position is arranged at a distance of 3 to 6 m, in particular 4 to 5 m to the third height position, and/or the second height position is to the third height position. Arranged at a distance of 1 to 3 m, in particular 1.5 to 2.5 m, and/or said first height position is arranged at a distance of 0 to 2 m, in particular 1 m from said base of said furnace chamber (11) And/or the second height position is arranged at a distance of 0 to 0.5 m with respect to the center of the furnace chamber (11), and/or the third height position is the furnace. A gas discharge arrangement (30) according to any one of claims 1 or 2, arranged at a distance of 0-2 m, in particular 1 m from the top of the chamber (11). The gas exhaust arrangement (30) according to claim 3, comprising at least one of the height positions a plurality of gas withdrawal lines (31, 33) which may be arranged at a plurality of sites, in particular at the periphery. At least one of a separate raw gas cooling, a tar shielding/separating container, a tar discharging device, an electronic filter installed for dust reduction, and a desulfurization unit for handling the gas discharged from the furnace chamber (11). A gas evacuation arrangement (30) according to any one of claims 1 to 4, comprising three components. A plurality of gas taking lines (31, 33) having the same function, which are provided in a parallel arrangement and can be connected to different furnace chambers at the same height position, are connected/connected to each other. A gas discharge arrangement (30) according to any one of claims 1 to 5, comprising a mixer (35.1) that can be. On at least one side of the furnace chamber, there is a serpentine heating channel with at least one inversion, in which there is an observation point or measurement point, and/or of the heating wall in the lower half. On at least one side of the furnace chamber (11) in at least one of them there are at least three horizontal heating channels (12.1) and one meandering heating channel (12.2) above them, The heating channels are each individually heatable by at least one burner (13), and/or the observation site has a sensor, in particular a temperature sensor, on which the meandering heating channel is arranged or carries out a measurement. With a reversal point (12.21) with (12.22) and/or the meandering heating channel with at least one reversal point (12.21), in particular operated by an external adjustment slide A possible closed observation site (12.22) is arranged and/or an adjusting slide for the sliding block (12.9) is provided in at least one of the heating channels, in particular at the reversal point (12.21). At least one observation site is arranged and/or has a measuring sensor system (14) and/or a manually accessible access tube for adjusting slides is provided in at least one of said heating channels, in particular 7. A gas evacuation arrangement (30) according to any one of claims 1 to 6, which is connected to the meandering heating channel. Said meandering heating channel comprises one or more vertical channels (12.5), and/or said meandering heating channel excludes or interrupts one or more horizontal or vertical positions, in particular vertical channels. By means of which it is arranged to be short-circuited/short-circuited and/or the meandering heating channel is provided with one or more vertical channels (12.5), each of which has at least one regulating member, 8. The gas discharge arrangement (30) according to claim 7, wherein in particular a sliding block (12.9) actable from the outside is arranged. Furnace apparatus (10) comprising at least one vertical furnace chamber (11) having a gas discharge arrangement (30) according to any one of claims 1 to 8, in particular a vertical furnace. Generating coke from a furnace device (10) having at least one vertical furnace chamber during coking of a solid feedstock, in particular from a feedstock from the group consisting of lignite, slightly caking bituminous coal, biomass, petroleum coke, petroleum coal A method for obtaining gas from the at least one vertical furnace chamber (11) of the furnace apparatus (10) during the process and for further management of the gas,
At least three different gas types from the furnace chamber, in particular due to the gas discharge arrangement (30) according to any one of claims 1 to 8, at least three different heights of each furnace chamber (11). Selectively taken/exhausted in the height position and selectively managed downstream of the operating step, in particular recycled, the discharge is at/at the height of the furnace chamber (11) in at least three height positions. Performed over a height corresponding to at least half, at least two of the at least three height positions being arranged in the upper half of the furnace chamber (11), said height positions being respectively relative to one another in the furnace chamber (11). ) Of at least 20% to 45% of the total height, and at least three different gases are