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    • 专利摘要:
    The invention relates in particular to a method for cleaning exhaust gas (15) laden with high-boiling organic pollutants by means of an exhaust gas cleaning system (1) with at least one rotatable adsorption body (2), a device for supplying the oxidizing agent (24) or the oxidizing gas (25) to the Adsorption body (2), with the exhaust gas (15) being fed to a first sector (6) of the adsorption body (2) during normal operation of the method, in which the pollutants of the exhaust gas (15) as the exhaust gas (15) passes through the adsorption body ( 2) are adsorbed by the adsorption body (2) and the resulting cleaned exhaust gas (16) is discharged from the first sector (6), with a second sector (7) of the adsorption body (2) desorption gas (17) during normal operation of the process for desorption of the adsorbed low-boiling pollutants is supplied, in which the low-boiling pollutants adsorbed on the adsorption body (2) at Durc When the desorption gas (17) passes through the adsorption body (2), the desorption gas (18) thus concentrated is fed to an aftertreatment system (10) and converted into pure gas (19), and an oxidizing agent (24) is added to the adsorption body (2). containing oxidizing gas (25) for removing high-boiling pollutants adsorbed on the adsorption body (2).
    公开号:AT522330A4
    申请号:T50614/2019
    申请日:2019-07-05
    公开日:2020-10-15
    发明作者:Mülleder Christian
    申请人:Ctp Chemisch Thermische Prozesstechnik Gmbh；
    IPC主号:
    专利说明:

    Process and system for cleaning organic pollutants
    laden exhaust gases
    The invention relates to a method, a device, a regeneration device and an arrangement according to the preambles of the independent claims.
    Different methods for cleaning exhaust gases laden with low-boiling pollutants are known from the prior art. For example, methods are known in which most of the pollutants are removed from the exhaust gas by a zeolite wheel and released into a desorption flow which is smaller by the enrichment factor. In conventional processes, the desorption stream is converted into pure gas either by regenerative thermal oxidation, regenerative catalytic oxidation or by recuperative catalytic oxidation.
    However, the disadvantage of these conventional zeolite wheel arrangements is that their field of application is limited to exhaust gases which exclusively contain low-boiling substances with a boiling range between preferably at least 60.degree. C. and a maximum of 200.degree
    contain.
    If high-boiling substances are only present in small parts in the exhaust gas, they will accumulate on the zeolite wheel over time. Since the high-boiling substances cannot be removed using conventional methods, the capacity of the zeolite wheel decreases. As a result, the cleaning performance deteriorates and the concentration of pollutants in the exit from the zeolite wheel increases.
    In addition, high-boiling substances can also be formed from low-boiling substances, for example by desorption or by polymerization, since the surface of the zeolite wheel has a catalytic effect to a certain extent.
    As soon as more than a certain percentage by weight, in particular seven and more percent by weight, based on the mass of zeolite, has been adsorbed on high-boiling substances, a sufficient cleaning performance is usually no longer given and furthermore, if the zeolite wheel is heated, the zeolite wheel can burn up in an uncontrolled manner and an accompanying destruction of the same.
    This means that the applicability of conventional methods is limited to exhaust gases where, in addition to the general requirements such as
    - exhaust gas temperature preferably between 20 ° C and 35 ° C,
    - Relative humidity preferably less than 80%,
    - Exhaust gas concentration 0.1 to max. 1.5 g / Nm®,
    - Boiling points of the substances in the exhaust gas between 60 ° C and 200 ° C, also the prerequisite for the essentially complete absence of high boilers
    must be fulfilled.
    The object of the invention is to overcome the disadvantages of the prior art. In particular, it is the object of the invention to create a method with which an exhaust gas containing high-boiling substances can be concentrated and purified. The invention is therefore based inter alia on the object of creating a method which does not reduce the durability of the adsorption body, in particular of the adsorbent. Further objects of the invention include providing an apparatus, a regeneration apparatus and an arrangement which
    enable the method according to the invention.
    The object of the invention is achieved in particular by the features of
    independent claims solved.
    The invention relates in particular to a method for cleaning exhaust gas laden with high-boiling organic pollutants by means of an exhaust gas cleaning system with at least one rotatable and essentially cylindrical adsorption body, with the exhaust gas being fed to a first sector of the adsorption body in normal operation, the pollutants of the exhaust gas in the first sector are adsorbed by the adsorption body when the exhaust gas passes through the adsorption body and the purified exhaust gas resulting from this is discharged from the first sector, with desorption gas being supplied to a second sector of the adsorption body in normal operation for desorption of the adsorbed low-boiling pollutants, in the second sector the low-boiling pollutants adsorbed on the adsorption body are desorbed when the desorption gas passes through the adsorption body and the concentrated desorption gas is added to an aftertreatment system hears and is converted to clean gas.
    It is preferably provided that the adsorption body is supplied with an oxidizing gas containing an oxidizing agent for removing high-boiling pollutants adsorbed on the adsorption body.
    In the context of the present invention, low-boiling pollutants can be understood to mean substances with a boiling point of less than 200 ° C and high-boiling pollutants to be understood as substances with a boiling point of over 200 ° C, in particular in the range between 200 ° C and 400 ° C inclusive.
    In the context of the present invention, the oxidizing agent is to be understood as meaning a substance which can oxidize other substances and is itself reduced in the process. For example, the oxidizing agent can be ozone, hydrogen peroxide, oxygen difluoride or fluorine. The oxidizing gas can include the oxidizing agent. The oxidizing agent can, in particular exclusively, be formed from the oxidizing agent
    be.
