Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
  • F23C13/00—Apparatus in which combustion takes place in the presence of catalytic material
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
  • F23C9/00—Combustion apparatus characterised by arrangements for returning combustion products or flue gases to the combustion chamber
• • 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
  • F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
  • F23L15/00—Heating of air supplied for combustion
  • F23L15/02—Arrangements of regenerators
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F28—HEAT EXCHANGE IN GENERAL
  • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
  • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
  • F28D21/0001—Recuperative heat exchangers
  • F28D21/0003—Recuperative heat exchangers the heat being recuperated from exhaust gases
  • F28D21/001—Recuperative heat exchangers the heat being recuperated from exhaust gases for thermal power plants or industrial processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2256/00—Main component in the product gas stream after treatment
  • B01D2256/22—Carbon dioxide
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
  • B01D53/34—Chemical or biological purification of waste gases
  • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
  • B01D53/86—Catalytic processes
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F28—HEAT EXCHANGE IN GENERAL
  • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
  • F28D19/00—Regenerative heat-exchange apparatus in which the intermediate heat-transfer medium or body is moved successively into contact with each heat-exchange medium
  • F28D19/04—Regenerative heat-exchange apparatus in which the intermediate heat-transfer medium or body is moved successively into contact with each heat-exchange medium using rigid bodies, e.g. mounted on a movable carrier
• • 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
  • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

• the invention relates to an apparatus for producing very pure carbon dioxide containing gas and thermal energy.
• the invention also relates to a method for producing carbon dioxide containing gas and thermal energy, as well as the use of such an apparatus and a method.
• Carbon dioxide can be used for a number of purposes. It can be directly applied in various uses, and on the other hand, it is suitable as a raw material for many processes. However, carbon dioxide is a problematic product, because emissions of it contribute to the greenhouse effect. Therefore, the controlled production of carbon dioxide is of primary importance.
• the content of CO 2 is about 380 ppm.
• the content of CO 2 will drop to a level of about 150 to 220 ppm if no supplementary CO 2 is added.
• the growth of, for example, cucumber, tomato and lettuces, as well as tulips has been found to increase by about 30 to 50% in a greenhouse.
• impurities in carbon dioxide containing gas slow down the growth of plants.
• nitrogen oxides at a level of 0.1 to 2 ppm block the fertilizing effect of supplementary CO 2 .
• the highest allowed levels range from 0.015 to 0.1 ppm, depending on the duration of exposure.
• ethene (C 2 H 4 ) the allowable limits are even more stringent, from
• Thermal energy and partly also carbon dioxide, is conventionally produced by burning to be used in, for example, greenhouses.
• the fuels suitable for this burning must be pure.
• the combustion takes place at a high temperature, and oxides of nitrogen and sulphur are easily formed as side products, and some of the ethene remains unburnt.
• the strict standards for purity of CO 2 hinder the application of gas produced in thermal combustion in greenhouses.
• Special Low NOx or Ultra Low NOx burners are needed to reach the level of 50 to 80 ppm in the production of nitrogen oxides. Even when strongly diluted, they do not meet the latest requirements set for plants.
• pure carbon dioxide containing gas is relatively expensive and involves relatively complex technology.
• pure carbon dioxide is used in the form of bottled gas or liquid. Used in this way, the costs of carbon dioxide become very high. The costs of the gas for a greenhouse may be almost in the order of the heating costs.
• the apparatus according to the invention which is suitable for producing thermal energy and very pure carbon dioxide (CO 2 ) containing gas, comprises at least one injector for injecting fuel and at least one main blower for supplying combustion air, and the production apparatus comprises at least one catalytic combustion unit with at least one catalytic burner for catalytic combustion of fuel effectively at a temperature of 350 to 850O in a retention time of 0.01 to 0.1 s, and at least one heat exchanger for at least partial transfer of heat from the gas produced in combustion to the combustion air and fuel to be supplied to the catalytic burner, and the production apparatus comprises at least one catalytic afterburner for at least partial after purification of the gas produced in combustion.