at least 3 in the bottom 1/3, middle 1/3 and top 1/3 of the furnace chamber, respectively. Method, characterized in that it is taken from three different height positions. The first gas is selectively withdrawn in the temperature range of 150-300° C., and/or the additional gas is selectively withdrawn in the temperature range of 300-600° C., and another additional gas is 600-950. C. or in the temperature range of 700-900.degree. C., and/or at least three different gases are respectively drawn from one height section over 20% to 30% of the height of the furnace chamber (11). Of the at least three different height positions of, and/or managing the at least three gas types comprises individual adjustment of the discharged volume flow by gas type, in particular with respect to the discharged volume. , And/or from the at least three different gas types withdrawn from the furnace chamber (11) produce valuable chemicals, in particular methanol, dimethyl ether, olefins, fumanic acid, or synthetic natural gas in further management, The method according to claim 10. The first gas is selectively withdrawn at a first height position within a region 2 m or less below the top of the furnace chamber (11) and additional gas is between 35% and 65% of the height of the furnace chamber. %, more specifically at a further height position within the range of 45% to 55%, another further gas is further heights within a region of not more than 2 m above the bottom of the furnace chamber. 12. A method according to any one of claims 10 or 11 wherein the height of the furnace chamber is selectively withdrawn at a position of at least 4-6 m. 13. At least one of the at least three different gas types withdrawn from the furnace chamber is fed as fuel to a burner (13) that indirectly heats the furnace chamber (11). The method according to any one of 1. A measurement, in particular a temperature measurement, is made at the reversal point (12.21) with the observation site (12.22) in the meandering heating channel on at least one side of the furnace chamber, and/or the adjustment is made to the meandering heating Performed in at least one reversal point (12.21) in the channel, in particular by adjusting slides from the outside, and/or in at least one heating channel, ie at least three horizontal heating channels and above them At least one measurement is made and/or at least one adjustment is made in the sliding block (12.9) in at least one heating channel from the group of one meandering heating channel, in particular at the reversal point (12.21). 14. A method according to any of claims 10 to 13 carried out using. A short circuit or bypass occurs in one or more vertical flow paths (12.5) of the furnace chamber/of the serpentine heating channel, in particular due to the exclusion or blocking of the vertical flow paths, and/or at least for regulation. 15. An adjusting member, in particular an externally actuable sliding block (12.9), arranged in each of the one or more vertical channels (12.5) of the meandering heating channel. The method according to any one of 1. 9. At least one vertical furnace chamber for venting at least three gas types from the furnace chamber for the purpose of establishing a vertical temperature profile in the briquette bed of the furnace chamber, 9. Use of the gas discharge configuration described in paragraph. For the purpose of providing fuel gas to at least one burner that indirectly heats the furnace chamber, the gas discharge arrangement according to any one of claims 1 to 8 causes at least three discharges from the vertical furnace chamber. Use of at least one gas type of gas types. A furnace arrangement (50) for producing coke briquettes, comprising a gas discharge arrangement (30) according to any one of claims 1 to 8 and further a furnace arrangement (10). At least one horizontal heating channel (12.1) on at least one side of the furnace chamber in the lower half, or at least one heating wall in the lower ⅓, and also above at least the upper half or In the middle ⅓ there are provided heating channels (12.2) that meander and extend in a plurality of height planes, each of these heating channels being at least 1 in particular using the gas discharged from the furnace chamber. Furnace configuration, which can be individually heated by two burners (13). A method of producing briquettes from a carbonaceous solid feedstock for not only drying the briquettes made from the feedstock in a briquette dryer, but also coking the briquettes in the furnace chamber (11). Gasification is also carried out in the furnace chamber (11) at at least three height positions, the at least three height positions being distributed over at least half the height of the furnace chamber, the gas being A method for heating a furnace chamber, at least partially through a burner arranged in the furnace chamber, the method being carried out by a furnace arrangement according to claim 18.

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