EP2213939A2 - Procédé destiné au fonctionnement d'une installation d'oxydation et installation d'oxydation - Google Patents

Procédé destiné au fonctionnement d'une installation d'oxydation et installation d'oxydation Download PDF

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Publication number
EP2213939A2
EP2213939A2 EP10000851A EP10000851A EP2213939A2 EP 2213939 A2 EP2213939 A2 EP 2213939A2 EP 10000851 A EP10000851 A EP 10000851A EP 10000851 A EP10000851 A EP 10000851A EP 2213939 A2 EP2213939 A2 EP 2213939A2
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EP
European Patent Office
Prior art keywords
heat
bed
concentration
oxidation
combustion chamber
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
EP10000851A
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German (de)
English (en)
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EP2213939A3 (fr
Inventor
Matthias Hänel
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Duerr Systems AG
Original Assignee
KBA Metalprint GmbH and Co KG
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Filing date
Publication date
Application filed by KBA Metalprint GmbH and Co KG filed Critical KBA Metalprint GmbH and Co KG
Publication of EP2213939A2 publication Critical patent/EP2213939A2/fr
Publication of EP2213939A3 publication Critical patent/EP2213939A3/fr
Ceased legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
    • F23G7/065—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel
    • F23G7/066—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel preheating the waste gas by the heat of the combustion, e.g. recuperation type incinerator
    • F23G7/068—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel preheating the waste gas by the heat of the combustion, e.g. recuperation type incinerator using regenerative heat recovery means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23M—CASINGS, LININGS, WALLS OR DOORS SPECIALLY ADAPTED FOR COMBUSTION CHAMBERS, e.g. FIREBRIDGES; DEVICES FOR DEFLECTING AIR, FLAMES OR COMBUSTION PRODUCTS IN COMBUSTION CHAMBERS; SAFETY ARRANGEMENTS SPECIALLY ADAPTED FOR COMBUSTION APPARATUS; DETAILS OF COMBUSTION CHAMBERS, NOT OTHERWISE PROVIDED FOR
    • F23M2900/00—Special features of, or arrangements for combustion chambers
    • F23M2900/13002—Energy recovery by heat storage elements arranged in the combustion chamber

