EP3237802A1 - Dispositif et procédé de purification thermique des effluents gazeux - Google Patents

Dispositif et procédé de purification thermique des effluents gazeux

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Publication number
EP3237802A1
EP3237802A1 EP15813330.6A EP15813330A EP3237802A1 EP 3237802 A1 EP3237802 A1 EP 3237802A1 EP 15813330 A EP15813330 A EP 15813330A EP 3237802 A1 EP3237802 A1 EP 3237802A1
Authority
EP
European Patent Office
Prior art keywords
heat exchange
heat exchanger
gas
exchange medium
thermoreactor
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.)
Withdrawn
Application number
EP15813330.6A
Other languages
German (de)
English (en)
Inventor
Martin Schröter
Erhard Rieder
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
Duerr Systems AG
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Duerr Systems AG filed Critical Duerr Systems AG
Publication of EP3237802A1 publication Critical patent/EP3237802A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
    • F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
    • F01D15/10—Adaptations for driving, or combinations with, electric generators
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K11/00—Plants characterised by the engines being structurally combined with boilers or condensers
    • F01K11/02—Plants characterised by the engines being structurally combined with boilers or condensers the engines being turbines
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/10—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle with exhaust fluid of one cycle heating the fluid in another cycle
    • 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
    • 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
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/02—Integration in an installation for exchanging heat, e.g. for waste heat recovery
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste

Definitions

  • the present invention relates to an apparatus and a method for thermal exhaust gas cleaning, in particular for cleaning a mine exhaust gas or a mine exhaust air, especially a methane-containing mine ventilation gas.
  • the present invention can also be used for the thermal cleaning of other flammable or exhaust gases containing combustible constituents, in particular volatile organic components (VOCs).
  • VOCs volatile organic components
  • thermoreactor for purifying mine exhaust gases, especially methane-containing mine ventilation gases (VAM), and to supply the hot gas resulting from the thermal oxidation process to an energy recovery device.
  • VAM methane-containing mine ventilation gases
  • CN 102733872 A proposes to use the heat energy of the hot gas to produce or further heat water vapor used to drive a steam turbine coupled to a generator for generating electrical power.
  • the inventors have recognized that the energy efficiency of this process, as well as many other heat exchange processes, is limited by the exclusive use of the gross calorific value or the enthalpy difference between a heat exchange entry temperature and a heat exchange exit temperature.
  • the use of the calorific value (lower calorific value) of fuels or the general use of the condensation energy of moist constituents of the (waste) gas is limited by the operating conditions of the secondarily generated energy form. This also applies, for example, to the generation of steam in the boiler operation of a power generation process.
  • the invention has for its object to provide an improved apparatus and an improved method for thermal exhaust gas purification, which have an improved energy balance.
  • the device according to the invention for thermal exhaust gas purification has a thermal reactor to which a raw gas to be purified can be supplied and in which the raw gas supplied is thermally cleanable, and an energy recovery device to which a gas purified in the thermoreactor can be supplied via at least one discharge line.
  • the energy recovery device in turn has at least one condensation heat exchanger in which the purified gas can be cooled in such a way that condensable substances contained in the purified gas condense and enthalpies released in this way can be released to a heat exchange medium and / or the raw gas upstream of the thermoreactor.
  • the thermoreactor has a combustion chamber in which the raw gas supplied is thermally cleanable.
  • the energy recovery device is preferably connected to the combustion chamber of the thermoreactor via a discharge line in order to supply the energy recovery device with a purified gas produced during the thermal cleaning process in the combustion chamber.
  • the energy recovery device preferably has a further heat exchanger in which the purified gas can be cooled to a first temperature level and an enthalpy released in this way can be delivered to a heat exchange medium, and the condensation heat exchanger downstream of the other Heat exchanger is arranged and in which the purified gas to a second temperature level lower than the first temperature stage is further cooled, so condense contained in the purified gas condensables, and released enthalpies to a heat exchange medium and / or the raw gas upstream of the thermoreactor can be issued , on.