• Said at least one catalytic afterburner connected to the burning unit guarantees and improves the purification results of the catalytic burner further. It enables different ways of running, and even in connection with reversals, the gas
• the production apparatus comprises at least one gas recirculating device for guiding the gas formed in combustion at least partly to the main blower.
• This solution improves substantially the energy balance of the plant, because the need to heat combustion air is reduced; advantageously, the content of recirculated gas is greater than 50%, such as 70 to 90%.
• the catalytic production apparatus comprises gas guiding members for guiding the flow of gas from the first stage of the catalytic burner to a catalytic afterburner and/or to another stage of the catalytic burner. This will make the usability of the plant even more versatile.
• the heat exchanger is selected from a group consisting of a two-stage heat exchanger, a multi-stage heat exchanger, and a rotary-bed heat exchanger. These are technologically and economically advantageous solutions.
• the heat exchanger is regenerative.
• the catalytic combustion unit comprises a two-stage or multi-stage heat exchanger and gas distribution means for guiding the flow of gas during a change in the direction of gas supply.
• the level of nitrogen oxides (NO x ) is lower than 5 ppm and the level of ethene (C 2 H 4 ) is lower than 1 ppm, calculated for an oxygen content of 3 vol%.
• the level of nitrogen oxides (NO x ) is lower than 2 ppm, calculated for an oxygen content of 3 vol%.
• the formed carbon dioxide containing gas CO2G typically contains about 14 to 17 wt% of carbon dioxide, such as 15 wt%, when for example fuel oil or gases are applied.
• the level of nitrogen oxides is advantageously lower than 5 ppm, calculated for an oxygen content of 3 vol%.
• the level of nitrogen oxides in the afterpurified carbon dioxide containing gas is lower than 2 ppm, calculated for an oxygen content of 3 vol%.
• Such a gas can be used particularly well in, for example, a greenhouse.
• a gaseous or liquid fuel can be burnt catalytically in a controlled manner by means of a catalyzer at a low temperature, 350 to 850O, so that very little nitrogen oxides ( NO x ) and sulphur oxides (SO x ) are produced by combustion, and as a result of almost complete combustion, negligible levels of hydrocarbons and carbon monoxide are left in the gas.
• the level of ethene, which is the most harmful of hydrocarbons to plants, is lower than 1 ppm, calculated for an oxygen content of 3 vol%. In diluted fertilizer gas, the content is less than 0.01 ppm, as well as the content of carbon monoxide.
• the thermal energy produced in combustion can be advantageously used for heating, and the cooled pure combustion gas can be led to utilization.
• the untreated exhaust gases of the heating boiler according to the invention are so pure that they meet even the most stringent international standards for emissions.
• the content of other emissions will depend on the sulphur content of the fuel.
• low emission fuels such as propanol, natural gas, bioalcohol, light fuel oil, pyrolysis gases, or the like. The plant will then clearly meet all the standards for emissions. (NOx and CO ⁇ 100 mg/Nm 3 )
• catalytic combustion takes place at a low fuel content below 20% from the LEL limit, which means a content of about 10 g/Nm 3 .
• LEL limit which means a content of about 10 g/Nm 3 .
• the flow of gas discharged from the boiler is kept low by recirculation.
• the temperature of the gas is about 50 to 90"C, depending on the heat exchange rs. Even from that, energy can still be recovered by means of a separate heat exchanger.
• the temperature is 350 to 850O.
• the catalyzer lowers the combustion temperat ure by about 100 to 400O compared to thermal combustion which typically requires a temperature of 750 to 950O.
• This temperature difference is very signific ant, because at the lower temperature, the nitrogen present in the air does not start to react with the oxygen in the air, and harmful nitrogen oxides are thereby not developed.
• the catalytic combustion is very fast, having typically a duration of only 0.01 to 0.1 s, such as about 0.02 to 0.05 s, in the catalyzer itself and after that, for example, about 0.1 s in the channel before the heat exchanger. This duration is about one tenth compared with the duration in a thermal boiler.
