WO2014056576A1 - Apparatus and method for producing multiple streams of steam or of hot water in a coke oven battery - Google Patents

Description

 Apparatus and method for producing a plurality of steam or hot water streams in a coke oven bank

[0001] The invention relates to a device for producing a plurality of steam or hot water flows in a coke oven bank, which is constructed from a heat exchanger with an integrated exhaust valve and which is arranged on a single coke oven of a coke oven bank, through which the exhaust gas flow rate regulate a coke oven, and at the same time steam can be generated by the heat exchanger. The invention also relates to a method for producing a plurality of steam or hot water streams in a coke oven bank, through which the steam or hot water streams are produced at the individual coke ovens of a coke oven bank of the type "heat recovery" by the exhaust gases of each coke oven through a Heat exchangers are guided, which is equipped with a controllable exhaust valve, so that the exhaust gas streams of the individual coke ovens can be controlled and the exhaust gas pressure can be maintained at a constant value, while at the same time steam generation takes place at each coke oven with a variable amount of steam flow.

The carbonization of coal takes place in the prior art in coke ovens, which are arranged in a coke oven bank or in a coke oven battery. The arrangement of the coke ovens can be done in any number and is made so that can be achieved over the total number of coke ovens over all coking cycles as good as possible equalization of the production of the exhaust gas and the main product coke and by-products. By-products are, in particular, the coking gas and the exhaust gas, which are obtained in different quantities in each coke oven bank or coke oven battery. The coking of coal takes place in coke ovens in cycles, which are formed from the process steps loading - coking and discharge. Depending on the type of coal used, a coking cycle lasts 16 to 192 hours.

When coking arises depending on the type of coal used a certain amount of coking gas, which is collected depending on the type of coke ovens for further processing or burned to heat the coke oven. The further processing of coke oven gas can be useful for various purposes, and requires a regulation of the pressure in the coke oven chamber. The coking gas, in turn, can be further processed into various derived products, including ammonia, hydrogen, hydrocarbons, and sulfur compounds. The heating takes place

CONFIRMATION COPY then with a foreign gas, whereby the coking process can be well regulated. Embodiments for a coke oven with a further use of the coking gas are taught in patents EP649455B1 and DE2654187C3.

In many locations, however, there is no need for the collected coking gas and the derived products, while at the same time want to dispense with heating with a foreign gas for economic reasons. For this purpose, coke ovens can be used, which use the coking gas produced during the coking for heating by the coking gas is burned with supplied air or a supplied oxygen-enriched gas, and is heated by the heat of combustion of coal cake intended for coking. Coke ovens of this type are called "non-recovery" coke ovens and produce after heating an exhaust gas, which can be cleaned of environmentally harmful compounds and released into the atmosphere Coke ovens of the "non-recovery" type teach the patents US4344820A, US4287024A, US5114542A, GB1555400A and CA2052177C.

When operating coke ovens of the type "non-recovery" type, as in the case of the conventional coke ovens, in which the coke oven gas is collected and further processed, the aim is to achieve as uniform a heating as possible of the coal cake intended for coking by For this purpose, when the coke ovens are loaded, the coke oven chamber is only partially filled so that a gas space is left over the coal cake for heating.This gas space is also called the primary heating space.When operating, the primary heating space is subjected to combustion air which is substoichiometric The partially combusted coking gas is then passed over coking gas passages, which in most embodiments are housed in the side walls of the coke oven chambers as so-called "downcomer" channels, into another combustion space below the coke where the partially burned coking gas from the primary heating space is completely burned with an excess amount of combustion air. This combustion chamber below the coke oven chamber is also called Sekundärheizraum. By this stepwise combustion of the coking gas, the coal cake in the coke oven is evenly heated from all sides. To carry out the stepwise combustion of the coking gas in a Primärheizraum and a Sekundärheizraum a controlled air supply is essential. For this reason, in the prior art methods and devices exist to precisely control the access of the combustion air into the primary heating space and the secondary heating space. An embodiment for controlling the entry of combustion air into the primary heating space of a coke oven chamber is taught by WO2010102707A1. A coke oven can have up to 30 primary air openings. An embodiment of the regulation of the entry of combustion air into the secondary heating chamber of a coke oven chamber is taught by WO2010034383A1. A coke oven can have up to 20 secondary air openings. An embodiment for simultaneously controlling the entry of combustion air into the primary and Sekundärheizraum a coke oven chamber teaches WO2007057076A1.

The coking gas is usually carried out after complete combustion in the Sekundärheizraum from this and fed into an exhaust gas collection channel. The exhaust gas thus obtained is discharged at a high temperature, since the coking within the coke oven chamber takes place at temperatures of 800 to 1500 ° C. Since the amount of exhaust gas emitted from a coke oven is substantial over time during coking, and coke oven compartments are typically combined in a plurality of coke oven banks, a significant amount of hot exhaust gas is discharged. For this reason, in most embodiments, to improve the economic performance of a coke oven bank, the sensible heat of the exhaust gas is recovered with a heat recovery unit by conversion to secondary energy. Coke ovens, in which the sensible heat of the exhaust gas is recovered by conversion to secondary energy, are also called "heat-recovery coke ovens." Recovering the sensible heat of the waste gas is particularly worthwhile if several coke ovens are combined to form a coke oven bank.

Coke ovens of the type "non-recovery" or "heat recovery", which are combined in a plurality, are also called coke oven banks. Coke ovens of conventional type, which are grouped together, are also called coke oven batteries. The discharge of the exhaust gas from a coke oven of the "non-recovery" or "heat-recovery" type is typically carried out by an exhaust gas duct, which carries out the completely burnt exhaust gas from the secondary heating chamber and leads into an exhaust gas collecting duct. Embodiments of coke oven banks for recovering the sensible heat of the exhaust gas are known in the art. US 5968320A describes a device for transporting and combusting a coke oven raw gas under reduced pressure in order to extract steam from the combustion energy, the device consisting of ordinary coke ovens with exhaust ducts leading into an exhaust gas collection duct where the coke oven gases are cooled by a liquid treatment, and led to a boiler with burner, where they are burned, and the burned exhaust gases are then sucked by applying a set negative pressure from the boiler, and in this way steam is generated, which can be used to generate electrical energy.

DE3701875A1 describes a method for generating electrical energy wherein the coal is heated in a regeneratorless coke oven with a coking chamber and with a gas line leading to a heating train below the coking chamber while maintaining a negative pressure in the coking chamber, and wherein air is introduced into the coking chamber and in the gas line only in such an amount that a reducing atmosphere is maintained not only in the coking chamber, but also in the heating train, further containing the flammable substances containing hot combustion gases from the heating train in an exhaust gas combustion chamber, in which the combustible substances are burned with excess air at a temperature which minimizes the formation of nitrogen oxides from nitrogen oxides constituents contained in the combustion gases, and the hot combustion gases which have been desulphurized to a steam boiler unit be passed in which steam generated by heat transfer from the combustion gases to feed water and this steam is used to generate electrical energy, after which the exhaust gases are discharged into the atmosphere.