  • thermoreactor is a thermal oxidation reactor, which is preferably designed for regenerative thermal oxidation (RTO) and exemplified in WO
  • thermoreactor may in this context, in particular a RTO reactor with two, three, four or more
  • the inventive method for thermal exhaust gas purification includes the steps of thermal cleaning of a raw gas to be purified in a thermoreactor; and cooling a purified gas resulting from the thermal purification process in the thermoreactor in a condensation heat exchanger to condense condensables contained in the purified gas, releasing released enthalpies to a heat exchange medium and / or the raw gas upstream of the thermoreactor.
  • the thermal cleaning of the raw gas takes place in a combustion chamber of the thermoreactor.
  • the purified gas produced in the thermal combustion process in the combustion chamber is preferably in a further heat exchanger to a first
  • the purified gas is preferably further cooled in the condensation heat exchanger downstream of the further heat exchanger to a second temperature level lower than the first temperature stage, so that condense condensables contained in the purified gas, and released enthalpies to a Heat exchange medium and / or the raw gas are discharged upstream of the thermoreactor.
  • the thermal cleaning of the raw gas takes place in a thermal
  • Oxidation reactor which is preferably designed for regenerative thermal oxidation (RTO) and described by way of example in WO 2008/011965 AI the applicant, the content of which in this respect is fully made the subject of the present invention.
  • the thermoreactor may in this context be in particular an RTO reactor with two, three, four or more regenerators or containers.
  • a first heat exchanger further heat exchanger of the invention
  • an enthalpy difference between the inlet temperature and the outlet temperature (first temperature step of the invention) of the purified hot gas into and out of the first heat exchanger can be utilized.
  • the second heat exchanger in the second heat exchanger
  • Condensation heat exchanger of the invention of the energy recovery device by condensation of the moisture in the hot gas and the inherent enthalpy of the hot gas evaporation are used.
  • the type of condensing second heat exchanger for example about 60-70% of the temperature difference between the outlet temperature of the hot gas from the first heat exchanger and the condensation temperature of the moisture (typically water vapor) and the enthalpy of vaporization can be transferred to the heat exchange medium.
  • the thermal cleaning process should in this context include all types of cleaning processes in which heat energy is supplied to the raw gas to be purified. These include, in particular, thermal oxidation processes of combustible substances contained in the raw gas to be purified.
  • the discharge line comprises, in particular, a so-called clean gas line, through which the gases purified in the thermoreactor, after flowing through the Regenerators with appropriate cooling (to eg about 70 ° C) are discharged as so-called clean gas from the thermoreactor, and a so-called hot gas line, through which the cleaned gases in the thermoreactor after thermal cleaning in the thermoreactor with appropriate heating (for example, about 1,000 ° C) are discharged as so-called hot gas from the combustion chamber of the thermoreactor.
  • the purified gas in this context comprises in particular the so-called clean gas and the so-called hot gas.
  • the energy latently contained in the (raw) gas in the form of relative humidity should also be determined by means of an RTO reaction.
  • the raw gas to be supplied to the exhaust gas purification system can be used in the reactor downstream of the condensation heat exchanger, thus improving the energy balance of the entire process n in addition to gaseous components also contain a significant amount of moisture (in the form of condensable substances). It can the
  • thermoreactor downstream condensation heat exchanger now uses this latent heat stored, so that the overall efficiency of the system can be recycled with moist, vapor-saturated crude gases to a level that corresponds to that typical TNV plants in the implementation of substantially arid raw gases. That is, the present invention is particularly advantageous for use in processes in which the crude gas supplied to the thermoreactor contains liquid droplets, but without being limited to this application.
  • the further heat exchanger and the condensation heat exchanger are in heat exchange with a common heat exchange medium circuit.
  • the condensation heat exchanger in the common heat exchange medium circuit is preferably arranged upstream of the further heat exchanger, and the heat exchange medium of the common heat exchange medium circuit can preferably be preheated in the condensation heat exchanger.
  • the further heat exchanger is in heat exchange with a first heat exchange medium circuit and is the
  • Condensation heat exchanger with a second, separate from the first heat exchange medium circuit heat exchange medium circuit in heat exchange.
  • the further heat exchanger is in heat exchange with a first heat exchange medium circuit and is the
  • Condensation heat exchanger provided, which is in heat exchange with a Rohgaszumoltechnischebergheatskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyinskyin
  • a power generating device is arranged in the common heat exchange media circuit or the first heat exchange medium circuit downstream of the further heat exchanger. That the heated in the further heat exchanger heat exchange medium is preferably used to generate electricity.