Definitions

  • the invention relates to a method for operating an oxidation system, with an intended average heat input by means of a present in varying concentration reactant, wherein the heat input a desired heat profile is maintained in at least one heat bed of a heat exchanger.
  • the invention further relates to an oxidation plant.
  • Such a method can be used, for example, for operating a thermal-regenerative exhaust air purification system that represents the oxidation system.
  • it serves to remove hydrocarbons, ie reactants, from exhaust air of an upstream process by oxidation, in particular total oxidation.
  • hydrocarbons ie reactants
  • the exhaust gas purification system supplied raw gas so with the hydrocarbons contaminated air, may have a time varying concentration of hydrocarbons. This means that the exhaust air supplied to the exhaust air purification system may contain different proportions of the reactant at different times.
  • the heat exchanger is provided. This results in the combustion of hydrocarbons heat resulting from the exhaust air, so that it already has a temperature when entering a reaction or combustion chamber of the exhaust air purification system, which is higher than the outlet temperature of the exhaust air.
  • the heat exchanger has a plurality of heat beds, which can be operated alternately in different operating modes, namely raw gas operation, clean gas operation and rinsing operation. In raw gas operation, the polluted exhaust air is passed through the heat bed, the heated bed was previously heated by passing, hot clean gas.
  • the hot, coming from the combustion chamber clean gas is passed through the appropriate heat bed, so that it is heated, then to make the crude gas operation, the oxidation of the hydrocarbons or the reactant can.
  • a heat bed is operated to ensure that no raw gas enters the environment during the transition from a heat bed from the raw gas operation in the clean gas operation, that is, it must be ensured that no raw gas is in the heat bed.
  • pure gas originating from the combustion chamber of the exhaust air purification plant is passed through the heat bed to be rinsed and returned to the raw gas stream.
  • a method for operating an oxidation system having the features of claim 1.
  • a, in particular directly to a combustion chamber of the oxidation system coupled for charging, heat accumulator is provided for receiving excess heat, especially at above-average concentration of the reactant, and / or release of heat, especially in the case of below-average heat input due to below-average concentration of the reactant, serves.
  • An oxidation system serves, for example, to purify a pollutant having raw gas, ie a gas which has the reactant, so that no negative influences of the reactant on an environment of the oxidation system occur. This is achieved by the raw gas is subjected to temperature so that the reactant completely reacts or oxidizes.
  • the reactant can therefore be a fuel.
  • the heat exchanger is provided, with which heat from the exhaust gas of the oxidation system is introduced into the raw gas supplied thereto. In this case, a re-heating of 95% to 97% is possible, that is, 95% to 97% of the heat contained in the exhaust gas of the oxidation system can be returned to the raw gas.
  • the heat accumulator is provided. This serves to absorb excess heat, ie heat that can not be implemented in the heat exchanger. Excess heat is present, for example, if the concentration of the present reaction substance is above the design concentration of the oxidation plant.
  • the method can be used to operate a thermal-regenerative exhaust air purification system in which exhaust air charged with a time-varying amount of pollutants is passed through the heat exchanger for heating and then for oxidation of the pollutants through the combustion chamber. Above and at the design concentration is a self-sustaining operation of the exhaust air purification system feasible.
  • the heat storage can be supplied with heat at a concentration greater than the design concentration, and at a smaller concentration of heat for continuous self-sustained operation of the oxidation system are returned to the combustion chamber.
  • the heat accumulator is arranged, for example, fluidically parallel to the heat exchanger.
  • the described procedure can be used not only to operate the oxidation plant but also to design it.
  • the design is thus provided so that the heat accumulator absorb heat surplus and / or heat, especially in the case of below-average heat input, can deliver again.
  • the oxidation plant can be designed so that an autothermal operation over a wide concentration range can be provided.
  • the design concentration of the system can be selected to be higher.
  • the method can also be applied to a generic thermal installation.
  • a sufficiently large heat storage can be temporarily stored and, if necessary, ie with a time delay, released again.
  • This heat supply can be used both for discharging the heat required for a reaction, as well as for ensuring a continuous operation of another system which is connected to the oxidation system.
  • a continuous heat release of the heat accumulator can be provided, so not only in the presence of below-average heat input. This is especially true in the case of a stationary operation of the oxidation system in which the heat accumulator continuously supplied heat and withdrawn.
  • the heat storage can be connected directly to the reaction space or the combustion chamber of the system. This means that the exhaust gas from the heat storage system is tapped before it passes through an optional existing, series-connected heat exchanger. It is also possible that the exhaust gas flows through the heat accumulator and the heat exchanger in parallel, that is, the heat exchanger is provided fluidically parallel to the heat accumulator. In this way, the heat storage fluid supplied to a high temperature level.