The recovery of the energy from the sensible heat of the exhaust gas of a coke oven bank is carried out in most cases by a steam boiler. The coke oven gas can also be completely burned in the coke oven and fed into a steam boiler to recover the heat. For this purpose, the completely combusted exhaust gas from the secondary heating chambers of the coke ovens is carried out via an exhaust gas line and introduced into an exhaust gas manifold, which leads the exhaust gases into the steam boiler. Afterburning is not absolutely necessary here. The exhaust manifold is usually equipped with cross sections up to 20 m ² and is usually provided with a correspondingly thick insulating layer to keep the heat loss of the hot exhaust gas on the way to the boiler low. The distance between see Koksofenbank and heat exchanger can be up to 60 meters in the prior art, and under or crosses the coke oven operating machines, which is why a corresponding heat loss must be counteracted. Temperature loss values of more than 100 ° C often have to be taken into account. In the utilization of the sensible heat of the exhaust gas, it is a problem in many cases that the coking is carried out cyclically, so that the exhaust gas is provided during the operation of a coke oven only during coking. In the remaining process steps during loading and unloading, there is no production of hot exhaust gas. As a result, the production of hot exhaust gas in the amount is not consistent. This is particularly a problem when generating steam from the hot exhaust gas which drives a turbine to produce secondary energy since it must be supplied with a steady stream of vapor. There are therefore in the prior art process steps which have a homogenization of the exhaust gas flow rate even with uneven exhaust gas generation by cycle change or malfunction of a coke oven bench to the destination.

[0013] WO2011054421 A1 describes a method for compensation of flue gas enthalpy losses of "heat recovery" coke ovens, wherein a plurality of coke oven chambers are combined to form a coke oven bank, and the coke oven bank are connected to one or more boilers via a flue gas channel or via flue gas channels wherein the operation of the coke oven chambers is periodically interrupted by removing the coke cake, and the individual coke oven chambers are kept warm during the interruption of operation with at least one externally fired auxiliary burner, so that a hot flue gas is also provided during the interruption of the operation the flue gas of the auxiliary burner comes, and the reduced compared to normal operation heat flow is compensated by at least one additional compensation burner, which is outside the coke oven chambers, so that the one or more boilers with a constant compared to the normal operation Heat flow to be supplied. In this way, the boilers, which are typically used for the production of steam, can be operated economically.

In the equalization of the exhaust gas flow for an economical operation of the boiler, the operator of a coke oven bank is often inclined to control the driving of the coke oven chambers so that a uniform generation of exhaust gas takes place to avoid problems in the operation of the steam turbine. This is especially then a problem when the air supply is controlled in the individual coke oven chambers with the aim of achieving the most uniform possible production of exhaust gas. Thereby combustion is not optimally controlled because the further supply of combustion air, while increasing the amount of exhaust gas expelled, does not directly affect the combustion of coking gas, since it also depends on the amount of coking gas discharged, which in turn depends on coking. The operator does not regulate the supply of air to the coke oven with the desired aim of controlling the coking in order to maintain a good coke quality, but substitutes and forcibly regulates the air supply to control the exhaust gas production and thus the steam production.

The combustion air can control the heat generation in a coke oven only conditionally, since this has a cooler temperature than the coke oven gas at the initiation, and must be fully heated before combustion only in the coke oven, and the combustion of the ejected amount of coking gas depends. The ejected amount of coking gas in turn varies considerably over time, which in turn leads to uneven exhaust gas flow rates. It is therefore not possible, as desired, to influence coking and coke quality by controlling the combustion air supplied to a coke oven.

For the operator of coke ovens and coke oven benches, therefore, a method which regulates the exhaust gas volume flow without influencing the air inflow into a coke oven chamber would be very helpful, and at the same time a constant volume flow of steam which is independent of coking in the coke ovens the turbine ensures. For this purpose, it is naturally necessary to be able to regulate the exhaust gas flow rate and to be able to keep the same amount in order to provide a uniform amount of steam, depending on the exhaust gas temperature. Also, the steam generation should be made as directly as possible to the coke ovens in order to better influence the amount of steam produced and to avoid the high temperature losses of the exhaust gas on the flow path to the boiler.

There is therefore the object to provide a device which performs a regulation of the exhaust gas flow rate after the exit of fully combusted exhaust gas from a single coke oven, and at the same time uses the hot exhaust gas of the coke oven directly, a steam flow rate in an integrated heat exchanger to create. As a result, the regulation of the exhaust gas flow rate is performed as the actual controlled variable, so that it can remain constant, and the air supply into the Coke oven concerned can only be geared to the needs of coking and thus to the coke quality provided. As a side effect is obtained by the integrated heat exchanger, a constant steam flow rate, the value of which is influenced only by the temperature of the exhaust gas. The invention solves this problem by a device which consists of a heat exchanger which is arranged in the exhaust passage between the Sekundärheizraum and Abgassammeisystem a single coke oven, which forms a device for emitting the heat of the exhaust gas to feed water by indirect heat exchange , And in the gas flow direction behind the heat exchanger, a valve for metering or blocking the exhaust duct is arranged, which is associated with a single coke oven. Each individual exhaust valve thus has an integrated heat exchanger.

A positive aspect of the present invention is that the steam flow rate compared to the conventional procedure is comparatively greater, since the exhaust gas experiences no loss of temperature in the lines by the direct steam conversion at the furnace without transport through lines. A further advantage of the present invention is that the steam lines through which the exhaust pipes pass are lower than the exhaust gas temperature due to the lower steam temperature, which results in cost advantages in the construction of a system equipped therewith. The method can be further adapted by providing a buffer for the steam, so that even in case of malfunction or failure of a coke oven chamber, a further constant amount of steam for the turbine can be ensured, and the coke oven chambers independently in the air supply for optimal Coke quality are controllable. The exhaust gas is passed after passing through the heat exchanger in an exhaust manifold. Since the device according to the invention also serves for the provision of secondary energy from steam, the device according to the invention also includes a feed water line, which serves for supplying feed water to the heat exchanger of the coke oven, and further a steam line, which serves for the removal of the steam passing through the heat exchanger is generated, and which leads into a vapor manifold, and a conversion unit of the heat energy of the steam from the vapor manifold in secondary energy. The latter is, in most cases, a steam turbine with generator for generating electrical energy, although also exemplary Turbine for recovering mechanical energy for driving auxiliary equipment is conceivable.

The invention solves this problem also by a method for metering the exhaust stream from a coke oven, which is measured by the method, the exhaust pressure at the entrance of the exhaust pipe in the heat exchanger, so that the exhaust gas pressure at each coke oven chamber at least temporarily adjusted to a constant value is generated, and the fully burned exhaust gas in response to the supplied exhaust gas flow a constant amount of steam, which is fed into a vapor manifold. After passing through the steam manifold, the steam is delivered to a conversion unit for generating secondary energy, so that the steam quantity, since at least temporarily a constant exhaust gas flow rate is set, with the assumption of a constant exhaust gas flow at the same temperature at the corresponding coke oven also remains the same. As a result, exhaust control and steam production can be decoupled. In contrast to the prior art, the steam is no longer produced on a single steam boiler for a coke oven, but at each coke oven, at the same time a control of the exhaust gas flow is performed on each coke oven, so that the amount of steam over all coke ovens at least at times remains the same. At the same time, the reduced heat loss provides an increased amount of steam compared to the prior art. Although it would be possible to carry out steam generation on each individual coke oven even without controlling the exhaust gas flow, this is generally undesirable because there is no consistent vapor flow rate.