  • the power generating device preferably has a steam turbine connected to the circuit and a generator coupled to the steam turbine for generating electric power.
  • At least one hot and / or hot water consumer and / or a district heating connection are arranged in the second heat exchange medium circuit downstream of the condensation heat exchanger.
  • the heat exchange medium of the second heat exchanger is preferably a process water or a heating medium.
  • the second heat exchange medium circuit serves as a heat source for the operation of an ORC system.
  • an intermediate medium for example a thermal oil
  • the second heat exchange medium cycle may be a working medium cycle of an ORC plant, the second heat exchanger acting as an evaporator for a working medium ORC plant can work.
  • a condensate produced in the condensation heat exchanger of the energy recovery device can be returned to the process via condensate removal.
  • the condensate may be supplied to a heat exchange medium circuit as a heat exchange medium.
  • the condensation heat exchanger of the energy recovery device transfers the residual and / or condensation enthalpy to the raw gas stream to be treated, especially methane-containing mine ventilation gas (VAM), before it enters the thermoreactor.
  • VAM methane-containing mine ventilation gas
  • small amounts of drops contained in the crude gas stream can be evaporated.
  • the thermoreactor correspondingly more energy for primary energy recovery in the other heat exchanger can be withdrawn.
  • alternative or supplementary embodiment of the invention utilizes the
  • Condensation heat exchanger of the energy recovery device the residual and / or condensation enthalpy of the (regenerative) thermoreactor via a clean gas discharge line effluent, purified clean gas flow as a heat source and transfers them to a heat exchange medium in the second heat exchange medium cycle.
  • This variant can be particularly advantageous if an outlet temperature of the clean gas flow in the
  • Clean gas discharge line is above the dew point of a vapor component in the exhaust stream, in particular min. 80 ° C, preferably min. 90 ° C, preferably min. 100 ° C or higher.
  • both the exhaust gas flow from the clean gas discharge line and the hot gas leaving the further heat exchanger are supplied to the condensation heat exchanger as heat source for heat transfer to the heat medium in the second heat exchange medium cycle.
  • the energy recovery device in addition to the aforementioned heat exchangers in a sequential arrangement in the hot gas line also a further heat exchanger for condensation of moisture having the pure gas flowing out in the clean gas line, so that the enthalpy of vaporization inherent in this clean gas is also usable.
  • This variant can be particularly advantageous if an outlet temperature of the (cooler) clean gas flow in the clean gas line is above the dew point of a vapor component in the exhaust gas stream, in particular min. 80 ° C, preferably min. 90 ° C, preferably min. 100 ° C or higher.
  • the apparatus of the invention described above and the method of the invention described above can be used in a particularly advantageous manner for cleaning a mine exhaust gas, in particular a methane-containing mine ventilation gas (VAM).
  • VAM mine ventilation gas
  • the ventilation air of coal mines is admixed with moisture of the order of, for example, 30 to 35% by volume in order to reduce the formation of underground dust during the intake process.
  • the invention utilizes the enthalpy of this moisture in the effluent of the thermoreactor in energy recovery.
  • Fig. 1 is a schematic representation of the construction of a thermal exhaust gas purification device according to a first embodiment of the invention
  • Fig. 2 is a schematic view of the structure of a thermal exhaust gas purification device according to a second embodiment of the invention.
  • FIG. 3 is a schematic view of the structure of a thermal exhaust gas purification device according to a third embodiment
  • FIG. 4 is a schematic view of the structure of a thermal exhaust gas purification device according to a fourth embodiment
  • Fig. 5 is a schematic view of the structure of a thermal exhaust gas purification device according to a fifth embodiment
  • FIG. 6 is a schematic diagram of the structure of a thermal exhaust gas purification device according to a sixth embodiment
  • Fig. 7 is a schematic representation of the structure of a thermal exhaust gas purification
  • Fig. 8 is a schematic representation of the structure of a thermal exhaust gas purification
  • Fig. 1 shows a system for purifying a methane-containing mine ventilation gas (VAM) according to a first embodiment of the present invention.
  • VAM methane-containing mine ventilation gas
  • the system illustrated in FIG. 1 also has, in particular, numerous (control) valves and sensors (in particular temperature sensors) which have been omitted for the sake of simplicity, but which are described, for example, in WO 2008/011965 AI are known.
