US20090241814A1 - Method and System for Heating of Water Based on Hot Gases - Google Patents

Method and System for Heating of Water Based on Hot Gases Download PDF

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US20090241814A1
US20090241814A1 US11/992,508 US99250806A US2009241814A1 US 20090241814 A1 US20090241814 A1 US 20090241814A1 US 99250806 A US99250806 A US 99250806A US 2009241814 A1 US2009241814 A1 US 2009241814A1
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water
gas
heat exchanger
heat
fluid
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Jens Dall Bentzen
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Dall Energy Holding ApS
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • 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 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/28—Control devices specially adapted for fluidised bed, combustion apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/50—Control or safety arrangements
    • 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
    • F23G7/10—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of field or garden waste or biomasses
    • 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
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious 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
    • 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
    • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
    • F23L7/002—Supplying water
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/20—Waste heat recuperation using the heat in association with another installation
    • F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/50—Cooling fluid supply
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/70—Condensing contaminants with coolers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/80—Quenching
    • 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
    • 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 present invention relates generally to a method and a system for heat recovery from hot gas, e.g. flue gas, produced in a thermal reactor, or—more precisely—for heating of water by means of the hot gases that are released by thermal conversion (gasification or combustion) of solid fuels e.g. biomass, waste or coal.
  • hot gas e.g. flue gas
  • thermal conversion gasification or combustion
  • Heating of water from hot gases that are released during thermal conversion of fuels is well known.
  • the hot water can be used for heating purposes, e.g. in houses, apartment houses, offices, in industries etc. and for domestic water. Installations for such purposes are produced in very different sizes, approx. 1 kW-250 MW input effect.
  • the water is usually heated in a closed circuit and led to a point of consumption, after which the water is returned to the heat production unit after release of the thermal energy.
  • the water temperature usually is 60-90° C.
  • the temperature of the water returning to the heat-production unit after cooling at the consumer (return) is about 30-50° C.
  • the hot water can be produced close to the required locations or be sent to the consumer via a district heating network.
  • the energy released by thermal conversion of a fuel can be transferred to hot water in stages, e.g.:
  • the gas leaving the thermal unit is usually around 700-1000° C., depending on technology, fuel and operation conditions. It is well known, e.g. at CHP stations, that the temperature in the thermal unit can be adjusted or controlled by water injection in order to protect materials, e.g. the superheater, against a too high temperature.
  • the amount of water injected in order to adjust the temperature in the boiler room is, however, very limited; the temperature of the gas remains high (above 600° C.), and the characteristics of the gas, e.g. the water dew point, are not changed substantially.
  • the energy from the hot gas is transferred to another medium, e.g. water, by using a heat exchanger where the hot gas is flowing at one side while another colder medium (e.g. water) is flowing at the other side.
  • another colder medium e.g. water
  • more heat exchangers are used, e.g. air preheating and/or steam superheating and/or hot water production.
  • heat exchangers are usually of the convection heat exchanger type, as the energy mainly is transferred from the gas via convection.
  • steel pipes are used.
  • the gas contains particles. These particles result in several problems in this heat exchanger: fouling, corrosion, low heat exchange rates etc. and often a device is mounted to keep the gas tubes clean, e.g. soot blowing or mechanical cleaning.
  • the heat exchanger used for transferring energy from the dry hot gas is made of materials matching the qualities of the gas, usually heat-proof steel.
  • the gas is cooled in the “convection part” to around 150° C., as the temperature of the gas then is above the acid dew point and the water dew point. If the gas is cooled to or below the acid or water dew points, severe corrosion may occur in the heat-proof material of the heat exchanger.
  • Ammonia, chlorine, sulphur, particles, salts etc. is often removed from the gas, for instance by a dry or semi-dry cleaning process. In this way, the materials causing problems for the environment or the materials blocking and/or corroding during the subsequent process stages can be removed.
  • the gas can be further cooled, by which vapours, including water vapour in the gas, are condensing.