    In the context of the present invention, the oxidizing gas is to be understood as a gas which contains the oxidizing agent. In other words, the oxidizing gas can be the desorption gas containing the oxidizing agent and / or the ambient air containing the oxidizing agent.
    In the context of the present invention, the concentrated desorption gas can be understood to mean the desorption gas containing the desorbed pollutants. In particular, the method can increase the concentration of the pollutants in the concentrated desorption gas compared to the exhaust gas by fifteen
    up to twenty-fivefold.
    In the context of the present invention, the contaminated oxidizing gas can be understood to mean the oxidizing gas containing the desorbed pollutants. The concentrated desorption gas optionally includes the contaminated oxidizing gas. In particular, conventional recirculation measures can further increase the concentration of the pollutants.
    In normal operation, the exhaust gas can be fed to a first area or a first sector of the adsorption body. The exhaust gas introduced can flow through the adsorption body, the pollutants of the exhaust gas being able to be adsorbed by the adsorption body as it flows through. After passing through the adsorption body, the exhaust gas can, if appropriate, exit the first area or the first sector into the surroundings. The temperature of the exhaust gas entering the first sector or area is preferably in the range from 10 ° C. to 40 ° C. inclusive, preferably in the range from 20 ° C. to 35 ° C. inclusive.
    The adsorption body can be formed from a zeolite, in particular from corrugate made of glass fibers, to which zeolite powder has been fixed with a suitable binder, or a zeolite-containing material. The adsorption body can comprise a zeolite, in particular corrugate made of glass fibers, to which zeolite powder has been fixed with a suitable binder, or a zeolite-containing material.
    Furthermore, during normal operation, the desorption gas for desorption of the adsorbed low-boiling pollutants can be fed to a second area or a second sector of the adsorption body. The desorption gas can flow through the adsorption body, with the adsorbed low-boiling pollutants being able to be desorbed by the adsorption body when it flows through. The concentrated desorption gas can be fed to the aftertreatment system and then converted into pure gas. The temperature of the desorption gas entering the second sector is preferably in the range from 100 ° C. to 300 ° C. inclusive, preferably 170 ° C. to 220 ° C. inclusive. To prevent damage to the adsorption body, the temperature of the
    Desorption gas must be limited to a maximum of 300 ° C.
    The adsorption body is preferably flowed through with an oxidizing gas containing an oxidizing agent. By supplying the oxidizing gas, the high-boiling pollutants deposited on the adsorption body can be brought into contact with the oxidizing gas and thereby removed again from the adsorption body. The oxidizing gas containing the removed pollutants, the so-called contaminated oxidizing gas, can be discharged from the adsorption body. By removing the high-boiling pollutants, the adsorption capacity of the adsorption body can be increased or essentially the original adsorption capacity can be restored.
    The exhaust gas cleaning system can have connections for the supply of the exhaust gas and the desorption gas and connections for the discharge of the cleaned exhaust gas and the concentrated desorption gas opposite on both sides relative to the rotatable or rotating adsorption body. Through these connections it may be possible to feed the various substances to specific areas or specific sectors of the adsorption body.
    In the context of the present invention, under a sector of
    Adsorption body can be understood as a certain limited area or a circular sector of the adsorption body at a certain point in time. Through the
    Rotation of the adsorption body can be a different area of the adsorption body under the fixed and sealed sector of the
    Be arranged exhaust aftertreatment system.
    In particular, it is provided that the second sector, preferably directly, adjoins the first sector and that the possibly present third sector, preferably directly, adjoins the second sector.
    Oxidation gas is preferably fed to an area or a sector, in particular the second sector, of the adsorption body which has a temperature of 100 ° C. to 300 ° C. inclusive, in particular 150 ° C. to 250 ° C. inclusive.
    If necessary, it is provided that the method steps of the method as described above take place essentially at the same time. In this case, it can be provided that, in normal operation, the first sector of the adsorption body is flowed through with exhaust gas, while the second sector of the adsorption body is flowed through with desorption gas
    is flowed through.
    The oxidizing gas can be fed to the adsorption body continuously or discontinuously, in particular only at certain times. For example, the oxidizing gas can be fed to the adsorption body once a quarter, once a month, once a week or twice a week. The oxidizing agent is preferably fed in at intervals, in particular for economic reasons, in order to increase the capacity of the adsorption body and in particular to restore the capacity of the adsorption body.
    The adsorption body can flow through axially or radially. For example, the adsorption body can be a hollow cylinder-like rotor through which flow radially flows. For example, the adsorption body can be an adsorber wheel, on which double-walled wood cylinders filled with zeolite pellets are distributed over the circumference, and these wood cylinders are gradually moved further and flow radially through them
    will.
    7739
    In all embodiments it is preferably provided that the method according to the invention is automated, in particular by a control device of the
    Exhaust gas cleaning system controlled and / or regulated, is executed.
    If necessary, it is provided that the adsorption body is cylindrical and that the adsorption body is rotated about its axis of rotation.
    If necessary, it is provided that the adsorption body of the exhaust gas cleaning system is a so-called zeolite rotor or a so-called zeolite rotor concentrator wheel, and / or that the exhaust gas cleaning system comprises fixed and sealed sectors, whereby the exhaust gas, the desorption gas, the oxidizing gas and / or the ambient air specific sectors of the rotatable or rotating adsorption body can be fed or are, and / or that the aftertreatment system is a regenerative thermal oxidation system.
    If necessary, it is provided that the oxidizing gas is fed to the second sector, in particular to a sub-area of the second sector.