  • the thermal emission control device of FIG. 1 includes a thermal reactor 10 for regenerative thermal oxidation (RTO) of combustibles in an exhaust or exhaust stream.
  • the thermoreactor 10 has a combustion chamber 12 and two regenerators 14 arranged below the combustion chamber 12, each of which comprises an antechamber and a heat storage mass chamber arranged above the prechamber.
  • the thermoreactor 10 has two regenerators 14, but in other embodiments, three, four or more regenerators 14 may be provided below the combustion chamber 12.
  • the combustion chamber 12 of the thermal reactor 10 projects a burner 16, which are supplied via a gas supply 18 fuel gas and combustion air.
  • the burner 16 serves to burn the pollutants (e.g., methane) contained in the raw gas to be purified.
  • the temperature in the combustion chamber 12 can be up to about 1000 ° C., depending on the energy content of the combustible substances contained in the raw gas.
  • each regenerator 14 of the thermoreactor 10 is connected via a Rohgaszweig effet 20 with a Rohgaszu09 effet 22.
  • An exhaust gas source 24, for example in the form of an exhaust gas collecting and exhaust mixing device feeds the raw gas supply line 22 with the exhaust gas (raw gas) to be cleaned.
  • the exhaust gas to be purified which is supplied to the regenerators 14 of the thermoreactor 10 via the raw gas branch lines 20, usually contains liquid droplets. These drops of liquid originate, for example, from the upstream process 24. This state can also occur, for example, if the temperature difference between the upstream Process 24 and the raw gas inlet into the emission control system at the transfer point from the RohgaszuQuerytechnisch 22 in the Rohgaszweig Oberen 20 condensation of the moisture contained in the raw gas result, which are delivered in the resulting gas stream at the outlet of Rohgaszweig Oberen 20 in the thermoreactor 10 as liquid drops.
  • each regenerator 14 of the thermoreactor 10 is connected via a respective clean gas branch line 26 to a clean gas line (first discharge line of the invention) 28.
  • the cleaned in the thermoreactor 10 and cooled in the regenerator 14 gas (clean gas) is passed through the clean gas line 28 to an exhaust chimney 30 through which the clean gas is discharged to the environment.
  • thermoreactor The operation of such a thermoreactor is described, for example, in WO 2008/011965 AI in more detail. In this regard, reference is made in full to this document.
  • the combustion chamber 12 of the thermoreactor 10 via hot gas branch lines 32 with a hot gas line (second discharge line of the invention) 34 is connected.
  • a hot gas line 34 hot exhaust gas (hot gas) purified by thermal oxidation is conducted past the regenerator 14 or removed from the exhaust gas purification device before passing through a regenerator 14.
  • the hot gas is supplied via the hot gas line 34 to an energy recovery device.
  • This energy recovery device has a first heat exchanger 36 (another heat exchanger of the invention) and a second heat exchanger 38 (condensation heat exchanger of the invention) downstream of the first heat exchanger 36. Both heat exchangers 36, 38 are in heat exchange with a common heat exchange medium circuit 40a.
  • the first heat exchanger 36 serves as a steam generator or steam heater.
  • the hot gas of, for example, about 1,000 ° C to, for example, about 400 ° C (first Temperature level) cooled.
  • the first temperature level may also be below 400 ° C, for example at about 300 ° C, 200 ° C or even about 150 ° C.
  • the enthalpy released during this cooling is used in the first heat exchanger 36 to heat up the heat exchange medium (here: water) of the circuit 40a to vaporization and overheating of the vapor.
  • the overheated by the first heat exchanger 36 steam is supplied in the circuit 40 a steam turbine 42.
  • This steam turbine 42 is coupled to a generator 44 for generating electricity in order to generate electrical energy in a known manner.
  • a cooling tower 43 Downstream of the steam turbine 42, a cooling tower 43 is preferably provided for further cooling of the water.
  • the hot gas exiting from the first heat exchanger 36 is further cooled, for example to about 60 ° C (second temperature level). During this cooling process, the moist components of the hot gas condense.
  • the second heat exchanger 38 can be inexpensively made of carbon or plastic material.
  • Such heat exchangers are known, for example, from WO 2009/007065 A1, the disclosure of which is to be included here.