In particular, a device is claimed for producing a plurality of steam or hot water flows in a coke oven bank, comprising

A coke oven of the "heat recovery" type, which is arranged in a coke oven bank, and with a coke oven chamber, a gas space arranged therein which forms a primary heating space in the loaded state, a coke oven chamber ceiling, coke oven chamber doors, primary air openings for the primary heating space, and a secondary heating space, which is located below the coke oven chamber and which contains secondary air openings, is equipped, A loading and unloading system for the coke oven, which is intended for loading the coke oven chamber with the coal cake intended for coking, and for discharging the finished coke cake for the extinguishing process,

 An exhaust duct which connects the secondary heating chamber to an exhaust gas collecting system, which releases the exhaust gas to the atmospheric environment after heat exchange and a required exhaust gas purification, and which is characterized in that

• Between the Sekundärheizraum and the Abgassammeisystem in the exhaust passage, a heat exchanger is arranged, which forms a device for discharging the heat of the exhaust gas to feed water by indirect heat exchange, and which is associated with a single coke oven, and

• In the gas flow behind the heat exchanger, a valve for metering or blocking the exhaust duct is arranged, which is associated with a single coke oven, and which is controllable by means of pressure probes in the exhaust duct, and the exhaust duct opens behind the valve in an exhaust manifold, and

 • There is a feed water line which serves to supply feed water to the heat exchanger of the coke oven, and a steam line, which serves to remove the steam generated by the heat exchanger, and which leads to a vapor collecting line, with which the transported away steam is continued , and

 • a unit of heat energy conversion of steam from the steam manifold to secondary energy.

In one embodiment of the invention, the coke oven bank is from 6 to 30

Coke ovens built. Theoretically, it is conceivable to equip a coke oven with the device according to the invention. In this case, however, no steam would be produced during the process of loading and unloading from the coke oven, since there would be no exhaust gas available during this process and steam generation would be interrupted. This is not wanted. For this reason, the device according to the invention is used in particular in coke oven benches with at least 6 to 30 coke ovens. To operate the coke oven, each individual exhaust valve, since it contains an integrated heat exchanger, supplied with feed water from a feedwater manifold and be provided with an exhaust steam line, which leads into a steam manifold. These lines are arranged along the coke oven bank in a typical embodiment.

In one embodiment of the invention, at least one heat exchanger for a single coke oven, a feedwater line and a steam manifold is arranged on only one frontal side of a coke oven of Koksofenbank. In one embodiment of the invention, at least one heat exchanger for a single coke oven, a feedwater line and a steam manifold is arranged on both frontal sides of a coke oven of the coke oven bank. For each coke oven, two heat exchangers with integrated exhaust valve are available.

In a further embodiment of the invention, at least one heat exchanger is arranged in a coke oven bank on the ceiling of the coke oven chamber. This embodiment makes sense, in particular, when the loading of the coke oven chamber takes place through the frontal doors of the coke oven chamber. This saves space on the front sides of the coke oven, which is required for loading, while the free space on the ceiling of the coke oven can be used. An embodiment for the loading through the coke oven chamber doors is taught by WO2010102708A2. In a further embodiment of the invention, the exhaust valve with the integrated heat exchanger is arranged in a trough in the Koksofenfundament before the coke oven. In turn, this saves space on the coke oven chamber ceiling when loaded through the coke oven chamber ceiling. An embodiment for the loading through the coke oven chamber ceiling is taught by WO2009106251 A1. To carry out the invention, it is advantageous to construct the heat exchanger so that they make an optimal indirect heat exchange between exhaust gas and feed water. Inside, the heat exchanger is equipped, for example, with a tube bundle through which water can flow, with plate elements through which water can flow, or with rib elements through which water can flow, which can be arranged simply or multiply. The embodiment to be selected depends in particular on the flow cross-section and the geometric shape of the heat exchanger in order to ensure the best possible heat exchange.

The flow-through type of the exhaust gas through the heat exchanger is also selected so that the flow-through mode optimally exchanges heat between see exhaust gas and feed water for steam generation guaranteed. The exhaust gas may also change its direction several times within the heat exchanger. For example, it is possible for carrying out the invention to use a heat exchanger which operates in the indirect heat exchange between the feed water and the exhaust gas according to the counterflow principle, the cross flow principle, the DC principle or a combination of these flow principles. The heat exchange coils within the heat exchanger are then arranged so that the respective flow principle is performed, wherein the arrangement of the pumps and valves for the feed water is then carried out so that the respective flow is carried out. To construct the present device, it is necessary to provide both the exhaust valve with heat exchanger and the laxative steam lines with an efficient insulation. In this way, the steam flow, which according to the invention must be conducted from each heat exchanger into the common steam manifold of the coke oven bank, can be well protected against heat losses. Insulation materials which are suitable for this purpose are well known to the person skilled in the art for the construction of coke oven plants. The elimination of control devices on long exhaust pipes also eliminates the disadvantageous intake of atmospheric air into the exhaust pipes, which often occurs due to elongation processes in long exhaust sections.

It goes without saying that the device according to the invention must also be resistant to high temperatures, since the arrangement of the heat exchanger according to the invention takes place in the immediate vicinity of the coke oven chamber in most cases. The temperatures in the immediate vicinity of the coke oven chambers are up to 1000 ° C. The exhaust manifold at the end of the Sekundärheizraumes for entry into the exhaust duct may consist of refractory bricks, steel or cast iron. All components of the heat exchanger must be made of a material which is resistant to water vapor on the water side and to hot exhaust gas with corrosive gas components on the exhaust gas side. This is a high-temperature resistant stainless steel in most embodiments, but in principle all resistant materials are suitable for this purpose. In one embodiment of the invention, the heat exchanger is equipped on the exhaust side to the inside of the exhaust pipe with a heat-resistant shell, which consists of at least one insulating layer, and which is secured with an anchor construction on the inner wall of the exhaust pipe. As a result, both good temperature resistance and good thermal insulation of the device according to the invention can be achieved. The construction of the valves themselves, which are arranged within the exhaust valves, may be arbitrary, but must have a sufficient temperature resistance to the hot exhaust gas. In one embodiment of the invention, the valve, which is integrated in the heat exchanger, a flap, a slide or a tap. This must be made of a heat resistant material to be durable. Suitable materials are, for example, high temperature resistant stainless steel, enamel, silicon carbide, corundum, fiber materials, alumina materials, copper, glass, silica, refractory ceramics or pieces of chamotte. The housing can be made of steel or cast iron, for example. The drive of the exhaust valves and the other valves must be temperature resistant. This must also be remotely controllable. In one embodiment of the invention, the exhaust valve is driven by an electrically driven engine. In a further embodiment of the invention, the exhaust valve is driven by a pneumatically or hydraulically operated engine. The control of the exhaust valve can ultimately be arbitrary, as long as it is reliable at the applied high temperatures. The controller preferably has a short reaction time to allow reliable control of the exhaust stream, so that a constant and constant exhaust pressure can be ensured at the end of the exhaust pipe. The control of the exhaust valve is heat-protected in an advantageous embodiment, since it is arranged in the vicinity of the hot coke oven. The heat protection can be done for example by installing at least one thin heat shield on the drive.