• the applications according to the invention apply a relatively low temperature and a very short retention time, hardly any nitrogen oxides (NOx) can be formed, their level remaining preferably below 5 mg/Nm 3 . Furthermore, in catalytic combustion, the oxidation is controlled so closely that hydrocarbons and eventual carbon monoxide burn out, their levels being normally lower than 5 mg/Nm 3 .
• NOx nitrogen oxides
• the investment costs of a catalytic boiler are lower than those of thermal boilers with their purification systems.
• the operating costs of thermal combustion are increased by the costs of acquisition, use and maintenance of a reducer.
• nitrogen oxides are usually formed at such a high level that they must be removed in large boilers.
• the removal takes place in a selective catalytic reducer (SCR) in which the reducing agent used is ammonia or urea dissolving into ammonia and carbon monoxide gas.
• SCR selective catalytic reducer
• the reduction takes place in a special catalyzer so that one molecule of ammonia reduces one NOx molecule.
• Urea or ammonia is normally needed in about 3 to 4% of the fuel content, and it is even more expensive than the fuel. In other words, it raises the combustion costs respectively.
• the SCR catalyzer will require a temperature of about 230 to 300O to operate well, yet another heat exchanger m ust be provided after the catalyzer. Because the SCR catalyzer requires a long retention time of about 0.3 s (space velocity of 10 to 12,000 1/h), its size is very large. It is often larger in size than the boiler. Furthermore, the SCR will require a tank of ammonia or urea and an automatic dosing system. Both ammonia and urea are difficult substances in their own way. Ammonia is very toxic to transport and store. The urea solutions used are almost saturated aqueous solutions with a solid content of 32 to 40%. They are easily crystallized and difficult to dose. Moreover, both urea and ammonia reduction will require an oxidation catalyst to eliminate possible leaks of ammonia.
• the injector comprises means for at least partial combustion of the fuel supplied.
• the incoming gas is heated, if necessary, to the combustion temperature, and after that, part of the energy produced in catalytic combustion can be transferred to heat the incoming gas.
• the apparatus is formed of two parts: the catalytic combustion plant and the heat exchanger.
• the catalytic combustion plant may be either a regenerative or a recuperative apparatus.
• the incoming liquid fuel is first vaporized, and the gas is then heated in the heat exchanger, after which it is oxidized in the catalyzer.
• Part of the produced energy is transferred to heat the incoming gas, and part is led via a post-catalyzer to the heat exchanger for useful energy. After this, the gas flow that had heated the incoming gas and the gas flow passed via the recovery of useful energy are combined.
• the main part, preferably 70 to 90%, of this gas flow is recirculated to the inlet side of the catalyzer, and the rest of the gas is discharged via a flue gas duct to atmospheric air. 10 to 30% of clean air which contains the oxygen needed for catalytic combustion is admixed to the gas flow entering the catalytic combustion. In many cases, the most advantageous efficiency is achieved when air is only admixed in the required amount, about 10%.
• the heat exchanger may be made of a fire-resistant material. This improves the strength of the plant and increases reliability and reduces the need for maintenance.
• the apparatus comprises an after heat exchanger for recovering heat from gas formed in the combustion and/or for aftercooling the carbon dioxide containing gas discharged from the combustion unit. After the catalytic combustion, an essential part of the heat can thus be recovered via the heat exchanger for the purposes of heating a greenhouse, and the clean CO 2 containing flue gas can be led, for example, into greenhouses for the purposes of fertilizing and partly heating.
• the after heat exchanger comprises means for producing hot water and/or district heat. This will improve the total economy of the production apparatus further.
• the production apparatus is used particularly for producing both thermal energy and carbon dioxide (CO 2 ) containing gas that is very pure in terms of nitrogen oxides, ethene (C 2 H 4 ) and hydrogen sulphide.