    The second sector of the adsorption body preferably has a temperature of 100 ° C. up to and including 300 ° C., in particular 150 ° C. up to and including 250 ° C. Furthermore, the second sector of the adsorption body can be heated to a temperature of 100 ° C. up to and including 300 ° C., in particular 150 ° C. up to and including 250 ° C., before the supply of the oxidizing gas.
    If necessary, it is provided that the concentrated desorption gas from the second sector, in particular from the sub-area of the second sector, a
    Aftertreatment system is supplied.
    If necessary, it is provided that the oxidation gas in the second sector is essentially completely washed around and / or flowed around by desorption gas.
    The oxidizing gas can only come into contact with the second sector or a partial area of the second sector of the adsorption body. Prefers
    the oxidizing gas can flow through a specific sub-area of the second sector, the surrounding sub-areas of the second sector from
    Desorption gas are flowed through.
    This makes it possible for the oxidizing gas, preferably exclusively, to come into contact with the adsorption body. Contact of the oxidizing gas with various parts of the oxidizing gas which are not resistant to the oxidizing gas is preferred
    Emission control system avoided.
    It is optionally provided that the oxidizing gas is generated by introducing the oxidizing agent into the desorption gas, or that the oxidizing gas is generated by introducing the oxidizing agent into a partial flow of the desorption gas
    is produced.
    The oxidizing gas can be formed by introducing oxidizing agent or oxidizing gas into a mixer. The oxidizing gas can be formed by mixing oxidizing agent or oxidizing gas with a carrier medium, in particular ambient air, desorption gas and / or nitrogen.
    If necessary, it is provided that the oxidizing gas is fed to the adsorption body during a maintenance operation, that the adsorption body is rotated continuously or discontinuously in the maintenance operation, and that, if necessary, the supply of exhaust gas to the first sector is shut off in the maintenance operation or, if necessary, in particular exclusively, ambient air is shut off first sector is fed.
    If necessary, provision is made to supply the oxidizing gas to the, in particular the entire, second sector of the adsorption body during maintenance operation. In order to allow the adsorption body to be heated to a temperature in the range from 150 ° C up to and including 200 ° C in this case, the adsorption body can be rotated discontinuously. This can inter alia prevent the intermediate formation of explosive mixtures, such as peroxides,
    avoided or prevented.
    The temperature of the adsorption body can be measured on the outlet side of the desorption sector or the partial area in which the oxidizing gas flows out. If necessary, the oxidizing gas or the oxidizing agent is only metered in when the temperature of the adsorption body is above 150 ° C.
    If necessary, provision is made to supply the oxidizing gas to only a partial area of the second sector of the adsorption body during maintenance operation. In this case, the adsorption body may already be preheated, which means that the same
    Mass flow of ozone a higher concentration in the partial flow can be used.
    If necessary, it is provided that before the supply of the oxidizing gas, the adsorption body is broken down into parts of the adsorption body, and / or that before the supply of the oxidizing gas, the adsorption body, the second sector, in particular the sub-area of the second sector, or at least one adsorption body part is heated to a temperature in the range of 150 ° C up to and including 250 ° C, in particular to 200 ° C, is heated.
    If necessary, the at least one adsorption body part outside the exhaust gas purification system, for example in a mobile regeneration device at the end user or in a stationary regeneration unit, with oxidizing gas
    regenerated.
    If necessary, the adsorption body, the second sector, in particular the sub-area of the second sector, or at least one part of the adsorption body is heated to a temperature in the range from 100 ° C. to 300 ° C., in particular to 200 ° C., before the oxidizing gas is supplied.
    It is optionally provided that the concentration of the oxidizing agent in the oxidizing gas is in the range from 200 ppm to 1000 ppm, in particular in the range from 400 ppm to 800 ppm, and is preferably 600 ppm, the oxidizing agent comprising ozone and / or hydrogen peroxide, or where the Oxidizing agent consists of ozone and / or hydrogen peroxide.
    In particular, it may be possible, by supplying an oxidizing gas with an ozone concentration in the range from 400 ppm up to and including 800 ppm to an approximately 200 ° C adsorption body, to oxidize even high-boiling pollutants with a boiling point of over 400 ° C essentially without leaving any residue
    to desorb with it.
    It is optionally provided that the concentration of the oxidizing agent in the desorption gas is in the range from 200 ppm to 1000 ppm, in particular in the range from 400 ppm to 800 ppm, and is preferably 600 ppm.
    If necessary, it is provided that the introduction of the ozone into the oxidizing gas or into the desorption gas takes place via a static mixer. If necessary, it is provided that the introduction of the hydrogen peroxide into the oxidizing gas or into the desorption gas via a nozzle, in particular via a mist nozzle or a 2-
    Fabric nozzle, or an ultrasonic evaporator.
    It is optionally provided that the oxidizing agent is formed in a generating device, or that the oxidizing agent is formed in order to form the oxidizing gas
    Oxidizing agent is supplied from a storage device.
    The generating device can be a device which is set up to generate the oxidizing agent. Preferably the generating device is a
    Ozone generator or a hydrogen peroxide generator.
    The storage device can be a device which is set up to store the oxidizing agent or the oxidizing gas. The storage device is preferably a tank for ozone, a tank for gas containing ozone, a tank for hydrogen peroxide or a tank for gas containing hydrogen peroxide.
    Optionally, ozone is stored in the storage device. Ozone is preferred
    on site, preferably with an ozone generator from dried air or from pure
    Oxygen. Preferably no pure ozone, only ozone in
    a carrier gas such as air or nitrogen generated.
    Hydrogen peroxide is preferably stored as an aqueous solution in the storage device. The aqueous solution can be nebulized, evaporated or evaporated without the hydrogen peroxide decomposing.