  • the hot gas gives it its inherent enthalpy between inlet and outlet temperature in and out of the second heat exchanger 38, the enthalpy of enthalpy of the moisture contained in the hot gas by condensation, and the inherent enthalpy of the condensate between inlet and outlet temperature in or out of the second heat exchanger 38 free.
  • the sum of these released enthalpies is released to the heat exchange medium of the circuit 40a to preheat the heat exchange medium.
  • the exhaust gas purification device described above enables efficient energy recovery, in particular also in the event that the raw gas supplied via the raw gas branch lines 20 is supersaturated and contains moisture in the form of liquid droplets.
  • thermoreactor During the heating process in the thermoreactor these liquid droplets are vaporized. If the evaporation product in the thermoreactor releases no reaction energy, as is the case, for example, for water, which can pass through the thermoreactor as steam, the evaporation enthalpy used for the evaporation of the liquid is recovered in the condensation heat exchanger 38 by condensation and in this embodiment to a Heating medium delivered for further use.
  • the emerging from the second heat exchanger 38 hot gas is finally fed via a connecting line 46 of the clean gas line 28 to be ultimately discharged through the exhaust chimney 30 to the environment.
  • the exhaust air flow in the exhaust chimney 30 is also relatively dry due to the condensation heat exchanger 38 used in the energy recovery device.
  • the condensate formed during cooling of the hot gas in the second heat exchanger 38 can optionally be returned to the process via a condensate removal 48.
  • the condensate can be supplied to the circuit 40a as a heat exchange medium.
  • Fig. 2 shows a system for purifying a methane-containing mine ventilation gas according to a second embodiment of the present invention.
  • the same or analogous components are identified by the same reference numbers and a repetition of the corresponding descriptions is dispensed with.
  • the exhaust gas purification device illustrated in FIG. 2 is different from that of the first embodiment by the energy recovery device.
  • the first heat exchanger 36 (another heat exchanger of the invention) of the energy recovery device is in heat exchange with a first heat exchange medium circuit 40b.
  • This first heat exchange medium circuit 40b contains, like the common heat exchange medium circuit 40a of the first embodiment, a power generation device comprising a steam turbine 42 and a generator 44 and a cooling tower 43.
  • the second heat exchanger 38 (condensation heat exchanger of the invention) of the energy recovery device is in heat exchange with a second heat exchange medium circuit 40c, which is configured as an open circuit and separately to the first heat exchange medium circuit 40b.
  • the heat exchange medium of the second heat exchange medium circuit 40c is, for example, service water which is supplied to a hot water consumer or a heating medium which is supplied to a district heating connection.
  • the heat exchange medium of the second heat exchange medium circuit 40c is a thermal oil of an intermediate circuit for
  • the second heat exchanger 38 serves as a direct evaporator for a working medium, in particular an organic working medium for operating a system according Rankine cycle, preferably the Rankine turbine drives a generator. In this way, an efficiency of
  • Electricity generation of the entire system comprising the steam turbine 42 and the Rankine turbine, be increased.
  • Fig. 3 shows a system for purifying a methane-containing mine ventilation gas according to a third embodiment of the present invention. Here are the same or
  • the exhaust gas purification device illustrated in FIG. 3 is different from those of the first two embodiments by the energy recovery device.
  • the first heat exchanger 36 of the energy recovery device is in heat exchange with a first heat exchange medium circuit 40b.
  • This first heat exchange medium circuit 40b includes, like the common heat exchange medium circuit 40a of the first embodiment and the first heat exchange medium circuit 40b of the second embodiment, a power generation device comprising a steam turbine 42 and a generator 44 and a cooling tower 43.
  • the second heat exchanger (condensation heat exchanger) 38 of the energy recovery device is in heat exchange with the raw gas stream delivered by the exhaust gas source 24, specifically methane-containing mine ventilation gases (VAM).
  • VAM methane-containing mine ventilation gases
  • the second heat exchanger 38 is arranged upstream of the thermoreactor 10 in the raw gas supply line 22.
  • the hot gas exiting the first heat exchanger 36 is cooled, for example, from about 300 ° C to about 200 ° C.