The supply line of the feed water into the heat exchanger, in which the exhaust valve is integrated according to the invention, and the export line for the steam can also be regulated in one embodiment of the invention so that the supply of feed water and the steam removal can be regulated if necessary , However, this is usually not used during operation, since the steam production is to depend on the exhaust gas flowing through, and thus depends only on the temperature of the exhaust gas at a constant exhaust gas flow rate. As a rule, therefore, a constant supply of feedwater and unregulated steam discharge are selected. In a further embodiment of the invention, a pitot probe for pressure measurement or a pressure gauge for measuring pressure in the exhaust gas are arranged in the exhaust pipe, which leads through the heat exchanger. This embodiment is used in almost all embodiments since an important goal is to provide a consistent exhaust pressure. It is also possible to carry out the pressure measurement with devices which do not fall under the mentioned embodiments. These must be but be stable at the temperatures used and can make a reliable pressure measurement.

Often it is also useful to measure the temperature or measurement of the

To carry out oxygen content in the exhaust gas in order to obtain information about the progress of the coking or the combustion of the coking gas. For this purpose, in the context of the invention in the exhaust gas channel, which leads through the heat exchanger, a thermocouple or a lambda probe for measuring the oxygen content may be arranged. Also, a probe for measuring other gas components may be disposed in the exhaust passage. All measuring devices are then used to determine the corresponding measured values and subsequently to regulate the exhaust gas flow.

At the exhaust pipe from the Sekundärheizraum a coke oven in the

Exhaust duct, which is equipped with the heat exchanger with the integrated exhaust valve, an auxiliary burner may be arranged, which performs an adjustable fuel line temporarily and with controllable power, an additional heating of the exhaust gas. This can be simple or even multiple. This may be present on one or more coke ovens. This makes it possible to carry out a further heating of the exhaust gas, so that in addition to the pressure of the exhaust gas, which is controlled by the exhaust valve, and the temperature of the exhaust gas can hold at a constant value. This makes it possible to further homogenize the steam production.

Since the heat exchangers must be supplied to the coke oven chambers with feed water, each heat exchanger must be connected to a feedwater manifold. This can be arranged anywhere within the coke oven bank. The feed water line supplies the heat exchangers in an advantageous embodiment via a water pump with feed water, and can be regulated or metered via a valve. In exceptional cases, a feed water line is conceivable, which carries out the promotion by a level difference promotion or convection promotion.

The exhaust ducts advantageously lead into an exhaust manifold, which serves to discharge the exhaust gases from the exhaust ducts. The steam pipes of the heat exchangers advantageously lead into a steam manifold for the removal of the steam from the heat exchangers. In a further embodiment, the vapor collection line between the heat exchanger and the conversion unit contains expandable or shrinkable intermediate pieces with which the temperature expansion of the vapor collection unit buffers. This lowers the operating costs of a coke oven bank or coke oven plant, as it requires much less frequent replacement of the vapor manifold, which otherwise undergoes frequent repair changes due to thermal expansion. The so-equipped steam manifold is insulated in a preferred embodiment. The steam manifold is provided in a preferred embodiment of the invention with a steam drum with which the steam can be stored. This serves, in particular, to provide the unit for converting the steam into secondary energy, which in most embodiments is a turbine, with a further uniformized vapor flow. The steam production in a coke oven depends not only on the amount of exhaust gas, but also on the temperature of the exhaust gas. In addition, the distribution of coking cycles across all coke ovens often deviates from the ideal distribution. With the steam drum, the turbine can be supplied with a constant steam flow at all times. For this purpose, the steam drum contains regulating and metering devices as well as pressure measuring devices for the steam flow. In one embodiment of the invention, the vapor manifold is disposed on at least one side of the coke oven chamber front and along the coke oven chamber front below the service platforms. In a further embodiment of the invention, the steam manifold is recessed into at least one side of the Koksofenkammerfront before and along the Koksofenkammerfront in the ground. This can also run parallel to the feed water line or to the exhaust manifold. The steam manifold can also be placed on the furnace roof of the coke oven bank.

If the coke oven bank, which contains coke ovens with the heat exchangers according to the invention, equipped with auxiliary burners, they are supplied in an advantageous embodiment with a manifold, which is connected to each auxiliary burner of the coke oven bank, with fuel. As a rule, the fuel is a hydrocarbon-containing fuel and, in the majority of cases, natural gas or liquid petroleum gas (LPG). In one embodiment of the invention, at least one coke oven chamber front for at least one auxiliary burner runs along a gas line In one embodiment of the invention, the exhaust manifold, the vapor manifold, the feedwater manifold and the gas line for the auxiliary burners or at least one of these conduits run in parallel along the coke oven chamber front.

It has already been mentioned that sometimes also a regulation of the feed water flow into the heat exchanger or the discharged vapor stream is required. It can be borrowed, which lead to and from the heat exchanger, in which the exhaust valve according to the invention is integrated. However, this is only the case in exceptional cases. In these cases, temperature sensors or pressure gauges can also be arranged in the feedwater feed line or in the steam discharge. With the measured values thus obtained, the control of the feedwater flow in the heat exchanger or the discharged vapor stream are then performed.

To carry out the invention are almost always temperature and

Pressure measuring devices in the vapor manifold, which serve to remove the vapor from the individual steam lines, for use, since they are essential for controlling the vapor pressure at the means for obtaining the secondary energy, usually a turbine. Prior to the establishment of the secondary energy, additional facilities for measuring and controlling the steam temperature and the vapor pressure can sit.

In a further embodiment of the invention, a closable blind stub is arranged in the exhaust pipe, which leads through the heat exchanger, which serves for the use of a mobile measuring device for measuring the temperature, the pressure or for measuring at least one gas component in the exhaust pipe. This is used to carry out a temporary measurement of the temperature, the pressure or at least one gas component. For this purpose, a mobile measuring device is used, which is temporarily inserted into the closable blind stub. This is preferably from the nozzle diameter DN20 to DN50 ("Diameter nominal" according to EN ISO 6708, under DN a nominal size according to DIN standard is understood.) The obtained values can be used by way of example, in order to permanently adjust one or more additional control valves for controlling the Exhaust flow in an exhaust valve.

In a further embodiment of the invention, a cleaning line for steam or compressed air is arranged in the exhaust pipe in front of or behind the exhaust valve. This allows the heat exchanger with the integrated exhaust valve during operation to be easily cleaned. For this purpose, the line is designed in an exemplary embodiment to a cleaning pressure of between 5 and 100 bar. Cleaning devices based on the sound principle can also be used. A discharge line can also be arranged on the heat exchanger with which excess steam or wastewater can be drained from the heat exchanger into a discharge line for discharge water and into a container. This is useful for the case where condensate has formed in the exhaust valve. This can also be done during operation. be drained. The drain line can also be regulated or automated controllable.