    It is preferably provided that the oxidizing agent or the oxidizing gas is introduced into the exhaust gas cleaning system from an external source, in particular from a mobile device. It is optionally provided that the oxidizing agent or the oxidizing gas is discontinuous or to the adsorption body
    is fed continuously.
    It is optionally provided that the oxidizing gas is fed to the adsorption body at a temperature in the range from 150 ° C. to 250 ° C. inclusive, preferably at a temperature of 200 ° C., and / or that the adsorption body is supplied with a flow rate of the oxidizing gas in the range of 2 m / s up to and including 6 m / s, in particular 3 m / s up to and including 5 m / s.
    In particular, an oxidizing agent-containing oxidizing gas at a temperature of 150 ° C. up to and including 250 ° C., preferably at about 200 ° C., is supplied to the adsorption body to remove high-boiling pollutants adsorbed on the adsorption body.
    If necessary, it is provided that the adsorption body is flowed through from its desorption outlet side in the direction of its desorption inlet side with oxidation gas, and / or that the adsorption body is flowed through from its desorption inlet side in the direction of its desorption outlet side with oxidation gas, and / or that the adsorption body for a first period of time Direction and the adsorption body for a second period in a second, in particular the first direction opposite, direction with oxidizing gas
    is flowed through.
    If necessary, it is provided that the adsorption body is flowed through with oxidizing gas counter to the adsorption direction and / or that the adsorption body is flowed through for a first period in a first direction and for a second period in the opposite direction.
    By reversing the direction of flow, the removal of the high-boiling pollutants can be accelerated and / or improved, among other things.
    If necessary, it is provided that the oxidizing gas, after flowing through the adsorption body, is fed to a conversion device, in particular an ozone destruction catalyst, in which the oxidizing agent is consumed or converted, and / or that the oxidizing gas, after flowing through the adsorbent body, is fed to the aftertreatment system in which the Oxidizing agent is consumed or converted.
    After flowing through the adsorption body, the oxidizing gas can contain the high-boiling pollutants removed from the adsorption body or the substances converted from them. The oxidizing gas containing pollutants can be fed to a conversion device and / or an aftertreatment system.
    In particular, it can be provided that the unreacted oxidizing agent in a conversion device upstream of the aftertreatment system
    is consumed or converted.
    In particular, it can be provided that the unreacted oxidizing agent is fed directly to the aftertreatment system and in the aftertreatment system
    is consumed or converted.
    If necessary, provision is made for exhaust gas or ambient air to be supplied to a third sector of the adsorption body during normal operation, which is heated when it passes through the adsorption body, and the desorption gas is produced by mixing clean gas generated in the aftertreatment system with the heated exhaust gas exiting the third sector or with the one from the third sector
    exiting heated ambient air is formed, or the heated exhaust gas exiting the third sector or the heated ambient air exiting the third sector is brought to the desorption temperature in an, in particular recuperative, heat exchanger with heat, in particular excess heat, from the reaction chamber.
    If necessary, exhaust gas and / or ambient air flows through the third sector for recooling the adsorption body after desorption. The exhaust gas and / or the ambient air can be preheated.
    The exhaust gas and / or the ambient air can then be brought to the desorption temperature of 170 to 300 ° C., in particular 200 ° C. to 220 ° C. inclusive, in a mixer, a heat exchanger or by direct heating, and then flow through the adsorption body. In particular, the adsorption body can be in countercurrent to adsorption or in the direction of adsorption
    reverse direction are flowed through by the desorption gas.
    If necessary, it is provided that the aftertreatment system comprises at least two heat-storing regenerators connected to a reaction chamber, that the concentrated desorption gas and / or the contaminated oxidizing gas is converted to pure gas in the reaction chamber, and that the desorption gas containing the desorbed pollutants alternates between the regenerators in cycles
    is fed.
    If necessary, a cycle can include the following steps:
    - Feeding the concentrated desorption gas and / or the contaminated oxidizing gas to the reaction chamber through at least one regenerator which has been heated in a previous cycle by the flow of hot clean gas in order to heat the concentrated desorption gas and / or the contaminated oxidizing gas and to increase it in the reaction chamber
    To implement clean gas,
    - Discharge of the hot clean gas from the aftertreatment system through at least one further regenerator, whereby the at least one further
    Regenerator is heated.
    In particular, the invention relates to a device for supplying the oxidizing agent or the oxidizing gas to the adsorption body according to the method according to the invention, characterized in that the device comprises a supply device, the supply device being set up to supply an oxidizing gas to the second sector, in particular a sub-area of the second sector or wherein the feed device is set up to introduce an oxidizing agent or an oxidizing gas into the exhaust gas purification system in such a way that the oxidizing gas can be fed to the second sector, in particular to a sub-area of the second sector.
    If necessary, it is provided that the device comprises a discharge device which is set up to feed the oxidizing gas containing the desorbed pollutants from the second sector, in particular from the sub-area of the second sector, to the aftertreatment system.
    It is optionally provided that the device comprises at least one generating device which is set up to generate an oxidizing agent or the oxidizing gas, or that the device comprises at least one storage device containing the oxidizing agent or the oxidizing gas,
    which is set up to store the oxidizing agent or the oxidizing gas.
    If necessary, it is provided that the device comprises at least one conversion device, in particular an ozone destruction catalyst, which is designed to consume or convert the oxidizing agent of the oxidizing gas, and that the oxidizing gas containing the desorbed pollutants via the discharge device of the at least one
    Conversion device can be fed.
    If necessary, it is provided that the device is a mobile module which is set up for temporary connection to the exhaust gas cleaning system.