  • FIG. 4 shows a system for purifying a VOC-containing exhaust air of an exhaust gas source 24, for example a methane-containing mine ventilation gas or a solvent-containing process exhaust air, according to a fourth exemplary embodiment of the present invention.
  • an exhaust gas source 24 for example a methane-containing mine ventilation gas or a solvent-containing process exhaust air
  • the same or analog components are identified by the same reference numerals and a repetition of the corresponding descriptions is omitted.
  • the exhaust gas purification device illustrated in FIG. 4 differs from the first exemplary embodiment according to FIG. 1 in that the cooler clean gas discharged via the clean gas line (eg about 70 ° C.) is mixed with the hot gas emerging from the first heat exchanger 36 of the energy recovery device (eg about 300 ° C) is mixed before this mixed clean gas (eg, about 180 ° C) downstream in the second heat exchanger
  • (Condensation heat exchanger) 38 enters as a heat source.
  • the mixed clean gas on the dew point of a vapor component, in particular Steam, cooled so that the stored in both partial streams evaporation enthalpy can be transferred to the circulating in the common heat exchange medium circuit 40 d heat exchange medium.
  • the admixture or supply of the gas streams via a mixing and / or swirling device is supported.
  • an advantageous mixing, in particular homogenization of the mixture of the differently tempered gas streams can be promoted.
  • the residual and / or enthalpy of vaporization of the gas mixture can also be transferred to a heat exchange medium circulating in the second heat exchange media circuit 40c.
  • the thus characterized variants are particularly suitable when the mixture formation between the hot gas of the first temperature stage and the cooler clean gas exit temperature from the thermoreactor 10, a mixture temperature of less than 250 ° C can be set, resulting in an advantageous and cost-effective implementation of the second heat exchanger according to the nature of WO 2009/007065 Al leads.
  • 5 shows a system for purifying a VOC-containing exhaust air of an exhaust gas source 24, for example a methane-containing mine ventilation gas or a solvent-containing process exhaust air, according to a fifth exemplary embodiment of the present invention.
  • the same or analog components are identified by the same reference numerals and a repetition of the corresponding descriptions is omitted.
  • the exhaust gas purification device illustrated in FIG. 5 differs from the second exemplary embodiment according to FIG. 2 in that a third heat exchanger 50 is provided in the clean gas line 28.
  • a third heat exchanger 50 condensation heat exchanger of the invention
  • Pure gas emerging from the thermoreactor 10 via the clean gas line 28
  • Pure gas further cooled, for example, to about 60 ° C (corresponding to the second temperature stage of the second heat exchanger 38).
  • the moist constituents of the pure gas condense, whereby a residual and / or enthalpy of vaporization of the pure gas can be transferred to a heat exchange medium.
  • the first heat exchanger 36 and the second heat exchanger 38 are in heat exchange with a common heat exchange medium circuit 40a (similar to the first exemplary embodiment of FIG. 1).
  • the second heat exchanger 38 and the third heat exchanger 50 are cooperatively communicated through a common heat exchange medium circuit 40e, and the heat exchange medium is preheated in the third heat exchanger 50.
  • all three heat exchangers 36, 38, 50 are in operative relationship via a common heat exchange medium circuit, whereby vapor formation for driving the steam turbine 42 can be advantageously maximized.
  • the second heat exchange medium circuit 40f is designed as a working medium circuit of a Rankine cycle.
  • the working medium and thus the second heat exchange medium is preferably an organic working medium, which in particular at lower temperature levels has more favorable evaporation properties than the medium water of the steam turbine 42.
  • the second heat exchanger 38 serves as an evaporator for the working medium, which subsequently via a Rankine turbine 54 is relaxed.
  • the Rankine turbine 54 drives another generator 56.
  • Generator 44 is in operative relationship, which could be dispensed with a second generator.
  • the relaxed in the Rankine turbine 54 working fluid is further cooled by a capacitor 58 so that it condenses out again. Subsequently, it is supplied in predominantly liquid form to the third heat exchanger 50.
  • the third heat exchanger 50 transmits the residual and / or enthalpy of vaporization of the clean gas of the thermal reactor 10 to the liquid working medium, as a result of which it is preheated and possibly even partially vaporized.
  • the second and / or third heat exchanger 38, 50 is designed according to DE 10 2014 201 908 AI, in particular when integrating an RC / ORC system in the manner of a flow apparatus or a system of flow apparatuses.