Also claimed is a method which is used to operate the device according to the invention, and which allows a constant exhaust gas pressure at each coke oven and a decentralized steam generation in a coke oven bank.

In particular, a method is claimed for producing a plurality of steam or hot water streams in a coke oven bank, wherein

 • a number of 6 to 30 "heat recovery" coke oven chambers are assembled into a coke oven bank, and

 The coal is heated to high temperatures by cyclic coking, one cycle consisting of loading, coking and discharging, coking the coal in the coke oven chamber where the coking gas is mixed with a portion of combustion air in a primary heating space a gas space is formed in the coke oven chamber, is stoichiometrically burned, and the partially burned coking gas is passed through arranged in the sides of the coke oven chamber exhaust ducts in Sekundärheizräume below the coke oven chamber, where this is completely burned with a superstoichiometric amount of combustion air,

 and which is characterized in that

 • The completely burned exhaust gas from the Sekundärheizraum a single coke oven chamber is passed through an exhaust passage in a heat exchanger with integrated controllable exhaust valve, so that the exhaust gas flow rate, which flows through the heat exchanger, is adjustable, and

The exhaust gas pressure at the inlet of the exhaust gas channel into the heat exchanger is measured, so that the exhaust gas pressure at each coke oven chamber is at least temporarily set to a constant value via the exhaust valve, and

The fully burnt exhaust gas in the heat exchanger generates a quantity of steam, which is fed into a vapor manifold, and is delivered to a secondary energy conversion unit after passing through the vapor manifold, depending on the exhaust gas flow supplied; the completely burned and cooled exhaust gas is passed, after passing through the controllable heat exchanger in an exhaust manifold, from which the exhaust gas is used or released into the environment.

By this procedure, the exhaust gas flow rate and the exhaust pressure can be maintained at a constant value, this constant value is naturally subject to slight fluctuations, but far from fluctuating to the extent, as is the case in the case of a coke oven without regulated exhaust gas flow is. The measurement of the pressure can only take place at the inlet of the exhaust gas channel into the heat exchanger, but can also take place both at the inlet and at the outlet of the exhaust gas channel at the heat exchanger.

By regulating the exhaust gas flow and the steam flow rate can be maintained at a constant value, which is subjected to somewhat larger fluctuations compared to the exhaust gas volume flow, since this is influenced by the heat exchange. The steam line is usually isolated to achieve low heat loss during transport of the steam. In one embodiment of the invention, the steam flow rate at each coke oven is set by controlling the exhaust gas flow to a value of 300 kg / h to 3000 kg / h. The steam is obtained here on one side of the coke oven.

It is also possible to generate the steam on two sides of the coke oven bank. The amount of steam recovered is then slightly lower, since the amount of heat of the exhaust gas in a single coke oven is not different from the amount of heat provided on one side of steam production. In one embodiment of the invention, steam is generated on at least one coke oven on two sides of the coke oven, wherein on each side of the coke oven, the steam flow rate is adjusted by regulating the exhaust gas flow to a value of 150 kg / h to 2850 kg / h.

The temperature in the exhaust gas is at the inlet of the exhaust pipe in the heat exchanger measurements between 850 ° C and 1550 ° C and after exit between 170 and 800 ° C and preferably at about 180 ° C. The exhaust gas volume flow is usually 1000 Nm ³ / h to 6000 Nm ³ / h. In one embodiment of the invention, the supply of water to the feed water can be regulated in the heat exchanger. As a result, the amount of steam generated can also be adapted to the temperature of the exhaust gas, although the amount of steam is already reasonably consistent with a constant regulation of the exhaust gas flow. For this purpose, the temperature at the inlet of the exhaust pipe is measured in the heat exchanger and regulated the water supply in the heat exchanger based on these measurements, so that the Steam generation in dependence on the temperature in the exhaust gas takes place. This also prevents the steam generator from possibly evaporating or no longer providing steam due to excessive water supply. For this purpose, it is also possible in one embodiment of the invention to provide a level control for the feed water in the heat exchanger.

In one embodiment of the invention, an auxiliary burner is arranged in the exhaust pipe of the heat exchanger, through which can increase and regulate the temperature in the exhaust gas before flowing through the heat exchanger. As a result, the temperature in the exhaust gas can also be kept constant, so that, given a constant amount of exhaust gas flow, only by the feedwater feed, even without further regulation of the feedwater or steam, a virtually constant steam flow rate is obtained. The regulation of the auxiliary burner takes place in an advantageous embodiment on the basis of the measured values for the temperature in the exhaust gas. The auxiliary burner can be operated with any heating gas, but is preferably operated with natural gas, a liquid gas (LPG, "liquid petroleum gas") or a coal pyrolysis gas.

The temperature in the exhaust gas is here after increasing the temperature through the auxiliary burner and by measuring and regulating the temperature at the inlet of the exhaust pipe in the heat exchanger between 850 ° C and 1550 ° C. After flowing through the heat exchanger this still has a temperature of about 175 ° C to 250 ° C. The feed water is advantageously supplied at a temperature of 10 to 170 ° C and has a pressure of 1 to 140 bar. The steam generated at the heat exchanger then has a temperature of 120 to 600 ° C, and in another embodiment 350 to 520 ° C, and is under a pressure of 5 to 130 bar, and in another embodiment under a pressure of 70 to 1 10 bar. This steam is then routed to the steam manifold and used to generate secondary energy. The temperature and pressure values of the steam may change slightly during transport to the secondary energy generating unit, and in particular depend on the insulation of the steam pipe and steam manifold and the cross sections and branches of the pipes used. It is also possible, by the heat exchanger according to the invention with

Provide exhaust valve hot water. This can be used, for example, for the auxiliary units of the coke oven bank. For this purpose, hot water with a temperature of 40 to 120 ° C is generated, for example, in at least one heat exchanger instead of steam. This can also be under pressure. In order to control the heat exchangers and the exhaust valves integrated therein, an automated control device is advantageously used, since a large number of measured values and control signals have to be processed in order to control the exhaust valves in a coke oven bank. The control of the valve for the exhaust gas in the heat exchanger is then carried out by means of the measured values for pressure in the exhaust gas channel by a computer. A control of the system by a computer is particularly suitable in the processing of other control signals, such as the temperature in the exhaust duct and the operation of auxiliary burners.

After passing through the heat exchanger and after regulation in the exhaust valve, the exhaust gases are supplied through an exhaust manifold for further use or disposal. These have after the heat exchange only a non-usable heat of at most 180 ° C and are cleaned in almost all cases and discharged in a harmless form with a temperature of about 80 ° C in the atmosphere. For exhausting the exhaust gases in the exhaust manifold, a negative pressure is expediently provided for this purpose by suction with an exhaust gas suction fan.