  • the composition of the gas depends on the fuel conversed and of the conditions in the thermal reactor. With high moisture content in the fuel and a low amount of excess air in the thermal unit, a high water dew point is obtained. Usually, the water dew point in the gas will be approx. 35-60° C., if the gas has atmospheric pressure. If the gas is cooled below the water dew point, water vapour will condense, and condensation energy is released which can be used for further heat production. Depending on the fuel and the conditions in the thermal process, the energy utilization can be increased by up to about 30%.
  • the condensing part is usually made of other materials.
  • the condensing part e.g. glass fibre, plastic material, glass, acid-proof stainless steel, titanium etc. are used.
  • the temperature of the water heated in the condensing unit becomes too low to be used for supply. Therefore, the water from the condensing unit must be further heated.
  • the energy in the gas after the condensing unit can be further utilized, for instance by transferring water vapour and heat to the combustion air that is added to the thermal process, or by means of a heat pump.
  • chilling of hot gases by massive water injection into a “quench” is used.
  • a “quench” is thus wet, as there is a surplus of water.
  • no considerable evaporations will take place of the injected water, as the water amount is very large in order to secure cooling of the gases.
  • no significant change of the gas characteristics e.g. the dew point
  • the nozzles used in a quench are of the type generating large water drops and delivering a large amount of water.
  • the heat capacity approximately 0.16 J/g/° C.
  • chilling of hot gases by water injection into an “evaporative cooler” is used.
  • the cooled gas can be dry and thus dry gas cleaning systems can be used for cleaning the gases, which is necessary due to environmental legislation.
  • dry gas cleaning systems can be used for cleaning the gases, which is necessary due to environmental legislation.
  • cement production plants One example of such plants.
  • the water vapour in the gas from “evaporative coolers” is not condensated and used for production of hot water.
  • the combustion chamber is very compact and followed by an injector which is used as a gas pump.
  • the ejector can then be followed by a heat exchanger where water vapours condensate and energy hereby is be retrieved.
  • a heat exchanger where water vapours condensate and energy hereby is be retrieved.
  • Feeding systems and combustion chambers for solid fuels are very different from feeding systems and combustion chambers for gaseous fuels.
  • the invention provides a method and a plant allowing transfer of energy from hot gases to water or another fluid by means of considerably fewer heat transfer units, as the heat transfer from hot gases can be gathered in a single condensing unit. Moreover, a more simple water circuit is obtained as coupling and control of water circuit for a condensing unit as well as a convection part are avoided.
  • the invention provides a method for heat recovery from hot flue gas, produced in a thermal reactor.
  • water is injected at one or more injection zones in such an amount and in such a way that the flue gas temperature is reduced to below 400° C. and the gas dew point is at least 60° C. due to water evaporation.
  • the gas is led through a condensing heat exchanger unit ( 8 ), where at least some of the water vapour is condensed, and the condensation heat is used for heating a liquid stream, mainly water.
  • the amount of water vapour in the gas is increased, and thus the dew point of the gas is increased.
  • injection of water into a flue gas from combustion of biomass in such an amount that the gas is cooled to 150° C. will increase the dew point for the flue gas to approx. 85° C.
  • the dew point in flue gas is usually 35-60° C. without water injection.
  • the cooled gas containing a large amount of water vapour can then produce the amount of energy in the condensing heat exchanger unit which was previously produced in at least two units, i.e. a dry and hot convection part and a condensing part.
  • the dew point of the flue gas has increased considerably due to the water injection, which means that the condensing heat exchanger unit can heat water or another liquid to a temperature suitable for using the water directly as supply.
  • At least a part of the water injected into the hot gases will atomize in a nozzle, by which the water will evaporate more quickly.
  • Water injection into the hot gas may take place in several injection zones, which may comprise the fuel, the thermal reactor, a gas cleaning unit and/or the condensing heat exchanger unit.
  • the same plant can be used for dry fuels by water injection into the fuel and/or the thermal reactor. Thus, a fuel flexible plant is obtained.
  • NOx-formation can be controlled and reduced, as NOx formation is independent of temperature.