  • an adapted dimensioning of the heat bed can be provided.
  • the heat bed is sized smaller than would be necessary for an autothermal reaction at a low concentration of the reactant. So there is a Unterdimensionleiter of the heat bed, the design concentration of the system is thus selected higher. This means that in a conventional oxidation system, a reaction of the reactant would be possible only with the introduction of additional fuel, if the concentration temporarily falls below the design concentration of the plant. This is prevented by the provision of the heat accumulator. As described above, heat is released therefrom, especially if the below-average heat input is present. Thus, even at a concentration that is below the design concentration of the system, operation of the system can be ensured.
  • a development of the invention provides that the system emits heat stored in the heat accumulator to at least one other system. In order to use the heat energy stored in the heat storage, this is delivered to another facility. Of particular importance in this case is the arrangement of the heat accumulator. While plants are known from the prior art, which provide heat storage in the other plant, the heat storage is included here in the oxidation system and arranged in this way between the combustion chamber and the other system. In this way, it is possible to increase the efficiency of the overall process, including both the oxidation plant and the at least one further plant. It can also be provided that the heat stored in the heat accumulator is released to the further system.
  • the concentration of the reaction substance falls below the design concentration of the oxidation system, so that only a below-average heat input is present.
  • the heat stored in the heat accumulator can ensure both the reaction of the reactant and the reliable and continuous operation of the further system.
  • the heat storage absorbs the heat surplus and releases only to operate the other system, while the reaction of the reactant is maintained, for example, with the introduction of additional fuel.
  • the oxidation system, in particular in the heat accumulator - due to the changing concentration of the reactant - releases heat stored discontinuously to at least one further unit. The delivery can preferably take place continuously.
  • a development of the invention provides that the temperature of a further system for the heat dissipation of supplied fluid is controlled and / or regulated.
  • the temperature present must be adapted. For example, adjusting the temperature to a design temperature of the other system. In particular, an over-temperature should be avoided, which can lead to damage to the other system. The adjustment takes place for example by mixing cold fluid and / or by appropriate alternate operation of different chambers of the heat accumulator.
  • a heat accumulator is used which is separate from the at least one heat accumulator.
  • "Separate” does not mean that the two elements (warm bed on the one hand and heat storage on the other hand) must be designed spatially separate, because they can be housed for example in a common outer housing.
  • the heat storage is an extra element, so not an element of the pure oxidation operation related oxidation plant.
  • the heat storage is therefore for example no further heat bed of the oxidation system.
  • the oxidation system has a plurality of heat beds, which are used alternately by flowing through a previously heated bed of heat, the reactant, thereby heated and then enters a combustion chamber. The resulting in the combustion chamber hot exhaust gas flows through another heat bed, which is preheated to - in the subsequent cycle - after reversing the gas flows to heat the reactant available.
  • the oxidation system in particular in the heat storage, in particular - due to the changing concentration of the reaction substance - discontinuous, stored heat to itself, in particular to the at least one heat bed to its / its heating, in particular before a restart of the Oxidation system, gives off.
  • the heat release can preferably be continuous.
  • the heat stored in the heat storage can be used to restart the oxidation system at the beginning of the week to heat the at least one heat bed, so that very fast and effective operation for the oxidation of the reactant can be performed.
  • the at least one heat-bed also has a certain heat-storage property, since it gives off the heat only slowly to the environment over a relatively long period of time, this procedure naturally ensures that the temperature of the heat-bed can be increased by means of the heat supplied by the heat store.
  • the heat accumulator is used with a heat retention capacity or a heat storage capacity that is greater than the heat retention capacity or the heat storage capacity of the at least one heat bed. Due to this fact, it is ensured that when the oxidation system cools down, the heat stored in the heat accumulator is available over a longer period of time and / or at a higher temperature than the heat which is present in the heat bed.
  • the oxidation system thus provides means to promote the medium, in particular the air, to make a heat removal from the heat storage can and be able to bring this heat in the heat bed.
  • the introduction into the heat bed takes place in particular from above.
  • a further development of the invention provides that a further heat exchanger, a heater, a production device, a refrigerating machine or an energy converter device is used as a further system.
  • the further heat exchanger may be part of a secondary circuit, the heat of the exhaust gas of the oxidation plant is supplied.
  • the further heat exchanger the heat is transferred to a fluid (for example, air, thermal oil, steam or water) of the secondary circuit, in which a further transport of the heat takes place to a place of use.