  • the disclosure of DE 10 2014 201 908 AI is hereby incorporated in full, in particular concerning the structure of the flow apparatus, the flow guide in the flow apparatus, a system of flow apparatus and the operating method for fluid guidance in
  • thermoreactors 10 without hot gas use via the second discharge line 34 and an energy recovery device in the sense of the embodiments of FIGS. 1 to 6 and WO 2008/011965 Al, it may also be useful and advantageous, a condensation heat exchanger 60 (for example, according to Art of the third heat exchanger 50 according to the example of FIG. 5) in the first discharge line 28, as illustrated in FIG. 7 as the seventh embodiment.
  • a condensation heat exchanger 60 for example, according to Art of the third heat exchanger 50 according to the example of FIG. 5 in the first discharge line 28, as illustrated in FIG. 7 as the seventh embodiment.
  • the clean gas flowing out in the clean gas line 28 cools in the condensation heat exchanger 60 below a dew point of a vapor component.
  • the residual and / or enthalpy of vaporization which has not been recovered in the regenerators 14 of the regenerative thermal reactor 10, can be transferred to a heat exchange medium of a corresponding heat exchange medium circuit 40g.
  • the incoming raw gas are preheated analogously to the embodiment according to FIG.
  • another heat user for example a hot or hot water supply or an ORC system, can be supplied with thermal energy.
  • 8 shows an eighth embodiment of an exhaust gas purification device according to the invention, a further modification of the embodiment of Fig. 1. In this case, the same or analogous components are denoted by the same reference numerals and a repetition of the corresponding descriptions is omitted.
  • the exhaust gas purification device illustrated in FIG. 8 is different from that of the first embodiment by the energy recovery device.
  • the first heat exchanger 36 and the second heat exchanger 38 are in heat exchange with a common heat exchange medium circuit 40h.
  • the heat exchange medium downstream of the steam turbine 42 is fed to a further condensation heat exchanger 64, which is arranged upstream of the thermoreactor 10 in the raw gas supply line 22.
  • the heat exchange medium cooled in this further condensation heat exchanger 64 to, for example, approximately 60 ° C. is then fed back to the condensation heat exchanger 38 upstream of the first heat exchanger 36.

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Treating Waste Gases (AREA)

Abstract

L'invention concerne un dispositif de purification thermique des gaz d'échappement qui possède au moins un thermoréacteur (10) auquel est acheminé un gaz brut à purifier et dans lequel le gaz brut acheminé est soumis à une purification thermique, et un appareil de récupération d'énergie auquel un gaz purifié dans le thermoréacteur est acheminé par le biais d'au moins une conduite d'évacuation (28, 34). Selon l'invention, en vue d'améliorer le bilan énergétique, l'appareil de récupération d'énergie possède au moins un échangeur de chaleur à condensation (38, 50, 60, 64) dans lequel le gaz purifié est refroidi de telle sorte que les substances pouvant se condenser qui sont contenues dans le gaz purifié se condensent et les enthalpies ainsi libérées sont délivrées à un fluide d'échange de chaleur et/ou au gaz brut en amont du thermoréacteur (10).
EP15813330.6A 2014-12-22 2015-12-15 Dispositif et procédé de purification thermique des effluents gazeux Withdrawn EP3237802A1 (fr)

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DE102014226882 2014-12-22
DE102015205516.7A DE102015205516A1 (de) 2014-12-22 2015-03-26 Vorrichtung und Verfahren zur thermischen Abgasreinigung
PCT/EP2015/079685 WO2016102231A1 (fr) 2014-12-22 2015-12-15 Dispositif et procédé de purification thermique des effluents gazeux

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EP (1) EP3237802A1 (fr)
CN (1) CN107407483A (fr)
AU (1) AU2015371529B2 (fr)
DE (1) DE102015205516A1 (fr)
WO (1) WO2016102231A1 (fr)

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US20170276347A1 (en) 2017-09-28
WO2016102231A1 (fr) 2016-06-30
US10429066B2 (en) 2019-10-01
AU2015371529B2 (en) 2020-08-13
AU2015371529A1 (en) 2017-07-06
CN107407483A (zh) 2017-11-28
DE102015205516A1 (de) 2016-06-23

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