    In particular, the invention relates to a regeneration device for supplying the oxidation gas to the adsorption body or to at least one adsorption body part according to the method according to the invention, characterized in that the regeneration device is optionally set up to bring the adsorption body or at least one adsorption body part at least in sections to a temperature in the range of 150 ° C up to and including 250 ° C, in particular to 200 ° C, and that the adsorption body or the at least one part of the adsorption body in the regeneration device
    Oxidation gas can be acted upon.
    Alternatively, the adsorption body is removed from the exhaust gas purification system before being introduced into the regeneration device and placed in
    at least two parts of the adsorption body are dismantled.
    In the regeneration device, the adsorption body or at least one part of the adsorption body can first be heated to a range from 100 ° C. up to and including 300 ° C., in particular to 200 ° C. Oxidation gas can then be fed to the heated adsorption body or the at least one heated adsorption body part. The oxidizing gas can flow through the adsorption body or the at least one adsorption body part, the pollutants being removed from the adsorption body or the at least one adsorption body part
    can be.
    If necessary, a regeneration process with the regeneration device can include the following steps: dismantling and dismantling the adsorption body into at least two adsorption body parts, introducing at least one adsorption body part into the regeneration device, heating the at least one adsorption body part to a temperature in the range from 150 ° C up to and including 250 ° C, in particular to 200 ° C. in the regeneration device, and loading of the at least one adsorption body part in the regeneration device
    Oxidizing gas. The steps of the regeneration process with the regeneration device preferably run in the order listed above.
    In particular, the invention relates to an arrangement comprising an exhaust gas purification system according to the invention and a device according to the invention, characterized in that the feed device of the device can be connected to the exhaust gas purification system so that the oxidizing agent or the oxidizing gas can be introduced into the exhaust gas purification system in such a way that the oxidizing gas is transferred to the second sector, in particular a part of the second sector, can be supplied.
    Further features according to the invention may emerge from the claims, the description of the exemplary embodiments and the figures.
    The invention will now be made more exemplary, not exclusive and / or using the example
    non-limiting exemplary embodiments further explained.
    Fig. 1 shows a schematic graphic representation of a first embodiment of the exhaust gas cleaning system according to the invention,
    Fig. 2 shows a schematic graphic representation of a second embodiment of the exhaust gas cleaning system according to the invention, and
    3 shows a schematic graphic representation of a third embodiment of the exhaust gas cleaning system according to the invention.
    Unless otherwise indicated, the reference symbols correspond to the following components: exhaust gas purification system 1, adsorption body 2, desorption inlet side 3, desorption outlet side 4, axis of rotation 5, first sector 6, second sector 7, part of second sector 8, third sector 9, aftertreatment system 10, reaction chamber 11 , Regenerators 12, conversion device 13, mixer 14, exhaust gas 15, purified exhaust gas 16, desorption gas 17, concentrated desorption gas 18, clean gas 19, ambient air 20, feed device 21, discharge device 22, arrangement 23, oxidizing agent 24 and oxidizing gas 25.
    FIG. 1 shows a schematic graphic representation of the first embodiment of the exhaust gas cleaning system 1 according to the invention, which is set up to carry out the method according to the invention. In other words, this exhaust gas cleaning system 1 can be used to clean exhaust gases 15 which are loaded with high-boiling organic pollutants.
    The exhaust gas cleaning system 1 comprises a rotatable about an axis of rotation 5
    cylindrical adsorption body 2.
    The adsorption body 2 of the exhaust gas purification system 1 is a so-called zeolite rotor or a so-called zeolite rotor concentrator wheel. The aftertreatment system 10
    is a regenerative thermal oxidation plant.
    The exhaust gas cleaning system 1 comprises fixed and sealed sectors 6, 7, 9, whereby the exhaust gas 15, the desorption gas 17, the oxidizing gas 25 and / or the ambient air 20 can be supplied to certain sectors 6, 7, 9 of the rotatable or rotating adsorption body 2 or are. In this embodiment, the adsorption body 2 are supplied via three sectors 6, 7, 9 gases. The second sector 7 adjoins the first sector 6 and the third sector 9 adjoins the second sector 7
    on.
    In normal operation, exhaust gas 15 is introduced into the exhaust gas cleaning system 1. This exhaust gas 15 is fed to a first sector 6 of the adsorption body 2, the pollutants of the exhaust gas 15 being adsorbed by the adsorption body 2 as it passes through the adsorption body 2. The cleaned exhaust gas 16 is discharged from the first sector 6 into the environment.
    Furthermore, a desorption gas 17 at a temperature of 200 ° C. is fed to a second sector 7 of the adsorption body 2 during normal operation. When the desorption gas 17 passes through the adsorption body 2, the low-boiling pollutants adsorbed by the adsorption body 2 are desorbed and given off to the desorption gas 17. In other words, the pollutants desorbing at a temperature of 200 ° C. desorb from the adsorption body 2.
    In this embodiment, the desorption gas 17 is formed in a mixer 14, in which hot clean gas 19 exiting from the reaction chamber 11 of the aftertreatment system 10 and preheated exhaust gas 15 or preheated ambient air 20 are mixed.
    In this embodiment, the hot clean gas 19 mainly flows into the chimney via main flaps. Only a partial flow of the clean gas 19 from the reaction chamber 11 is used in the mixer 14 to heat the exhaust gas 15 fed to the mixer 14, possibly the ambient air 20 fed to the mixer 14 and, if appropriate, that fed to the mixer 14
    Oxidizing gas 25 or oxidizing agent 24 is used.
    According to this embodiment, the oxidizing gas 25 or the oxidizing agent 24 is introduced into the mixer 14.