  • the secondary circuit may cooperate with a heater or a production device. This is called indirect heat use. But the heating or the production device can also represent the other system and be directly charged with the heat (direct heat use).
  • the heat energy can also be used an energy conversion device used as a further system, for generating, for example, electrical or mechanical energy.
  • a gas or steam turbine or a fuel cell can be used.
  • the special feature of the oxidation system is that the heat storage between the combustion chamber and the other system is provided, so not first a heat exchange to a lower temperature is performed and only then the heat is stored.
  • a development of the invention provides that a reaction of the reaction material in the heat bed and / or the combustion chamber takes place, wherein by means of the heat exchanger of the heat bed and / or the combustion chamber supplied reactant is heated with heat flowing from the combustion chamber exhaust gas.
  • the reaction of the reactant proceeds as soon as it has reached a sufficiently high temperature. This can already be the case when passing through the heat bed, so that the reaction can already take place in the heat bed.
  • the combustion chamber is provided for the reaction of the reactant.
  • a burner is arranged, which generates a permanent flame.
  • a support temperature is generated or ignited by passing through the heat bed warmed up reactant.
  • the heat exchanger serves to extract heat from the exhaust gas flowing out of the combustion chamber and to supply it to the reactant or the exhaust air.
  • the reaction mixture supplied to the heat bed or the combustion chamber is heated, whereby a reaction of the reactant in the heat bed or the combustion chamber is made possible.
  • a development of the invention provides that at least part of the exhaust gas is used in addition to heating the heat accumulator.
  • the resulting in the combustion chamber exhaust gas, in which the reactant is already completely oxidized, is used both for a heat exchange process between the exhaust gas and the unoxidized or spent reactant and for heating the heat accumulator.
  • the heating is carried out in particular when the concentration of the reactant exceeds the design concentration of the oxidation plant and thus there is excess heat.
  • a development of the invention provides that the heat storage is heated to almost the highest temperature present in the oxidation system.
  • the present or the highest temperature present in the reaction of the reactant should also be available in the heat accumulator. This is therefore heated at least almost to this highest temperature.
  • unloading the heat accumulator for releasing heat to maintain the heat profile or to operate the other system is therefore essentially this high temperature available.
  • a further development of the invention provides that a long-term heat store is used as the heat store.
  • the heat storage can hold the stored heat for a longer period of time, for example up to several days, in particular over a longer time, than the at least one heat bed. It is advantageous if a resulting during heating of the heat storage temperature stratification in the heat storage remains as long as possible, so no equalization of the temperature takes place in the heat storage.
  • a temperature which corresponds to a mean temperature of the heat accumulator By means of the heat accumulator so only a temperature can be achieved when removing the heat, which corresponds to the average temperature.
  • An advantageous embodiment of the invention provides that at a concentration which is below a minimum concentration, additional fuel is introduced into the combustion chamber and / or the heat bed. If the concentration of the reactant present is too low, ie if it is below the design concentration, the system can only be operated with the introduction of heat. This means that either heat must be released from the heat storage or additional fuel must be introduced into the system. If the minimum concentration, which is less than the design concentration, is also less than that, then this is the case only the introduction of fuel provided. The introduction can take place in the combustion chamber and / or the heat bed. In this way, a complete oxidation of the reactant is ensured even when falling below the minimum concentration. It may also be provided to dynamically adjust the minimum concentration of the oxidation system during operation. Thus, it may be advantageous to lower the minimum concentration at least temporarily to zero in order to ensure the reaction of the reactant only by heat from the heat storage. This can be done, for example, with a high amount of stored heat.
  • an autothermal operation is carried out with the release of heat from the heat accumulator into the heat bed and / or the combustion chamber. If the concentration of the reactant therefore lies between the minimum concentration and the design concentration of the system, autothermal operation of the system is nevertheless to be enabled, although this is not possible with below-average heat input in systems known from the prior art, since the concentration is less than the design concentration , For this purpose, heat is released from the heat storage. This can be done both in the warm bed and in the combustion chamber. By the discharge of heat into the heat bed and / or the combustion chamber, the reactant is brought to the temperature required for its reaction, so that it can proceed without further notice.
  • the temperature of the reactant can not be brought to the necessary temperature by means of the heat exchanger.
  • the desired heat profile should be maintained in the heat bed of the heat exchanger.
  • the minimum concentration can also be variably provided and in particular can be lowered to zero.
  • the excess of heat is present at a concentration which is above a design concentration.
  • the oxidation system is designed for the presence of a certain concentration, the design concentration.