The recovered steam or the recovered hot water can be used to obtain the secondary energy as desired. The conversion unit in secondary energy is in one embodiment of the invention to a turbine and a generator and the secondary energy to electrical energy. The device according to the invention and the method according to the invention have the advantage of keeping the exhaust gas flow of a coke oven at a constant pressure value and thus constant, so that the air supply into the coke oven can be controlled largely independently of the pressure prevailing therein, and thus the course the coking can be controlled only by the amount of supplied primary and secondary air. As a further effect, an almost constant vapor flow is obtained at each coke oven as a function of the exhaust gas temperature during the coking, so that viewed over the entire coke oven bank receives a very uniform vapor stream, and the generation of secondary energy is thereby considerably simplified. As a result, the economic result of the coke oven plant can be substantially improved, and the quality of the coke produced can be increased.

The invention will be explained in more detail with reference to five drawings. The drawings represent only exemplary embodiments, which are not limited to these. 1 shows a heat exchanger according to the invention with integrated exhaust valve. FIG. 2 shows an embodiment of the heat exchanger in which Exhaust pipe a foreign-fired auxiliary burner is present. 3 shows a coke oven bench from the prior art, which is equipped with a central steam generation. 4 shows a coke oven bank comprising four coke ovens in a vertical view from above, which are equipped with the heat exchanger according to the invention for decentralized steam generation. FIG. 5 shows the exemplary arrangement possibilities of a heat exchanger according to the invention on a coke oven.

FIG. 1 shows a heat exchanger (1) according to the invention with integrated exhaust valve (2). The coke oven chamber (3) is arranged on the right side and provides a hot exhaust gas flow (4). This enters the exhaust duct (5) and, after measuring the exhaust pressure through a pressure measuring probe (6), passes through a heat exchanger (1) with heat exchange coils (1a). The heat exchanger (1) has a controllable feedwater supply (1 b), which is controlled by a valve (1 c), and an unregulated steam discharge (1 d). After passing through the heat exchanger (1), the exhaust gas (4) flows into an exhaust valve (2). The heat exchanger (1) is provided in the gas flow direction in front of the exhaust valve (2) with a supply line (7) for steam (7a) under pressure. The supply line (7) can be shut off (7b). This allows the heat exchanger (1) to be cleaned at certain intervals. The heat exchanger (1) is in the gas flow direction (8) in front of the exhaust valve (2) also provided with an export line (9) for condensed water (9a), which from the steam (7a) for cleaning or coke oven gas, depending on the coal quality also small amounts of water (9a) may contain condensed out. The condensed water (9a) is discharged via a line (9b) with valve (9c) at periodic intervals. After flowing through the heat exchanger (1), the exhaust gas (4) flows through an exhaust valve (2). This regulates the exhaust gas flow (4) so that the exhaust gas pressure remains at the same value at least temporarily after flowing through the exhaust gas valve (2). The exhaust valve (2) is formed by a rotatable flap (2a) with servomotor (10). The export of the exhaust stream (4) takes place in an exhaust manifold (11), which is under a slight negative pressure of about -50 mbar. The control of the exhaust valve (2) via a computer control (12), which communicates via a control line (12a) with the pressure measuring probe (6) and the servo motor (10). FIG. FIG. 2 shows an embodiment of the invention in which an externally fired auxiliary burner 13 is arranged in the exhaust pipe 5 through which further exhaust gas temperature homogenization is carried out and the exhaust gas 4 can be kept warm when it interrupts the operation of the engine upstream coke oven (3a) comes. As a result, even during the interruption of the operation, a The exhaust gas (4) provided. The auxiliary burner (13) is supplied with a fuel gas via a gas line (13a), which can be controlled via a valve (13b).

Shows a coke oven bank (14) from the prior art, in which the exhaust gas (4) of the individual coke oven chambers (3) is collected and fed via a metering in an exhaust duct (5). From the exhaust duct (S), the exhaust gas (4) via an exhaust manifold (11) and a branch (5a) in a common heat exchanger (15), which uses the heat of the exhaust gas (4) for generating steam (15a). The inlet of the exhaust gas (4) into the heat exchanger (15) via control valves (16), which in the gas flow direction between the branch (5a) from an exhaust gas collection line (11) in the channel to the heat exchanger (15) and in front of the heat exchanger (15) sit. These are often gas-permeable to a small extent in the prior art in order to allow an expansion tolerance at the prevailing high temperatures in the lines (5,11). As a result undesirable air (17) from the atmosphere enters the lines (5,11). After flowing through the heat exchanger (15), the exhaust gas (4) is passed into an exhaust gas purification system (18), which is for example a gas scrubber for desulfurization, and via an exhaust fan (19), which generates a slight negative pressure in the exhaust manifold (11) , sucked into a flue (20). At the branch (5a) of the exhaust manifold (11) in the channel to the heat exchanger (15) sits a shut-off valve (5b), with which the heat exchanger (15) can be shut off from the coke ovens (3a). This is necessary in case of failure of the heat exchanger (15) or in the repair of a coke oven (3a), if it comes due to repair interruption of the supply of hot exhaust gas (5a), and the heat exchanger (15) must be taken out of service. When the coke ovens (3) of the heat exchanger (1) are shut off, the exhaust gas (4) flows through an emergency chimney (21). In front of the coke ovens (3), a movable coke breeze (22) is arranged, with which a pick-up of the hot coke (22a) and a transport to an extinguishing device (not shown) can be made. The recovered steam (15a) serves to drive a turbine (23) and, after passing through the turbine (23), is condensed in a condenser (24) and returned to a feedwater tank (26) via a pump (25a) after cleaning (25) , The turbine drives a generator (27) for the production of electrical energy.

Shows an arrangement of four coke ovens (3a), which are equipped with a heat exchanger according to the invention (1) with exhaust valve (2). The coke oven chambers (3) are combined to form a coke oven bank (14) and are loaded with a carbon cake (29) via a coke oven operating machine (28), which is connected to an entry punch (28a). You can also see the coke oven chamber doors (30) and the ventilation openings (31) for the inlet of primary air on the ceiling (32) of the coke oven chambers (3). On the other side of the coke oven chambers (3), a coke quencher (22) is moved along the coke oven chamber front (3b) with which the coke (22a), which is expressed from the coke oven chambers (3), is received and discharged into a quenching device (not shown) can be moved. From the Sekundärheizräumen (3c), the exhaust gas (4), which is completely burned, flows into the heat exchanger (1) according to the invention. Thereby, steam (1a) is generated, which is discharged into a vapor collecting pipe (33), and then supplied to a converting unit in secondary energy. The heat exchanger (1) is supplied with feed water via a feedwater line (1b) which can be controlled by valves (1c) from a feed water collecting line (34). The exhaust gas (4) passes through the heat exchanger (1) and is maintained after passing through the heat exchanger (1) by an exhaust gas control valve (2) at a constant pressure. This is measured by pressure measuring sensors (6) in front of and behind the exhaust valve (2) and controlled by a computer control (12) and control lines (12a) through the exhaust gas control valve (2).