    The exhaust gas 15 or the ambient air 20 which enters the mixer 14 is first fed to a third sector 9 of the adsorption body 2, which was previously heated by the supply of the desorption gas 17. As a result, the heat generated by the desorption gas 17 as it passes through the adsorption body 2 can be applied to the latter
    can be partially recovered.
    To remove high-boiling pollutants adsorbed by the adsorption body 2, an oxidizing gas 25 containing an oxidizing agent 24 is fed to the second sector 7 of the adsorption body 2. The supply of oxidizing gas 25 can take place continuously and discontinuously, for example quarterly or monthly for a few hours.
    If necessary, it is provided that the oxidation gas 25 is supplied to the adsorption body 2 in a maintenance operation. In this maintenance operation, no exhaust gas 15 can be fed to the adsorption body 2 and the adsorption body 2 can
    be rotated continuously or discontinuously, in particular stepwise.
    If necessary, provision is made for the adsorption body 2 to be removed and dismantled before the oxidizing gas 25 is supplied from the exhaust gas cleaning system 1. The adsorption body 2 or the adsorption body parts can be heated to a temperature of 200 ° C. prior to the supply of the oxidizing gas 25.
    In this embodiment, ozone is used as the oxidizing agent 24 and the ozone is added to the desorption gas 17 in the mixer 14. The concentration of the oxidizing agent 24 in the desorption gas 17 is 700 ppm according to this embodiment. Since the entire desorption gas 17 contains oxidizing agent 24, the desorption gas 17 containing the oxidizing agent 24 is essentially supplied to the entire second sector 7 of the adsorption body 2.
    According to this embodiment, the desorption gas 17 containing the oxidizing agent 24 is fed to the adsorption body 2 at a temperature of 200 ° C. and a flow rate of 5 m / s. The second sector 7 is also heated to a temperature of 150 ° C. up to and including 200 ° C. before the oxidizing agent 24 is supplied.
    After passing through the adsorption body 2, the concentrated desorption gas 18, which optionally contains the desorbed low-boiling pollutants, optionally the desorbed high-boiling pollutants, the desorption gas 17 and optionally unconverted oxidizing agent 24, is fed to the aftertreatment system 10. In the aftertreatment system 10, the concentrated desorption gas 18 is converted into pure gas 19. In other words, unused oxidizing agent 24 is also consumed or converted in the aftertreatment system 10.
    In order to improve and / or accelerate the removal of the high-boiling pollutants, the direction of flow of the desorption gas 17 containing the oxidizing agent 24 flowing through the adsorption body 2 is changed, in particular vice versa. Here, the adsorption body 2 is for a first period in a first direction, in particular from its desorption inlet side 3 in the direction
    its desorption outlet side 4, and for a second period of time in a second
    Direction, in particular from its desorption outlet side 4 in the direction of its desorption inlet side 3, flows through.
    The method according to the invention enables the use of an adsorption body 2, in particular a so-called zeolite rotor, for exhaust gases 15 which contain high-boiling pollutants. In particular, it is possible with the method according to the invention to free the zeolite rotors from high-boiling pollutants
    and to keep their cleaning performance constant.
    FIG. 2 shows a schematic graphic representation of the second embodiment of the exhaust gas cleaning system 1 according to the invention, which is set up to carry out the method according to the invention. The features of the embodiment according to FIG. 2 can preferably correspond to the features of the embodiment according to FIG.
    According to this embodiment, the oxidizing gas 25 is fed to only a partial area of the second sector 8 of the adsorption body 2. Furthermore, the oxidizing gas 25 is formed by adding the oxidizing agent 24 to a partial flow of the desorption gas 17. The addition of the oxidizing agent 24 to the partial flow of the desorption gas 17 can take place, for example, in a static mixer.
    Since the oxidizing gas 25 is only supplied to a partial area of the second sector 8, the oxidizing gas 25 in the second sector 7 is essentially completely surrounded by the remaining desorption gas 17. As a result, contact between the oxidizing gas 25 and system parts which are not resistant to oxidizing agents can
    be prevented.
    FIG. 3 shows a schematic graphic representation of the third embodiment of the exhaust gas cleaning system 1 according to the invention, which is set up to carry out the method according to the invention. The features of the embodiment according to FIG. 3 can preferably correspond to the features of the embodiments according to FIGS. 1 or 2.
    21739
    As in the second embodiment, the oxidizing gas 25 is only in one
    Part of the second sector 8 of the adsorption body 2 is supplied.
    In this embodiment, a device for supplying the oxidizing gas 25 is temporarily connected to the exhaust gas cleaning system 1. This device is designed as a mobile module and comprises a feed device 21 which is set up to feed the oxidizing gas 25 to the sub-area of the second sector 8 and a discharge device 22 which is set up to remove the oxidizing gas 25 containing the desorbed pollutants from the sub-area of the second Sector 8 to be removed and fed to the aftertreatment system 10.
    The device further comprises a generating device which is set up to generate an oxidizing agent 24 or the oxidizing gas 25. According to this embodiment, the device is connected to the exhaust gas cleaning system 1 in such a way that a partial flow of the desorption gas 17 is fed to the generating device of the device. In this generating device, an oxidizing agent 24 is added to the partial flow of the desorption gas 17 and the oxidizing gas 25 is thereby formed.
    Furthermore, the device comprises a conversion device 13, in particular an ozone destruction catalyst, which is set up to consume or convert the oxidizing agent 24 of the oxidizing gas 25. According to this embodiment, the concentrated oxidizing gas 25, which, among other things, contains the desorbed high-boiling pollutants and possibly unused oxidizing agent 24, is fed to the ozone destruction catalytic converter via the discharge device 22.