  • the thermal reactor and the gas pipes to the condensing heat exchanger unit may be separated or be built together in one unit, as the thermal conversion then takes place in one zone, whereas water injection may take place in that reactor zone and possible also somewhere else in a subsequent zone.
  • the gas Before and/or after the condensing unit, the gas can be cleaned of undesirable materials such as e.g. ammonia, heavy metals, acids, chlorine, sulphur, particles, salts, etc. This may for instance be done in a bag filter, a cyclone, and electrofilter or in a scrubber, possibly combined with addition of absorbents such as active carbon, lime, bicarbonate etc. As long as the gas temperature is above the water dew point, dry gas cleaning technologies can be used, e.g. bag filter or electrofilter. If the gas is wet, scrubbers and/or wet electrofilters can be used.
  • undesirable materials such as e.g. ammonia, heavy metals, acids, chlorine, sulphur, particles, salts, etc.
  • absorbents such as active carbon, lime, bicarbonate etc.
  • dry gas cleaning technologies can be used, e.g. bag filter or electrofilter. If the gas is wet, scrubbers and/or wet electrofilters can be used.
  • a part of the water injected into the gas can advantageously be injected at great speed in the direction of the gas flow.
  • kinetic energy from the water can be transferred to the gas, and the water injection may then act as a gas pump (ejector).
  • the water heated in the condensing heat exchanger unit can be further heated, e.g. via a water-cooled feeder, a water-cooled grate water-cooled areas in the reactor and/or other cooled surfaces around the thermal conversion area or via another thermal production.
  • a certain energy amount will be left in the gas in the form of heat and water vapour.
  • Some of that energy can be utilized by transfer to the combustion air via an enthalpy exchanger.
  • water vapour and heat are transferred to the combustion air, implying an even higher water vapour amount in the gas and thus a higher efficiency of the condensing unit.
  • Enthalpy exchangers can be designed in different ways, e.g. as rotating units, where combustion air flows on one side and hot gas on the other, or as a system where the gas after the condensing heat exchanger unit changes with cold water, whereby the water is heated. The heated water can then be used for heating and humidifying the combustion air.
  • the hot water can be produced close to the consumption place or be sent to the consumer via a district heating network.
  • Plants designed according to the invention can be built in a very wide spectrum of sizes, approx. 1 kW-250 MW input effect.
  • the thermal unit may have other purposes than only heat production, e.g. production of gas and electricity among others.
  • technologies relevant for the invention can be mentioned: Combustion plants for solid fuel (biomass, waste and coal) for mere heat production as well as CHP production, gas and oil fired boilers, motors, gas turbines, gasification plants etc.
  • thermal unit is of the fluid bed type
  • water injection into the bed can be used for adjusting the temperature in the bed, by which operational (e.g. slag formation) and environmental (e.g. reduction of NOx) advantages can be obtained.
  • Water injection into the bed will further contribute to fluidization of the bed. This kind of temperature adjustment is considerably more robust than the traditional technique in the form of cooling coils which are quickly worn down of the bed material.
  • the condensed water can be cleaned of particles, salts, heavy metals etc. and be adjusted for pH, before it is used or led away.
  • the water injected into the fuel in the thermal unit, in the gases or in the condenser may be condensate, segregated in the condensing unit, or water added from outside.
  • the condensing unit and in the connecting gas duct there may be atmospheric pressure, or pressures above or below the atmosphere.
  • the invention further provides a system for decomposition of fuel and production of hot water, and comprising a thermal reactor, a flue gas duct, one or more water injection devices e.g. in the form of nozzles and a condensing heat exchanger unit connected to the flue gas duct.
  • a thermal reactor e.g. a thermal reactor
  • a flue gas duct e.g. a flue gas duct
  • one or more water injection devices e.g. in the form of nozzles
  • a condensing heat exchanger unit connected to the flue gas duct.
  • the condensation heat is used for heating of a flow of fluid, preferably water, and means for control of the water injection into the flue gas in order that the flue gas temperature is reduced to below 400° C., and the gas dew point becomes at least 60° C. due to the evaporation of water.