Shows the possible arrangement of the heat exchanger (1) with the exhaust valve (2). The coke oven chamber (3), which is loaded with a coal cake (29), and the primary heating chamber (3d) located above the coal cake (29) can be seen. Under the coke oven chamber (3) is the Sekundärheizraum (3c). The partially combusted exhaust gas is completely burned in the secondary heating chamber (3c). The completely combusted exhaust gas (4) is led out of the secondary heating chamber (3c) into the heat exchanger (1) with exhaust valve (2). In one embodiment (A), the heat exchanger (1) is arranged at the level of the ground to the right of the secondary heating chambers (3c) of the coke oven chambers (3). This can be done to one side, to the right or to the left or to both sides of the coke oven chamber (3). In a further embodiment (B) of the invention, the heat exchanger (1) with the integrated exhaust valve (2) below the ground (35) is also arranged next to the coke oven chamber (3). This can be done on the right or left of the coke oven chamber (3) or on both sides of the coke oven chamber (3). In a further embodiment (C) of the invention, the heat exchanger (1) is arranged on a carrying device (36) above the coke oven chambers (3). This can be done on the right or left or on both sides of the coke oven chamber (3). In a further embodiment (D) of the invention, the heat exchanger (1) is arranged on the ceiling (32) of the coke oven chamber (3). This can be done on one or more coke oven chambers (3) of a coke oven bank (13). In a further embodiment (E) of the invention, the heat exchanger (1) is arranged below a coke oven chamber (3) below the earth level (35). This can be found in the foundation of a coke oven chamber (3) or in front of the coke oven chamber (3) in a corresponding tub (37) done. The manifolds (11, 33, 34) for the feed water (1 b), the steam (1 d) and the exhaust gas (4) can also be arranged as desired, but must supply all the heat exchangers (1) with feed water and the exhaust gas (4). and remove the steam (1d). The lines (11, 33, 34) are preferably arranged parallel to the coke oven chambers (3).