    According to this embodiment, the direction of flow of the oxidizing gas 25 can be changed by controlling four butterfly valves.
    The configurations described can be provided in all embodiments
    be.
    The effects according to the invention can be achieved by these exemplary configurations
    be achieved. The invention is not limited to the illustrated embodiments, but rather
    includes any method, apparatus and arrangement 23 according to the following claims.
    权利要求:
    Claims (1)
    [1]
    Claims
    1. A method for cleaning exhaust gas (15) laden with high-boiling organic pollutants by means of an exhaust gas cleaning system (1) with at least one rotatable and essentially cylindrical adsorption body (2),
    - wherein in normal operation the exhaust gas (15) is fed to a first sector (6) of the adsorption body (2), the pollutants of the exhaust gas (15) in the first sector (6) as the exhaust gas (15) passes through the adsorption body ( 2) are adsorbed by the adsorption body (2) and the cleaned exhaust gas (16) resulting from this is discharged from the first sector (6),
    - In normal operation, a second sector (7) of the adsorption body (2) is supplied with desorption gas (17) for desorption of the adsorbed low-boiling pollutants, in the second sector (7) the low-boiling pollutants adsorbed on the adsorption body (2) when the desorption gas passes through ( 17) are desorbed by the adsorption body (2) and the desorption gas (18) thus concentrated is fed to an aftertreatment system (10) and converted to clean gas (19),
    characterized,
    - That the adsorption body (2) is supplied with an oxidizing agent (24) containing oxidizing gas (25) for removing high-boiling pollutants adsorbed on the adsorption body (2).
    2. The method according to claim 1, characterized in that the adsorption body (2) is cylindrical, and that the adsorption body (2) is rotated about its axis of rotation (5).
    3. The method according to claim 1 or 2, characterized in - that the adsorption body (2) of the exhaust gas cleaning system (1) is a so-called zeolite rotor or a so-called zeolite rotor concentrator wheel,
    24/39
    - and / or that the exhaust gas cleaning system (1) comprises fixed and sealed sectors (6, 7, 9), whereby the exhaust gas (15), the desorption gas (17), the oxidizing gas (25) and / or the ambient air (20) certain sectors (6, 7, 9) of the rotatable or rotating adsorption body (2) can be fed,
    - and / or that the aftertreatment system (10) is a regenerative thermal oxidation system.
    Method according to one of the preceding claims, characterized in that the oxidizing gas (25) is fed to the second sector (7), in particular to a sub-area of the second sector (8).
    Method according to one of the preceding claims, characterized in that the concentrated desorption gas (18) from the second sector (7), in particular from the sub-area of the second sector (8), a
    Aftertreatment system (10) is supplied.
    Method according to one of the preceding claims, characterized in that the oxidation gas (25) in the second sector (7) of desorption gas (17), essentially completely, flows around and / or around it
    becomes.
    Method according to one of the preceding claims, characterized
    marked,
    - That by introducing the oxidizing agent (24) into the desorption gas (17) the oxidizing gas (25) is generated,
    - Or that by introducing the oxidizing agent (24) into a partial flow
    of the desorption gas (17) the oxidizing gas (25) is generated.
    Method according to one of the preceding claims, characterized
    marked,
    - That the oxidizing gas (25) is fed to the adsorption body (2) during maintenance operation,
    11.
    12.
    25 - 58989 CTP Chemisch Thermische Prozesstechnik GmbH
    - That in the maintenance operation the adsorption body (2) is rotated continuously or discontinuously,
    - And that the supply of the exhaust gas (15) to the first sector (6) is blocked if necessary in the maintenance operation or, if necessary, in particular exclusively, ambient air (20) is supplied to the first sector (6).
    Method according to one of the preceding claims, characterized
    marked,
    - That before the supply of the oxidizing gas (25) the adsorption body (2) is broken down into parts of the adsorption body,
    - and / or that before the supply of the oxidizing gas (25) the adsorption body (2), the second sector (7), in particular the sub-area of the second sector (8), or at least one part of the adsorption body to a temperature in the range from 150 ° C to including 250 ° C, in particular to 200 ° C, is heated.
    Method according to one of the preceding claims, characterized
    marked,
    - That the concentration of the oxidizing agent (24) in the oxidizing gas (25) is in the range from 200 ppm to 1000 ppm, in particular in the range from 400 ppm to 800 ppm, and is preferably 600 ppm,
    - wherein the oxidizing agent (24) comprises ozone and / or hydrogen peroxide,
    - Or wherein the oxidizing agent (24) consists of ozone and / or hydrogen peroxide.
    Method according to one of the preceding claims, characterized
    marked,
    - That the oxidizing agent (24) is formed in a generating device,
    - or that the oxidizing agent (24) is supplied from a storage device to form the oxidizing gas (25).
    Method according to one of the preceding claims, characterized in that
    14th
    15th
    26 - 58989 CTP Chemisch Thermische Prozesstechnik GmbH
    - That the oxidizing gas (25) is fed to the adsorption body (2) at a temperature in the range from 150 ° C up to and including 250 ° C, preferably at a temperature of 200 ° C,
    - and / or that the adsorption body (2) is flowed against with a flow velocity of the oxidizing gas (25) in the range of 2 m / s up to and including 6 m / s, in particular 3 m / s up to and including 5 m / s.