• the production apparatus is used particularly for producing thermal energy.
• the production apparatus (PA) is used particularly for producing carbon dioxide (CO 2 ) containing gas that is very pure in terms of nitrogen oxides, ethene (C 2 H 4 ) and hydrogen sulphide.
• the selected object of production will affect the temperature to be used in combustion.
• temperatures from 600 to 800O are preferably used, and for the production of carbon dioxide (CO 2 ) containing gas, the temperatures of catalytic combustion may range, for example, from 350 to 500O or from 500 to 700O, de pending on the quantity of the gas to be produced and on the object to be filled in.
• CO 2 carbon dioxide
• the fuel is selected from the group of butane, propane, natural gas, fuel oil, biogas, bioalcohols, organic solvents, pyrolysis gases, and light fuel oil.
• the utilization of such fuels is technologically advantageous and simple.
• the catalyzer it is possible to oxidize various gaseous and liquid fuels which may be fossil or various biofuels from renewable sources (alcohols, gases released by pyrolysis, biogas, etc.). It is also possible to oxidize catalytically emissions of volatile organic solvents (VOC) or carbon monoxide either as such or in combination with other actual fuels.
• VOC volatile organic solvents
• the apparatus comprises means for diluting carbon monoxide containing gas and leading it to a greenhouse.
• the production apparatus according to the invention has technical and economical advantages.
• the thermal energy produced by combustion can be used entirely for heating when the cooled pure combustion gas can be led into a greenhouse for fertilization with CO 2 .
• the thermal energy remaining in the cooled combustion gas also contributes to the heating of the greenhouse. It is advantageous, for example, when the greenhouse is used in the winter.
• the gas combustion unit may be a metal honeycomb system with a rotary structure, comprising a catalyzer and a heat exchanger unit one after the other.
• the gas comes in from one side first into the heat exchanger, in which the gas is heated, and it then enters the catalyzer, in which the gases are oxidized. Next, the gas passes through the other side which collects heat.
• the structure may also be a honeycomb system in two parts, wherein one cell is used for collecting heat and the other is used for heating incoming gas.
• the catalytic burner comprises two or more stages. This arrangement makes the apparatus controllable in a more versatile way and contributes to the efficiency of the combustion.
• the heat exchanger may be advantageously coated with a catalytically active coating. This will further improve the efficiency of the production apparatus.
• the heat exchanger may also be a honeycombed system with a steel structure and consisting of two parts, wherein one cell is used for collecting heat and the other is used for heating incoming gas. The direction of flow is reversed after the cell that heats the incoming gas has cooled to a given limit value. The other cell that has trapped heat from the exhaust gas will start to heat the incoming air.
• the ratio of energy entering the greenhouse via the fertilizing gas and the heat exchanger can be easily controlled.
• the production apparatus comprises one or more heat exchanger and/or catalyzer means which are advantageously made of thin corrugated metal sheets, with channels between them for conducting gas.
• This kind of a structure is used as a static mixer.
• the structure increases substantially, for example, the number of contacts of hydrocarbons with a catalytically active surface.
• Sherwood number (Sh) representing the efficiency of mass transport, increases from 2.5 to 12; in other words, the gas molecules to be burnt are almost five times more frequently in contact with the catalytically active surface. With the intensified contact, the fuel can be made to burn completely (SAE 2002-01 -0357).
• the heat exchanger can be made of a steel sheet having a thickness of 0.2 to 1.5 mm and being coated with Al and/or Zn or being acid-proof, by corrugated "strips" with a width of 100 to 200 mm, in the same way as the catalyzer.
• This kind of a mixing structure will substantially intensify the transfer of heat from the gas into the steel sheet, and vice versa.
• the Nusselt number, representing the heat transfer in a flow channel will increase from 2.5 to 12, compared with a straight channel. This will improve substantially the efficiency of the heat exchanger.
• the heat exchanger is advantageously a metal honeycomb system with a rotary structure, which is passed through by gas that is heated in the catalyzer to the required combustion temperature, which is typically 500 to 700O.