  • FIG. 1 schematically depicts a first design of a plant according to the invention
  • FIG. 2 schematically depicts a second design of the plant according to the invention, where solid fuel is burned in a grate-fired boiler, and where particles are removed from the flue gas in a bag filter before condensing;
  • FIG. 3 schematically depicts a third design of the plant according to the invention, where solid fuel is burned in a grate-fired boiler, and where water is added by means of an ejector;
  • FIG. 4 schematically depicts a fifth design of the plant, where fuel is gasified and the heat energy in the gas is utilized;
  • FIG. 5 is a diagram of the flue gas output from cooling, with and without preceding water injection and evaporation.
  • FIG. 6 are two tables with energy calculations, where wet and dry fuel, respectively, are converted. The calculations show results for today's standard technology and for the invention with and without moistening of combustion air.
  • FIG. 1 of the drawings there is shown a unit or reactor 1 , to which fuel is added.
  • the fuel is converted thermally by addition of air (and/or oxygen).
  • a warm gas is produced in the thermal unit 1 .
  • the fuel added to unit 1 is solid e.g. biomass, waste or coal. If the thermal unit 1 is designed for fuels with low calorific power, e.g. wet fuel, and if the added fuel has a higher calorific power, the temperature in the unit or in the generator 1 can be adjusted by adding water to the fuel at 2 and/or by adding water at 3 within the thermal unit 1 .
  • water is injected into the hot gases leaving the thermal unit 1 .
  • the water evaporates and cools the gases considerably, as the evaporation energy from water is very high.
  • the unit in which injection 4 is placed can be built of heat-proof steel, bricks, castings and/or other materials.
  • the amount of water dosed at 4 can be controlled on basis of the gas temperature and/or the dew point by means of adequate control means S, placed in a position after 4 , where the injected water has evaporated.
  • a gas cleaning unit 5 can remove these impurities from the dry gas.
  • the gas Via a gas blower or pump 6 , the gas can be pumped on to a condensing heat exchanger unit 8 , where the heat in the gases, including the condensation heat in the water vapour, can be transferred to the water to be heated.
  • water can also be injected at 7 .
  • the gas sucker 6 can also be placed after the condensing unit 8 , where the gas flow is lower due to the cooling of the gas and the condensing of the water vapours.
  • more impurities can be removed from the gas at 9 and/or from the produced condensate at 12 .
  • some of the energy left in the gas in the form of heat and moist can be transferred, at 10 , to the combustion air which is added to the thermal unit 1 .
  • the humidified air can be further heated in a heat exchanger 11 , before the air is added to the thermal unit 1 , whereby the supply lines are kept dry.
  • This type of plant can be produced in many different sizes, from a few kW (villa boilers) to large plants above 100 MW.
  • FIG. 2 shows a combustion plant for production of district heating, and where the gas is cleaned before condensing and combustion air is moisturized.
  • 1 is a burner for combustion of solid fuel.
  • the plant is brick-lined so that it can burn fuels with a high water content (up to 60% water) or which otherwise have a low calorific value (below 10 MJ/kg). Fuels with a higher calorific value can also burn in such a plant, as water can be added to the fuel at 2 , or in the boiler room at 3 . Further, at 4 water is added to the hot gases leaving the burner 1 . The water evaporates and cools the gases to ca. 150-200° C. Subsequently, the gas is cleaned of particles in a bag filter 5 . If other substances are to be removed from the gas, absorbents can be added before the filter, e.g. lime, active carbon, bicarbonate etc.
  • absorbents can be added before the filter, e.g. lime, active carbon, bicarbonate etc.
  • the flue gas is sucked through the gas sucker or the pump 6 and is cooled in the condensing unit 8 , comprising two cooling towers placed above each other, designated respectively “Kol. 1 ” and “Kol. 2 ”, and a heat exchanger 13 , as the flue gas flows counter-flow with the cooled condensate 7 a .