    Method according to one of the preceding claims, characterized
    marked,
    - That the adsorption body (2) from its desorption outlet side (4) in the direction of its desorption inlet side (3) is flowed through with oxidizing gas (25),
    - and / or that the adsorption body (2) is flowed through from its desorption inlet side (3) in the direction of its desorption outlet side (4) with oxidizing gas (25),
    - and / or that the adsorption body (2) is flowed through for a first period of time in a first direction and the adsorption body (2) for a second period of time in a second, in particular the first direction opposite, direction with oxidizing gas (25).
    Method according to one of the preceding claims, characterized
    marked,
    - That the oxidizing gas (25), after flowing through the adsorption body (2), is fed to a conversion device (13), in particular an ozone destruction catalyst, in which the oxidizing agent (24) is consumed or converted,
    - or that the oxidizing gas (25), after flowing through the adsorption body (2), is fed to the aftertreatment system (10) in which the oxidizing agent (24) is consumed or converted.
    Method according to one of the preceding claims, characterized
    marked,
    27739
    - that in normal operation a third sector (9) of the adsorption body (2) is supplied with exhaust gas (15) or ambient air (20) which is supplied which is heated when passing through the adsorption body (2),
    - wherein the desorption gas (17) by mixing the clean gas (19) generated in the aftertreatment system (10) with the heated exhaust gas (15) emerging from the third sector (9) or with the heated ambient air emerging from the third sector (9) ( 20) is formed,
    - or the heated exhaust gas (15) exiting from the third sector (9) or the heated ambient air (20) exiting from the third sector (9) in an, in particular recuperative, heat exchanger with heat, in particular excess heat, from the reaction chamber (11 ) on the
    Desorption temperature is brought.
    16. The method according to any one of the preceding claims, characterized in,
    - That the aftertreatment system (10) comprises at least two heat-storing regenerators (12) connected to a reaction chamber (11),
    - That the concentrated desorption gas (18) and / or the contaminated oxidation gas (25) is converted into pure gas (19) in the reaction chamber (11),
    - and that the concentrated desorption gas (18) is alternately fed to the regenerators (12) in cycles.
    17. Device for supplying the oxidizing agent (24) or the oxidizing gas (25) to the adsorption body (2) according to a method according to any one of claims 1 to 16, characterized in that
    - That the device comprises a feed device (21),
    - wherein the feed device (21) is set up to feed an oxidizing gas (25) to the second sector (7), in particular to a sub-area of the second sector (8),
    - or wherein the feed device (21) is set up to feed an oxidizing agent (24) or an oxidizing gas (25) into the
    To bring in the exhaust gas purification system (1) so that the oxidizing gas (25) the second sector (7), in particular a sub-area of the second sector (8)
    is feedable.
    18. The device according to claim 17, characterized in that the device optionally comprises a discharge device (22) which is set up to remove the desorbed pollutants containing oxidizing gas (25) from the second sector (7), in particular from the sub-area of the second sector (8) to be fed to the aftertreatment system (10).
    19. Apparatus according to claim 17 or 18, characterized in that
    - that the device comprises at least one generating device which is set up to generate an oxidizing agent (24) or the oxidizing gas (25),
    - or that the device comprises at least one storage device containing the oxidizing agent (24) or the oxidizing gas (25), which storage device is set up to store the oxidizing agent (24) or the oxidizing gas (25).
    20. Device according to one of claims 17 to 19, characterized in that
    - That the device comprises at least one conversion device (13), in particular an ozone destruction catalyst, which is set up to consume or convert the oxidizing agent (24) of the oxidizing gas (25), and that the oxidizing gas (25) containing the desorbed pollutants via the The discharge device (22) of the at least one conversion device (13) can be fed.
    21. Device according to one of claims 17 to 20, characterized in that
    the device is a mobile module which is set up for temporary connection to the exhaust gas cleaning system (1).
    22. Regeneration device for supplying the oxidizing gas (25) to the adsorption body (2) or to at least one adsorption body part according to a method according to any one of claims 1 to 16, characterized in that, if necessary, the regeneration device is set up to the adsorption body (2) or to heat at least one adsorption body part (2) at least in sections to a temperature in the range from 150 ° C up to and including 250 ° C, in particular to 200 ° C,
    - and that the adsorption body (2) or the at least one adsorption body part in the regeneration device can be acted upon with oxidizing gas (25).
    23. Arrangement (23) comprising an exhaust gas purification system (1) and a device according to one of claims 17 to 21, characterized in that the feed device (21) of the device can be connected to the exhaust gas purification system (1) so that the oxidizing agent (24) or the oxidizing gas (25) can be introduced into the exhaust gas cleaning system (1) in such a way that the oxidizing gas (25) can be fed to the second sector (7), in particular a sub-area of the second sector (8).
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    同族专利:
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    引用文献:
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    DE4036354A1|1990-11-15|1992-05-21|Hasso Von Bluecher|Removing solvent vapour from off-gases contg. oil, grease etc. - by passing the gas through a wide-pore adsorption filter and then through a fine-pore adsorbent|
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    JP6420115B2|2014-10-17|2018-11-07|高砂熱学工業株式会社|Gas processing apparatus and function regeneration method of gas processing apparatus|CN112619368B|2020-12-07|2022-02-18|南京瑞宜恒环境科技有限公司|VOC waste gas treatment method|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    ATA50614/2019A|AT522330B1|2019-07-05|2019-07-05|Process and system for cleaning exhaust gases laden with organic pollutants|ATA50614/2019A| AT522330B1|2019-07-05|2019-07-05|Process and system for cleaning exhaust gases laden with organic pollutants|
    PCT/EP2020/066585| WO2021004730A1|2019-07-05|2020-06-16|Method and system for cleaning exhaust gases charged with organic contaminants|
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