• the heat exchanger may be made of, for example, creased (corrugated) metal band or wire mesh.
• the catalyzer may be a rotary metal honeycomb with a shape similar to that of the heat exchanger.
• the gas comes in from one half, through both/all of the cells.
• the gas In the accumulator cell, the gas is heated to the combustion temperature, and in the catalyzer following the accumulator, the gases are oxidized. After that, the gases enter the other half of the heat exchanger, in which most of the heat is transferred to the accumulator cell.
• the rotation speed of the accumulators is preferably 0.3 to 5 rpm.
• the combustion apparatus according to the invention comprises no bulky tube systems or valves. It is very advantageous in its structure, wherein the acquisition and operating costs are very low compared with the prior art. Also, the operation and maintenance of the apparatus is very inexpensive. Furthermore, the process is simple and efficient to control.
• the production apparatus comprises at least two processing compartments placed within each other.
• the catalyzer and the heat accumulator do not rotate but the gas flow direction is reversed at intervals by valves or by temperature control. They are advantageously connected to each other by one or more connecting parts to introduce the gas to be processed into the processing compartments within each other, and the gas purification production apparatus also comprises one or more adjustable gas guiding parts for discharging gas and/or for supplying it into the processing compartments within each other.
• the connecting parts it is advantageously possible, for example, to reverse the gas flow direction in the processing compartment.
• the same connecting part can be used both for supplying and for discharging gas, depending on the flow direction. In this way, the apparatus can be made not only technically but also economically advantageous.
• the processing compartments within each other have a cylindrical shape.
• the processing compartments can be preferably provided in a common body which is also equipped with the gas flow channels that replace a tube system.
• a common body which is also equipped with the gas flow channels that replace a tube system.
• the production apparatus applies catalyzers made of noble metal and having a very large surface area, which are known for their resistance to so-called catalyzer toxins and high temperatures. With such catalyzers it is possible to achieve an efficiency of even more than 99.9% in the long term.
• the predicted lifetime of such a catalyzer may be as long as 20 years.
• the production apparatus comprises one or more particle filters.
• the filter secures the undisturbed operation of the plant and advantageously reduces the particle emissions of the plant.
• the production apparatus according to the invention can be made relatively compact, because the functions are integrated with respect to each other in its structure. The volume/capacity ratio of such a plant is good, and furthermore, the volume can be used efficiently. This will facilitate transportations and installations on the site of use.
• the container does not require a foundation or any supporting structures.
• the production apparatus can be coupled to be ready for use very fast, for example in a couple of days.
• the container can be advantageously moved to a new location, if necessary.
• a combustion plant with a capacity of even 3 MW can be advantageously installed in a standard marine container (6 m).
• the production apparatus is automated. It can automatically adjust its operation for various loads, and its operation can be controlled either by a computer or by a GMS phone, if desired.
• Figure 1 shows a schematic chart on a production apparatus with a rotary bed heat exchanger.
• Figure 2 shows a schematic chart on a production apparatus with a two-stage heat exchanger.
• Figure 3 shows a schematic chart on a production apparatus with a two-stage thermal boiler as an after heat exchanger.
• Figure 1 shows a production apparatus PA comprising one main blower 1 of combustion air AIR, equipped with an injector J for injecting fuel PG into the combustion air AIR, as well as a catalytic combustion unit 2.
• a catalytic burner NCB for catalytic burning of fuel at a temperature of 350 to 850O in a retention time of 0.01 to 0.1 s for generating carbon dioxide containing gas.
• a particle filter PF which improves the operation of the plant and reduces the particle emissions of the plant in an advantageous way.
• the injector J comprises means for at least partial burning of the fuel PG to be supplied.
• the production apparatus comprises a rotary-bed RHE regenerative heat exchanger for transferring heat from the carbon dioxide containing gas CO2G generated in the catalytic burner to the combustion air AIR to be supplied into the catalytic burner NCB, and to the fuel PG.