  • the condensing unit 8 is built of glass fibre, it is important that the gas is cooled to below ca. 150° C., before the inlet. Addition of water in the nozzle in 7 b protects the condenser inlet 14 from becoming too warm. In the cooling tower “Kol. 1 ” cooling water is added at 7 a .
  • the condensate is gathered in a room 15 under the cooling towers and the inlet 14 .
  • the hot condensate is heat exchanged in the heat exchanger 13 by water in a district heating system which is not shown, as the cold district heating water is added via a return pipe, whereas the hot water is led back to the system via a supply pipe.
  • the flue gas dew point is high, e.g. ca. 85° C.
  • the temperature of the produced condensate can be about 85-90° C.
  • the district heating water can be heated from the condensate at one single stage.
  • the combustion air added to the burner 1 can be heated in a humidifier 17 , where hot water is added at 18 , or by means of a heater device 11 , ensuring that the air ducts are kept dry.
  • the water added at 2 - 4 , 7 a , 7 b and 18 may—as shown—be the cooled condensate that leaves the heat exchanger 13 , and any surplus condensate can be led away at 19 .
  • Condensate gathered at the bottom of the humidifier 17 can be used for addition to the cooling tower “Kol. 2 ”.
  • FIG. 3 shows a combustion plant for production of district heating.
  • the gas is led through the plant by means of an ejector pump.
  • 1 is a burner for combustion of solid fuel.
  • water is added to the hot gases leaving the burner 1 .
  • the water evaporates and cools the gases.
  • 7 a water is injected at great speed in the direction of the gas flow through a pipe 20 , the cross section of which is increased in the flow direction.
  • the water injection at 7 a through the pipe 20 acts as an ejector.
  • a condensing heat exchanger 8 heat energy is transferred from the flue gas to the district heating water.
  • the heat exchanger in 8 may be made of glass, plastic or acid-proof stainless steel, but needs not be heat-proof.
  • the exchanger can be cleaned of particles by means of water injected at 7 b , but this needs not be a continuous cleaning.
  • the produced condensate can be cleaned of particles etc. at 12 , before it is used as injection water at 4 a , 4 b and 7 or drained off to a drain at 19 .
  • FIG. 4 shows a preferred design of a gasifier plant 1 , where the produced gas firstly is cooled by being used for preheating of combustion air in a heat exchanger 21 , and then is cooled by water injection at 4 .
  • the drafted gasifier is of the type “staged fixed bed”, but can in principle be other gasifier types, e.g. a fluid bed gasifier.
  • the gas is cleaned of particles (and possibly tars) e.g. in a bag filter and/or an active carbon filter 5 , after which the gas in a heat exchanger 8 is cooled during condensing of water.
  • a gas blower or pump 6 the gas is blown to a conversion unit, here illustrated by an engine, but there could also be other conversion units, e.g. a gas turbine, liquefaction equipment for conversion of the gas to fluid fuel etc.
  • the flue gas energy from the conversion unit can be utilized e.g. for heat production.
  • the invention can be utilized twice.
  • FIG. 5 is a diagram showing the calculation of the output from cooling of flue gas from respectively a traditional boiler and by water injection according to the invention, cf. FIGS. 2 and 3 . Common data for the two calculations are:
  • FIG. 6 shows two tables with key figures for selected calculations for district heating plants. It appears from the key figures that the efficiency by use of wet fuels will be the same for a standard design with condensing operation and with “water injection”.
  • the most important advantage of the concept is that the construction becomes considerably simpler and cheaper than for traditional condensing plants with both a convection part and a condensing unit.
  • a convection boiler and belonging boiler circuit with shunt and heat exchanger can be saved, and the water circuit and the control of the heat productions become much simpler and thus cheaper.
  • the efficiency is increased by lower air consumption, as the flue gas loss becomes smaller.
  • the air consumption can be reduced compared to plants with “boiler operation”, which will give a better efficiency.
  • the efficiency is further increased by 5-15% by moistening of combustion air.
  • Thermal NOx can be reduced by water injection in and around the combustion chamber, especially in case of gas and coal combustion.
  • Particle emissions will be reduced when filters are used e.g. bag filters.