  • the autothermal operation is feasible. This means that from a concentration greater than this design concentration, more heat is introduced into the system, as can be recycled through the heat exchanger. In this case, therefore, there is the excess heat that can be used to load the heat accumulator.
  • the reactant is a pollutant, in particular a volatile hydrocarbon.
  • the reactant must therefore not be discharged untreated into an environment of the system. It is therefore intended to carry out a reaction of the reactant in the system, in particular to oxidize it, so that no negative effects on the environment are exerted.
  • the pollutant may be a volatile hydrocarbon such as is found in many processing industries, particularly paint industries.
  • An advantageous embodiment of the invention provides that a bed and / or at least one molding element is used as a heat bed, wherein in particular a ceramic material is provided. It can be provided to assemble the heat bed from at least one molding element, for example a honeycomb, which advantageously consists of ceramic.
  • a bed is also possible.
  • the thermal bed may consist partly or entirely of a ceramic material.
  • the ceramic material is highly heat resistant and has a low coefficient of expansion. This means that with varying temperature exposure of the heat bed no strong expansion or contraction of the material occurs. Therefore, with a ceramic heat bed, both the design of the system can be simplified, and their life, due to the high temperature resistance of the ceramic material can be increased.
  • the invention further relates to an oxidation plant, in particular thermal-regenerative exhaust air purification system, preferably for carrying out the method described above, with an intended average heat input by means of a present in varying concentration reactant, wherein the heat input a desired heat profile is maintained in at least one heat bed of a heat exchanger.
  • a, in particular directly to a combustion chamber of the oxidation system coupled for charging, heat accumulator is provided which serves to absorb excess heat and / or for the release of heat, in particular in the case of a below-average heat input.
  • the above statements are also applicable.
  • the oxidation system is aimed at allowing an autothermal operation at an expected average concentration of the reactant. If the concentration of the reaction substance is below this design concentration, heat is taken from the heat store and fed to a combustion chamber or the heat bed of the oxidation system in such a way that a reaction of the reaction substance can take place.
  • At least two heat beds are provided, wherein at least one first heat bed in front of a combustion chamber and at least one second heat bed are arranged after a combustion chamber.
  • the heat exchanger thus has at least two heat beds, wherein a first fluidically provided before the combustion chamber and a second fluidically after this.
  • an alternating flow through the heat beds is preferably provided.
  • the respective heat bed is heated, whereas heat is given off to it during the passage through the reaction material, whereby the heat bed cools.
  • the reaction of the reaction substance can take place both in the combustion chamber and in the heat bed arranged in front of the combustion chamber.
  • the heat accumulator is arranged substantially parallel to the second heat bed and in particular connected to the combustion chamber is.
  • the heat storage is thus fluidly operated in parallel to the heat bed.
  • an inlet of the heat accumulator can also simultaneously be an inlet of the heat bed and an outlet of the heat accumulator can simultaneously be an outlet of the heat bed or these are fluidically connected to one another.
  • the heat storage can therefore be connected as well as the second heat bed directly to the combustion chamber.
  • a further system is connected to at least one medium connection, in particular exhaust connection, the system.
  • the medium connection may be in fluid communication with the heat storage and / or with at least one, in particular the second heat bed.
  • the medium connection can thus be fed by means of the heat storage and / or by means of the at least one heat bed with heat, which is passed on to the other system, in this way can be operated with the heat generated in the oxidation system, the other system and the heat be used meaningfully.
  • the at least one heat bath for heating is connected to the heat accumulator. This procedure according to the invention has already been discussed above in the discussion of the method.
  • the heat retention capacity or the heat storage capacity of the heat accumulator is greater than the heat retention capacity or the heat storage capacity of the at least one heat bed. hereby it is ensured that the heat accumulator keeps heat longer and / or at a higher temperature for a certain period of time than the heat bed, so that it is possible to use heat of the heat accumulator to heat up the heat bed.
  • the FIG. 1 shows an oxidation system 1 in the form of an exhaust air purification system 1 ', which has a heat exchanger 2 in the form of three heat sinks 3, 4 and 5, which are equipped for example with ceramic honeycomb bodies.
  • the oxidation system 1 is used to clean with volatile hydrocarbons or the reaction substance contaminated exhaust air K, which is raw gas.
  • the exhaust air K should therefore be freed from the hydrocarbons.
  • it is passed through one of the heat beds 3, 4 or 5.
  • FIG. 1 is shown how the exhaust air K is passed through the heat bed 4.
  • the thermal bed 4 is at a high temperature, for example, 800 ° C, preheated. Subsequently, the exhaust air K enters a combustion chamber 6 of the exhaust air purification system 1 '.
  • a burner 7 is arranged, which can produce a flame 8.
  • the burner 7 is intended to generate a support temperature in the combustion chamber 6.