• the catalytic combustion unit 2 is equipped with a catalytic after burner ACB for after purification of the carbon dioxide containing gas CO2G.
• the production apparatus PA also comprises an after heat exchanger AHE for aftercooling the carbon dioxide containing gas CO2G discharged from the combustion unit 2.
• Figure 2 shows a production apparatus PA comprising one main blower 1 of combustion air AIR, equipped with an injector J for injecting fuel PG into the combustion air AIR, as well as a catalytic combustion unit 2.
• a catalytic burner NCB for catalytic burning of fuel at a temperature of 350 to 850"C in a retention time of 0.01 to 0.1 s for generating carbon dioxide containing gas.
• a particle filter PF is provided in front of the main blower to improve the operation of the plant and to reduce the particle emissions of the plant in an advantageous way.
• the injector J comprises means for at least partial burning of the fuel PG to be supplied.
• the production apparatus comprises a two-stage regenerative heat exchanger THE for transferring heat from the carbon dioxide containing gas CO2G generated in the catalytic burner to the combustion air AIR to be supplied into the catalytic burner NCB, and to the fuel PG.
• the catalytic combustion unit 2 is equipped with a catalytic after burner ACB for after purification of the carbon dioxide containing gas C02G.
• a by-pass channel with a by-pass valve BBV which is opened at the same time when the main valve MV in the main channel is closed.
• the flow direction is reversed by the control valves of the two-stage heat exchanger (not shown in the figures).
• the gas is passed via catalyzers directly into the bypass channel.
• the by-pass channel BBV is closed and the main valve MV is opened.
• the production apparatus PA also comprises an after heat exchanger AHE for aftercooling the carbon dioxide containing gas C02G discharged from the combustion unit 2.
• Figure 3 shows a production apparatus PA comprising one main blower 1 of combustion air AIR and an injector J for injecting combustion air AIR and fuel PG, as well as a catalytic combustion unit 2.
• a catalytic burner NCB for catalytic burning of fuel at a temperature of 350 to 850O, s uch as advantageously at a temperature of 600 to 800O, in a retention time of 0.01 to 0.1 s for generating carbon dioxide containing gas.
• a particle filter PF is provided to improve the operation of the plant and to reduce the particle emissions of the plant in an advantageous way.
• the production apparatus comprises a two- stage regenerative heat exchanger THE for transferring heat from the carbon dioxide containing gas CO2G generated in the catalytic burner to the combustion air AIR and the fuel PG to be supplied into the catalytic burner NCB.
• the catalytic combustion unit 2 is equipped via a main valve MV with a catalytic after burner ACB for after purification of the carbon dioxide containing gas CO2G. Part of the gas is guided after the catalytic combustion into the by-pass channel BBV via the heat exchanger THE, to maintain the process heat.
• the production apparatus PA is equipped with an after heat exchanger AHE for recovering heat from the gas C02G formed in the combustion.
• the production apparatus PA is also equipped with a gas recirculation apparatus CG for returning the gas C02G formed in the combustion at least partly to the main blower 1 ; preferably, the content of recirculated gas is 70 to 90% of the discharged gas.

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• Engineering & Computer Science (AREA)
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• Mechanical Engineering (AREA)
• General Engineering & Computer Science (AREA)
• Combustion & Propulsion (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Environmental & Geological Engineering (AREA)
• Physics & Mathematics (AREA)
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• 2009
  • 2009-04-07 FI FI20090137U patent/FI8492U1/fi not_active IP Right Cessation
• 2010
  • 2010-04-07 EP EP10761232A patent/EP2417390A1/de not_active Withdrawn
  • 2010-04-07 CN CN2010900009228U patent/CN202902267U/zh not_active Expired - Fee Related
  • 2010-04-07 US US13/263,358 patent/US20120040295A1/en not_active Abandoned
  • 2010-04-07 WO PCT/FI2010/050270 patent/WO2010116035A1/en active Application Filing

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