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  • Sustainable Energy (AREA)
  • Chimneys And Flues (AREA)
  • Sorption Type Refrigeration Machines (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
US11/992,508 2005-09-27 2006-09-27 Method and System for Heating of Water Based on Hot Gases Abandoned US20090241814A1 (en)

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JP2012523948A (ja) * 2009-04-17 2012-10-11 プロターゴ インコーポレーテッド 有機廃棄物のガス化方法およびその装置
JP2015087043A (ja) * 2013-10-29 2015-05-07 三浦工業株式会社 ボイラシステム
US9103560B2 (en) 2010-04-09 2015-08-11 Carrier Corporation Furnace vent with water-permeable inner pipe
EP2870989A4 (en) * 2012-06-15 2016-03-30 Rafik Nailovich Khamidullin PROCESS FOR PURIFYING GAS
WO2018157947A1 (en) * 2017-03-03 2018-09-07 Douglas Technical Limited Apparatus and method for continuously drying bulk goods, in particular wood chips and/or wood fibers comprising a heat exchanger
IT201800003238A1 (it) * 2018-03-02 2019-09-02 Ambiente E Nutrizione Srl Procedimento e sistema ottimizzati per la produzione di un fluido riscaldato tramite combustione di un combustibile
US11079106B2 (en) 2017-03-03 2021-08-03 Douglas Technical Limited Apparatus and method for continuously drying bulk goods, in particular wood chips and/or wood fibers comprising multi-fuel burner with a muffle cooling system
EP3722669A4 (en) * 2017-12-04 2021-10-27 Tsinghua University DEEP RECOVERY SYSTEM FOR RESIDUAL HEAT OF SMOKE GASES
US11384981B2 (en) 2017-06-06 2022-07-12 Kronoplus Limited Apparatus and method for continuously drying bulk goods
US11499778B2 (en) 2017-03-03 2022-11-15 Douglas Technical Limited Apparatus and method for continuously drying bulk goods, in particular wood chips and/or wood fibers comprising a solid fired hot gas generator
US11543124B2 (en) 2017-03-03 2023-01-03 Kronoplus Limited Apparatus and method for continuously drying bulk goods, in particular wood chips and/or wood fibers comprising a hot gas cyclone

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BRPI0918569A2 (pt) 2008-08-30 2015-12-01 Dall Energy Holding Aps método e sistema para converter um combustível carbonífero em gás de combustão e cinza em um reator térmico
JP2012502246A (ja) * 2008-09-07 2012-01-26 ダル エナジー ホールディング エーピーエス 水注入による高温ガスの冷却方法及び冷却システム
US8327779B2 (en) * 2008-09-26 2012-12-11 Air Products And Chemicals, Inc. Combustion system with steam or water injection
AT506701B1 (de) * 2008-12-16 2009-11-15 Froeling Heizkessel Und Behael Heizkessel für festbrennstoffe, insbesondere aus nachwachsenden rohstoffen
EA201270081A1 (ru) * 2009-06-26 2012-05-30 ДАЛЛ ЭНЕРДЖИ ХОЛДИНГ АпС Способ и система для очистки горячих газов и рекуперации тепла из них
CN101906321B (zh) * 2010-08-12 2012-11-28 中冶京诚（营口）装备技术有限公司 煤气站酚水处理工艺
US9291390B2 (en) 2011-05-11 2016-03-22 Shell Oil Company Process for producing purified synthesis gas
CN102226542B (zh) * 2011-06-03 2014-04-23 北京建筑工程学院 一种引射式热泵型换热机组
CN102995702A (zh) * 2011-09-17 2013-03-27 天华化工机械及自动化研究设计院有限公司 利用真空凝汽冷却法回收煤干燥蒸发水汽的方法及其设备
EP2636951A1 (en) * 2012-03-07 2013-09-11 Flare Industries, LLC Apparatus and method for flaring waste gas
DE102014203039A1 (de) * 2014-02-19 2015-08-20 Siemens Aktiengesellschaft Verfahren und Vorrichtung zur Trennung von Abgas bei der Verbrennung bestimmter Metalle