  • the hydrocarbons are oxidized, so that from the raw gas containing hydrocarbons, pure gas is, which has only oxidized, that is burned, hydrocarbons.
  • the oxidation can take place both in the heat bed 4 and only in the combustion chamber 6.
  • the clean gas present in the combustion chamber 6 is then passed through the heat bath 5 in order to heat it up. Subsequently, the clean gas is discharged in accordance with the flow path 9 into an environment or outside atmosphere of the exhaust air purification system 1 '.
  • FIG. 3 is now a first variant of the exhaust air purification system 1 'shown in an operating mode in which the raw gas or the exhaust air K first passes through the heat bed 4, enters the combustion chamber 6 and then passes through the heat bed 3.
  • a heat accumulator 91 is provided, which is bypassable by means of a bypass device 12, which is shown here as a controllable or controllable valve.
  • the clean gas can thus flow out of the combustion chamber 6 through the heat bed 3 (flow path 9 ') and / or through the heat accumulator 11 (flow path 13) and / or past the heat accumulator 11 through the bypass device 12 (flow path 14).
  • the bypass device 12 may be omitted in a preferred embodiment.
  • the heat storage 11 1 By the heat storage 11 1 a possible energy loss is avoided.
  • the bypass device 12 it is also possible to provide a device by means of which the inflow from the combustion chamber 6 to the heat accumulator 11 is interrupted immediately. This is in FIG. 3 but not shown.
  • the clean gas is discharged either along the flow path 15 in the vicinity of the exhaust air purification system 1, or the pure gas flowing through the heat exchanger 11 or the bypass device 12 as indicated by the flow path 16, fed to another system 17.
  • a supply of the clean gas, which passes through the heat exchanger 2 or the heat bed 3 may be provided in the further system.
  • the clean gas flowing along the flow paths 13 and / or 14 can also be combined at one or several points with the clean gas which flows along the flow path 9 '.
  • the exhaust air purification system 1 ' has not shown fans and / or control valves, with which the fluid (clean gas and / or raw gas) within the Abluft mecanicsantage 1' can be moved. Through the flow flaps different flow paths are adjustable - for example, individual flow paths lockable - while the fans are used to transport the fluid.
  • the clean gas flows through the heat bed 5 in addition to or as an alternative to the heat bed 3.
  • the thermal bed 5 is also fluidly connected to the exhaust gas stream according to the flow path 9 '.
  • the bypass device 12 is a so-called bypass. With this, the clean gas or exhaust gas, bypassing the heat accumulator 11, for example, be discharged directly from the combustion chamber 6 in the environment of the system or to the further system 17.
  • the bypass device 12 is controlled or regulated as a function of the temperature of the heat accumulator 11. In particular, the clean gas should be guided around it when a maximum temperature of the heat accumulator 11 is exceeded. This means that an overfilling of the heat accumulator 11 may occur or that a loading of the heat accumulator 11 is interrupted as soon as the maximum temperature occurs or is detected in this.
  • Exhaust air purification systems 1 'known from the prior art are designed such that, given a concentration of the reaction substance which reaches at least one design concentration, an autothermal operation of the exhaust air purification system 1' can be carried out.
  • the heat beds 3, 4 and 5 must be sufficiently large to supply the highest possible amount of heat from the exhaust gas or clean gas emitted from the combustion chamber 6 to the raw material containing reactive substance, and in this way to increase its temperature as far as possible. It follows that the smaller the design concentration at which the exhaust air purification system 1 'is operable, the larger the heat beds 3, 4 and 5 must be dimensioned.
  • exhaust air purification system 1 now has under dimensioned heat beds 3, 4 and 5.
  • the heat sinks 3, 4 and 5 are designed smaller than an autothermal operation at a design concentration required.
  • the exhaust air purification system 1 ' is designed for a design concentration which is higher than a minimum concentration. Below the minimum concentration of additional fuel is added, at a concentration that is between minimum concentration and design concentration, however, heat is removed from the heat accumulator 11 to continuously continue the oxidation of the reactant.
  • the design concentration essentially corresponds to the minimum concentration.
  • the concentration of the reactant falls below the design concentration, that by means of the heat exchanger 2, the reagent or the raw gas can not be brought to a temperature which is necessary for the oxidation of the reactant.
  • the heat storage 11 is now provided to give off heat in the case of below-average heat input, in particular in the combustion chamber 6 and / or in the heat bed 3, to further allow a continuous reaction of the reactant without additional fuel through the burner 7 in the combustion chamber. 6 or to bring in the warming beds 3, 4 or 5. This means that when the heat input is below average, the heat stored in the heat accumulator 11 is used to increase the temperature of the raw gas, that is to say of the reactant.
  • the exhaust air purification system 1 At a concentration of the reaction substance below the minimum concentration, the exhaust air purification system 1' or the combustion chamber 6 and / or the heat beds 3, 4 and / or 5 additional fuel supplied to allow oxidation of the reactant. At a concentration which is greater than or equal to the minimum concentration but less than the design concentration, heat stored in the heat accumulator 11 is returned to the combustion chamber 6 or one or more of the heat beds 3, 4 and 5, respectively. Corresponds to the concentration of the design concentration, so is the exhaust air purification system 1 'in the autothermal operation, which means that neither additional fuel nor heat from the heat storage 11 must be supplied.