[0066] List of Reference Numerals

 1 heat exchanger

 1 a heat exchange coils

 1 b Feedwater supply

 1 c feed water valve

 1 d steam removal

 2 exhaust valve

 2a flap in exhaust valve

 3 coke oven chamber

 3a coke oven

 3b coke oven chamber front

 3c secondary boiler room

 3d primary boiler room

 4 exhaust

 5 exhaust duct

 5a branch in the exhaust duct

 5b Shut-off valve in branch

 6 pressure probe

 7 supply line for steam

 7a steam

 7b valve

 8 gas flow direction for exhaust gas

 9 Drain pipe for condensate

 9a condensate

 9b line for condensate

 9c valve for condensate line

 10 servomotor

 1 1 exhaust manifold

 12 computer control

12a control lines 13 additional burners

 13a gas line to additional burner

 13b stop valve

 14 coke oven bench

 15 heat exchangers

 15a steam

 16 shut-off valve

 17 Atmospheric air

 18 emission control system

 19 exhaust fan

 20 exhaust stack

 21 emergency chimney

 22 coke quenching car

 22a Hot coke

 23 turbine

 24 capacitor

 25 cleaning unit

 25a pump

 26 feedwater tank

 27 generator

 28 coke oven operating machine

 28a Einfahrstempel

 29 coal cake

 30 coke oven chamber doors

 31 vents

 32 coke oven chamber ceiling

 33 steam manifold

 34 Feedwater line

 34a feedwater valve

 35 earth level

 36 carrying device

 37 tub

 A-E Arrangements of heat exchanger and valve on coke oven

Claims

claims An apparatus for producing a plurality of steam (1 d) or hot water streams in a coke oven bank (14)  A coke oven (3a) of the "heat recovery" type, which is arranged in a coke oven bank (14), and with a coke oven chamber (3), a gas space (3d) arranged therein, which in the loaded state has a primary heating space (3d ), a coke oven chamber ceiling (32), coke oven chamber doors (30), primary air openings (31) for the primary heating space (3d), and a secondary heating space (3c) located below the coke oven chamber (3) and containing secondary air openings;  A loading (28) and unloading system (22) for the coke oven (3a), which is responsible for loading the coke oven chamber (3) with the coking cake (29) provided for coking, and discharging the finished coke cake (22a) for the deletion process is provided,  An exhaust gas duct (5) which connects the secondary heating chamber (3c) to an exhaust gas collecting system (11) which discharges the exhaust gas (4) to the atmospheric environment after heat exchange and a required exhaust gas purification (18) have taken place,  characterized in that between the Sekundärheizraum (3c) and the Abgassammeisystem (11) in the exhaust passage (5), a heat exchanger (1) is arranged, which comprises a device for discharging the heat of the exhaust gas (4) to feed water (1 b) forms indirect heat exchange, and which is associated with a single coke oven (3a), and  · In the gas flow behind the heat exchanger (1) a valve (2) for dosing or Barrier of the exhaust duct (5) is arranged, which is associated with a single coke oven (3a), and which is controllable by means of pressure probes (6) in the exhaust passage (5), and the exhaust passage (5) behind the valve (2) in an exhaust manifold (11) opens, and A feedwater line (34) is provided, which serves for the supply of feed water (1 b) to the heat exchanger (1) of the coke oven (3a), and a steam line (1 d), which serves for the removal of the steam (1d) by the heat exchanger (1) is generated, and which leads into a vapor collecting line (33), with which the discharged steam (1 d) is continued, and A conversion unit (23) of the heat energy of the steam from the steam manifold (33) in secondary energy. 2. Apparatus according to claim 1, characterized in that the coke oven bank from 6 to 30 coke ovens (3a) is constructed. 3. Device according to one of claims 1 or 2, characterized in that on both frontal sides of a coke oven (3a) of the coke oven bank (14) at least one heat exchanger (1) for the individual coke oven (3a), a feedwater line (34) and a Steam line (33) are arranged. 4. Device according to one of claims 1 to 3, characterized in that at least one heat exchanger (1) in a coke oven bank (14) on the ceiling (32) of the coke oven chamber (3) or in a trough (37) in the Koksofenfundament before Coke oven (3a) is arranged. 5. Device according to one of claims 1 to 4, characterized in that the heat exchanger (1) in the interior with a by water (1b) flow through the tube bundle (1a), with by water (1 b) flow-through plate elements, or with water-flow Rib elements is equipped. 6. Device according to one of claims 1 to 5, characterized in that the heat exchanger (1) in the indirect heat exchange between the feed water (1 b) and the exhaust gas (4) according to the countercurrent principle, the cross-flow principle, the DC principle or a combination of these flow principles is working. 7. Device according to one of claims 1 to 6, characterized in that the heat exchanger (1) on the inside of the exhaust pipe (5) is equipped with a heat-resistant jacket, which consists of at least one insulating layer, and which with an anchor construction on the Inner wall of the exhaust pipe (5) is attached. 8. Device according to one of claims 1 to 7, characterized in that the exhaust valve (2) which is integrated in the heat exchanger (1), a flap (2a), a slide or a tap, which in the exhaust pipe (5 ) by the Heat exchangers (1) are arranged, and which are made of a heat-resistant material. 9. Device according to one of claims 1 to 8, characterized in that the exhaust valve (2) by an electrically operated motor (10) is driven. 10. Device according to one of claims 1 to 8, characterized in that the exhaust valve (2) by a pneumatically or hydraulically operated motor (10) is driven. 11. Device according to one of claims 1 to 10, characterized in that in the exhaust pipe (5), which through the heat exchanger (1) leads, a Pitotson- de (6) for pressure measurement or a manometer (6) for measuring pressure in the exhaust gas (4) is arranged. 12. Device according to one of claims 1 to 11, characterized in that in the exhaust pipe (5), which leads through the heat exchanger (1), a thermoelement or a lambda probe for measuring the oxygen content is arranged. 13. Device according to one of claims 1 to 12, characterized in that on the exhaust pipe (5) from the Sekundärheizraum (3c) of a coke oven (3a) at least one auxiliary burner (13) is arranged, which with a controllable fuel line (13a) temporarily and with adjustable power performs an additional heating of the exhaust gas (4). 14. The device according to claim 13, characterized in that along at least one coke oven chamber front (3b) for at least one auxiliary burner (13) a gas line (13a) extends, which can be shut off (13b). 15. Device according to one of claims 1 to 14, characterized in that on the heat exchanger (1) a feedwater supply line (1 b) is arranged, which is supplied via a water pump with feed water (1 b), and via a valve (1 c ) is adjustable or metered. 16. Device according to one of claims 1 to 15, characterized in that the vapor collecting line (33) between the heat exchanger (1) and the conversion unit (23) contains stretchable or shrinkable intermediate pieces, with where the thermal expansion of the isolated vapor manifold (33) can be buffered. 17. Device according to one of claims 1 to 16, characterized in that the vapor collecting line (33) is provided with a steam drum with which the steam can be stored. 18. Device according to one of claims 1 to 17, characterized in that the vapor collecting line (33) is arranged on at least one side of the coke oven chamber front (3b) in front of and along the Koksofenkammerfront (3b) below the operating stages. 19. Device according to one of claims 1 to 17, characterized in that the vapor collecting line (33) on at least one side of the coke oven chamber front (3b) before and along the Koksofenkammerfront (3b) in the bottom (35) is sunk. 20. Device according to one of claims 1 to 19, characterized in that in the exhaust pipe (5), which leads through the heat exchanger (1), a closable blind stub is arranged, which is for use of a mobile measuring device for measuring the temperature, the pressure or for measuring at least one gas component in the exhaust pipe is used. 21. Device according to one of claims 1 to 20, characterized in that in the exhaust pipe (5) in front of or behind the exhaust valve (2) a cleaning line (7) for steam (7a) or compressed air is arranged. 22. Device according to one of claims 1 to 21, characterized in that on the heat exchanger (1) a discharge line (9) is arranged, with which excess steam or waste water (9a) from the heat exchanger (1) in a discharge line (9b ) for drainage and drain into a container. 23. A method for producing a plurality of steam or hot water streams in a coke oven bank (14), wherein  • a number of 6 to 30 coke oven chambers (3a) of the type "heat recovery" is combined to form a coke oven bank (14), and The coal (29) is heated to high temperatures by cyclic coking, one cycle consisting of the charging, coking and discharging steps, and the coal (29) is coked in the coke oven chamber (3), where the Coke gas with a subset of combustion air in a Primärheizraum (3d), which is formed by the release of a gas space in the coke oven chamber (3) is stoichiometrically burned, and the partially burned coking gas in the sides of the coke oven chamber (3) arranged exhaust ducts in Sekundärheizräume (3c ) is passed below the coke oven chamber (3), where it is completely burned with a superstoichiometric amount of combustion air,  characterized in that • the completely burned exhaust gas (4) from the Sekundärheizraum (3c) of a single coke oven chamber (3) via an exhaust duct (5) in a heat exchanger (1) with integrated controllable exhaust valve (2) is given, so that the exhaust gas flow rate, which by the Heat exchanger (1) flows, is adjustable, and  The exhaust gas pressure at the inlet of the exhaust gas duct (5) into the heat exchanger (1) is measured so that the exhaust pressure (4) at each coke oven chamber (3) is set to a constant value via the exhaust valve (2) at least temporarily, and  The fully combusted exhaust gas (4) in the heat exchanger (1) generates a quantity of steam (1d) which is fed into a vapor manifold (33) in dependence on the supplied exhaust gas flow (5) and after passing through the vapor manifold to a conversion unit (23 ) is discharged to generate secondary energy, and  • the completely burned and cooled exhaust gas (8) is passed, after passing through the controllable heat exchanger (1) in an exhaust manifold (11) from which the exhaust gas (8) is used or discharged into the environment. 24. The method according to claim 23, characterized in that the steam flow rate at each coke oven (3a) by adjusting the exhaust gas flow (8) is set to a value of 300 kg / h to 3000 kg / h. 25. The method according to claim 23, characterized in that on at least one coke oven (3a) on two sides of the coke oven (3a) steam (1d) is generated, wherein on each side of the coke oven (3a) the steam flow rate by regulating the exhaust gas flow (8 ) is set to a value of 150 kg / h to 2850 kg / h. 26. The method according to any one of claims 23 to 25, characterized in that the temperature in the exhaust gas (4) at the inlet of the exhaust pipe in the heat exchanger (1) is between 850 ° C and 1550 ° C. 27. The method according to any one of claims 23 to 26, characterized in that the water supply (1 b) in the heat exchanger (1) is adjustable, and the temperature at the inlet of the exhaust pipe (5) in the heat exchanger (1) measured and the water supply (1 b) is controlled in the heat exchanger (1) on the basis of these measured values (6), so that the steam generation (1 d) takes place as a function of the temperature in the exhaust gas (4). 28. The method according to any one of claims 23 to 27, characterized in that in the exhaust pipe (5) of the heat exchanger (1) an auxiliary burner (13) is arranged, through which the temperature in the exhaust gas (4) before flowing through the heat exchanger (1 ). 29. The method according to claim 28, characterized in that the control of the auxiliary burner (13) on the basis of the measured values (6) for the temperature in the exhaust gas (4). 30. The method according to any one of claims 23 to 29, characterized in that the temperature in the exhaust gas (4) after the increase in temperature by the auxiliary burner (13) at the inlet of the exhaust pipe (5) in the heat exchanger (1) between 850 ° C and 1550 ° C is located. 31. The method according to any one of claims 23 to 30, characterized in that the vapor (1 d), which is generated on the heat exchanger (1), has a temperature of 120 to 600 ° C. 32. The method according to any one of claims 23 to 31, characterized in that the vapor (1 d), which is generated on the heat exchanger (1), has a pressure of 5 to 130 bar. 33. The method according to any one of claims 23 to 32, characterized in that at least one heat exchanger (1) instead of steam (1 d) hot water at a temperature of 40 to 120 ° C is generated. 34. The method according to any one of claims 23 to 33, characterized in that the regulation of the valve (2) for the exhaust gas (4) in the heat exchanger (1) based on the measured values (6) for pressure in the exhaust duct (5) by a computer ( 12). 35. The method according to any one of claims 23 to 34, characterized in that for sucking the exhaust gases (5) in the exhaust manifold (11) by suction (19), a negative pressure is provided. 36. Method according to claim 23, wherein the secondary energy conversion unit is a turbine (23) and a generator (27) and the secondary energy is electrical energy.