CN107238092A (zh) * 2017-06-12 2017-10-10 清华大学 燃煤锅炉排烟超低温冷凝热回收及进风加湿的方法与装置
FI128210B (en) 2018-10-04 2019-12-31 Valmet Technologies Oy Method for recovering heat from the boiler flue gas, and arrangement
AT525481B1 (de) 2021-10-04 2024-03-15 Scheuch Man Holding Gmbh Verfahren und Anlage zur Herstellung von Zementklinker

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Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2012523948A (ja) * 2009-04-17 2012-10-11 プロターゴ インコーポレーテッド 有機廃棄物のガス化方法およびその装置
US9103560B2 (en) 2010-04-09 2015-08-11 Carrier Corporation Furnace vent with water-permeable inner pipe
EP2870989A4 (en) * 2012-06-15 2016-03-30 Rafik Nailovich Khamidullin PROCESS FOR PURIFYING GAS
JP2015087043A (ja) * 2013-10-29 2015-05-07 三浦工業株式会社 ボイラシステム
US11248845B2 (en) 2017-03-03 2022-02-15 Douglas Technical Limited Apparatus and method for continuously drying bulk goods, in particular wood chips and/or wood fibers comprising a heat exchanger
WO2018157947A1 (en) * 2017-03-03 2018-09-07 Douglas Technical Limited Apparatus and method for continuously drying bulk goods, in particular wood chips and/or wood fibers comprising a heat exchanger
US11543124B2 (en) 2017-03-03 2023-01-03 Kronoplus Limited Apparatus and method for continuously drying bulk goods, in particular wood chips and/or wood fibers comprising a hot gas cyclone
US11499778B2 (en) 2017-03-03 2022-11-15 Douglas Technical Limited Apparatus and method for continuously drying bulk goods, in particular wood chips and/or wood fibers comprising a solid fired hot gas generator
US11079106B2 (en) 2017-03-03 2021-08-03 Douglas Technical Limited Apparatus and method for continuously drying bulk goods, in particular wood chips and/or wood fibers comprising multi-fuel burner with a muffle cooling system
EA038915B1 (ru) * 2017-03-03 2021-11-09 Дуглас Текникал Лимитед Устройство и способ непрерывной сушки сыпучих продуктов, в частности древесной щепы и/или древесного волокна, включающие теплообменник
US11384981B2 (en) 2017-06-06 2022-07-12 Kronoplus Limited Apparatus and method for continuously drying bulk goods
EP3722669A4 (en) * 2017-12-04 2021-10-27 Tsinghua University DEEP RECOVERY SYSTEM FOR RESIDUAL HEAT OF SMOKE GASES
US20210041102A1 (en) * 2018-03-02 2021-02-11 Vomm Impianti E Processi S.P.A. Optimized process and system for the production of a heated fluid by means of combustion of a fuel
WO2019166320A1 (en) * 2018-03-02 2019-09-06 Ambiente E Nutrizione S.R.L. Optimized process and system for the production of a heated fluid by means of combustion of a fuel
IT201800003238A1 (it) * 2018-03-02 2019-09-02 Ambiente E Nutrizione Srl Procedimento e sistema ottimizzati per la produzione di un fluido riscaldato tramite combustione di un combustibile

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DK1946006T3 (da) 2009-12-21
PL1946006T3 (pl) 2010-03-31
ES2334262T3 (es) 2010-03-08
CN101273235B (zh) 2011-07-06
EP1946006B1 (en) 2009-08-19
BRPI0616576A2 (pt) 2011-06-21
UA89279C2 (ru) 2010-01-11
EA200800912A1 (ru) 2008-12-30
CA2623978A1 (en) 2007-04-05
EA011970B1 (ru) 2009-06-30
EP1946006A1 (en) 2008-07-23
ATE440251T1 (de) 2009-09-15
DE602006008650D1 (de) 2009-10-01
WO2007036236A1 (en) 2007-04-05
CN101273235A (zh) 2008-09-24

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