  • the concentration is higher than the design concentration, then more heat is formed by the oxidation of the reactant than can be reacted by means of the heat exchanger 2. It creates a heat surplus. This heat surplus can be absorbed by the heat accumulator 11 and stored for later use. This means that at least part of the exhaust gas or the clean gas from the combustion chamber 6 is used for heating the heat accumulator 11. If the heat accumulator 11 is completely loaded or a temperature of the heat accumulator 11 exceeds a maximum temperature, then the heat accumulator 11 can be relieved by means of a bypass device 12 by the exhaust gas or the clean gas is guided around the heat accumulator 11. Thus, there is no further loading of the heat accumulator 11.
  • bypass device 12 it is provided that no bypass device 12 is present, that is, it is an arrangement according to FIG. 3 , but without by-pass device 12 (with or without system 17).
  • the combustion chamber 6 only the heat storage 11 is connected downstream.
  • the bypass device 12 (hot bypass) is not present.
  • the design of the exhaust air purification system 1 ' is such that the heat sinks 3, 4 and 5 are undersized. While in a known exhaust air purification system 1 ', for example, an autothermal operation is provided at a concentration of 1.3 to 1.5 g / m 3 , for which heat beds 3, 4 and 5 are necessary with a height of 2.0 m, according to the invention, a design the exhaust air purification system 1 'to a design concentration of 3 g / m 3 . In this way, heat beds 3, 4 and 5 with a height of for example 1 m are sufficient. So far, only an optimization of the running in the exhaust air purification system 1 'process.
  • both the exhaust air purification system 1 'and the other system 17 can be operated with high efficiency and the lowest possible energy costs.
  • FIG. 4 shows a further variant of the exhaust air purification system 1 '.
  • the further system 17 is a production device 18 which is fed directly, ie directly, with waste gas from the exhaust air purification system 1 ', as indicated by the flow path 16.
  • the production device 18 consists of three hot air dryers 19, which are parallel to each other Exhaust gas are applied. After passing through the hot air dryer 19, the exhaust gas can again be contaminated with solvents or hydrocarbons. It is therefore, as indicated by the flow path 20, again as exhaust air K of the exhaust air purification system 1 'is fed to be cleaned there again.
  • a further heat exchanger 21 may be provided, which is arranged, for example, fluidically parallel to the heat storage 11.
  • the heat exchanger 21 can be switched through in parallel to the heat storage 11 of exhaust gas from the combustion chamber 6.
  • a secondary circuit 22 associated fluid for example, thermal oil, steam or the like
  • another system not shown here
  • this fluid can be supplied.
  • This fluid passes through the heat accumulator 11 in the direction of the combustion chamber 6 and thereby heats up, advantageously to a temperature which corresponds almost to the maximum temperature used during loading of the heat accumulator 11.
  • the heated fluid can now optionally the combustion chamber 6, the heat exchanger 21 and / or the other system 17 are supplied. In this way, both the reaction of the reactant in the combustion chamber 6 can be maintained, as well as the secondary circuit 22 by means of the heat exchanger 21 and the further system 17 further heat are supplied.
  • the heated fluid must be brought to a temperature which is suitable for the operation of the further system 17. This can be done by the fluid is first passed through the heat exchanger 21, wherein the fluid withdrawn heat and thus it is brought to a lower temperature. Alternatively, however, it is also possible to displace the heated fluid with cooler fluid and thus adjust its temperature so that it can be supplied to the further system 17. In this way, the other system 17 can be continuously supplied with heat, should the amount of heat generated in the exhaust air purification system 1 'be insufficient.
  • the heat stored in the heat accumulator is used to promote the operation of the oxidation system itself.
  • the heat supplied by the heat storage is thus not supplied to another system, but is used in the own oxidation plant.
  • the heat of the heat accumulator is used only for the further investment.
  • the heat accumulator When using the heat of the heat accumulator for own purposes, ie for the operation of the oxidation system, it is especially provided that in the event of shutdown of the oxidation system, ie a cooling of their components, in particular the at least one heat bed, before switching on again heat the heat accumulator is used to heat these components again. Accordingly, the heat accumulator has a better heat retention capacity or a better heat storage capacity than the components mentioned, so that the heat accumulator can provide heat which makes it possible to heat these components. Consequently, this results in a reaction-free preheating of the plant. If a desired temperature level is reached, the usual operation can be carried out, is oxidized at the reactant. If there is a heat surplus, it is stored in the heat storage. By storing the heat surplus, the inflow area of the heat bed does not become so hot that chemical reactions with the reactant take place there. Therefore, the thermal load of the construction is reduced.
  • the decoupling of excess heat and their storage in the heat storage simplifies and facilitates the operation of the oxidation operation of the relevant part of the oxidation plant, this part does not receive uncontrolled energy inputs.
  • the heat storage therefore performs an energy buffering and / or temperature smoothing function.

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Incineration Of Waste (AREA)
EP10000851A 2009-01-28 2010-01-28 Procédé destiné au fonctionnement d'une installation d'oxydation et installation d'oxydation Ceased EP2213939A3 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE200910007725 DE102009007725A1 (de) 2009-01-28 2009-01-28 Verfahren zum Betreiben einer Oxidationsanlage sowie Oxidationsanlage

Publications (2)

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EP2213939A2 true EP2213939A2 (fr) 2010-08-04
EP2213939A3 EP2213939A3 (fr) 2011-05-25

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EP (1) EP2213939A3 (fr)
DE (1) DE102009007725A1 (fr)
WO (1) WO2010086085A2 (fr)

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DE102010062144A1 (de) 2010-11-29 2012-05-31 Koenig & Bauer Aktiengesellschaft Druckmaschine mit mindestens einem einen Heißlufttrockner aufweisenden Trocknersystem sowie Verfahren zum Betreiben eines einen Heißlufttrockner aufweisenden Trocknersystems
DE102010062142A1 (de) 2010-11-29 2012-05-31 Koenig & Bauer Aktiengesellschaft Trocknersystem einer Bedruckstoff be- und/oder verarbeitenden Druckmaschine sowie Verfahren zum Betrieb eines Trockners einer Bedruckstoff be- und/oder verarbeitenden Druckmaschine
DE102010062145A1 (de) 2010-11-29 2012-05-31 Koenig & Bauer Aktiengesellschaft Druckmaschinen mit mindestens einem einen Heißlufttrockner aufweisenden Trocknersystem sowie Verfahren zum Betrieb einer Druckmaschine mit mindestens einem Heißlufttrockner
EP3168282A1 (fr) * 2015-11-12 2017-05-17 Benninghoven GmbH & Co.KG Mülheim Installation et procede de fabrication d'asphalte
US10042004B2 (en) 2015-02-12 2018-08-07 Mediatek Inc. Apparatus used with processor of portable device and arranged for performing at least one part of fuel gauge operation for battery by using hardware circuit element(s) when processor enter sleep mode
CN112513528A (zh) * 2018-11-12 2021-03-16 北京康肯环保设备有限公司 废气除害装置

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DE102016102506A1 (de) 2015-12-22 2017-06-22 Elringklinger Ag Packung und Kolonne umfassend eine oder mehrere Packungen

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WO2000011405A1 (fr) * 1998-08-21 2000-03-02 Key Engineering Co. Ltd. Systeme d'incineration regenerateur et a evaporation pour eaux usees
WO2010051916A1 (fr) * 2008-11-04 2010-05-14 Kba-Metalprint Gmbh Dispositif de transfert de chaleur et de purification d'air et procédé pour transférer de la chaleur

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102010062144A1 (de) 2010-11-29 2012-05-31 Koenig & Bauer Aktiengesellschaft Druckmaschine mit mindestens einem einen Heißlufttrockner aufweisenden Trocknersystem sowie Verfahren zum Betreiben eines einen Heißlufttrockner aufweisenden Trocknersystems
DE102010062142A1 (de) 2010-11-29 2012-05-31 Koenig & Bauer Aktiengesellschaft Trocknersystem einer Bedruckstoff be- und/oder verarbeitenden Druckmaschine sowie Verfahren zum Betrieb eines Trockners einer Bedruckstoff be- und/oder verarbeitenden Druckmaschine
DE102010062145A1 (de) 2010-11-29 2012-05-31 Koenig & Bauer Aktiengesellschaft Druckmaschinen mit mindestens einem einen Heißlufttrockner aufweisenden Trocknersystem sowie Verfahren zum Betrieb einer Druckmaschine mit mindestens einem Heißlufttrockner
WO2012072283A1 (fr) 2010-11-29 2012-06-07 Koenig & Bauer Aktiengesellschaft Systèmes de séchage d'une machine à imprimer traitant et/ou transformant un support d'impression et procédé servant à faire fonctionner un séchoir d'une machine à imprimer traitant et/ou transformant un support d'impression
DE102010062145B4 (de) * 2010-11-29 2015-10-29 Koenig & Bauer Ag Druckmaschine mit mindestens einem einen Heißlufttrockner aufweisenden Trocknersystem sowie Verfahren zum Betrieb einer Druckmaschine mit mindestens einem Heißlufttrockner
DE102010062142B4 (de) * 2010-11-29 2015-11-12 Koenig & Bauer Ag Druckmaschine mit einem Trocknersystem sowie Verfahren zum Betrieb eines Trockners einer Bedruckstoff be- und/oder verarbeitenden Druckmaschine
DE102010062144B4 (de) * 2010-11-29 2015-11-12 Koenig & Bauer Ag Druckmaschine mit mindestens einem einen Heißlufttrockner aufweisenden Trocknersystem sowie Verfahren zum Betreiben eines einen Heißlufttrockner aufweisenden Trocknersystems
US10042004B2 (en) 2015-02-12 2018-08-07 Mediatek Inc. Apparatus used with processor of portable device and arranged for performing at least one part of fuel gauge operation for battery by using hardware circuit element(s) when processor enter sleep mode
EP3168282A1 (fr) * 2015-11-12 2017-05-17 Benninghoven GmbH & Co.KG Mülheim Installation et procede de fabrication d'asphalte
EP3168282B1 (fr) 2015-11-12 2018-12-12 Benninghoven GmbH & Co. KG Installation et procede de fabrication d'asphalte
CN112513528A (zh) * 2018-11-12 2021-03-16 北京康肯环保设备有限公司 废气除害装置

Also Published As

Publication number Publication date
EP2213939A3 (fr) 2011-05-25
DE102009007725A1 (de) 2010-09-09
WO2010086085A3 (fr) 2011-06-16
WO2010086085A2 (fr) 2010-08-05

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