EP2657597B1 - Vorrichtung zur Abgasrückgewinnung - Google Patents

Vorrichtung zur Abgasrückgewinnung Download PDF

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Publication number
EP2657597B1
EP2657597B1 EP13466004.2A EP13466004A EP2657597B1 EP 2657597 B1 EP2657597 B1 EP 2657597B1 EP 13466004 A EP13466004 A EP 13466004A EP 2657597 B1 EP2657597 B1 EP 2657597B1
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EP
European Patent Office
Prior art keywords
heat exchanger
direct
water
flue gases
flue
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EP13466004.2A
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English (en)
French (fr)
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EP2657597A1 (de
Inventor
Milan Ptacek
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Kovosta-Fluid Akciova Spolecnost
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Kovosta-Fluid Akciova Spolecnost
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Priority to PL13466004T priority Critical patent/PL2657597T3/pl
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
    • F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
    • F22D1/003—Feed-water heater systems
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
    • F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
    • F22D1/16—Feed-water heaters, i.e. economisers or like preheaters with water tubes arranged otherwise than in the boiler furnace, fire tubes, or flue ways
    • F22D1/18—Feed-water heaters, i.e. economisers or like preheaters with water tubes arranged otherwise than in the boiler furnace, fire tubes, or flue ways and heated indirectly

Definitions

  • the present invention relates to a system comprising a device for the utilisation of a residual heat of flue gases having a temperature, which exceeds their dew point and containing aggressive constituents, in particular of flue gases discharged from solid fuel firing boilers.
  • the present invention also relates to a system for increasing a thermal efficiency of a boiler as well as that of a steam cycle during a generation of an electrical energy of a steam.
  • the contemporary method of steam generation consists in that stem having high parameter values is extracted by a steam turbine and condenses inside the same under low pressure of about 0,008 MPa and under a temperature, which usually ranges between 30 and 45°C, thus turning to water having approximately the same temperature.
  • the condensed water has to be reheated to reach the temperature of the so called feedwater, usually at least about 105°C.
  • reheating of water from about 30 - 45°C up to 105°C is accomplished by means of the intermediate steam extraction.
  • the so called regeneration of feedwater occurs.
  • the steam used for reheating the feedwater is lost and cannot contribute to the output power of the turbine any more.
  • the temperature of the flue gases discharged from such boilers typically range between 120 and 170°C.
  • the residual heat contained of such flue gases is not utilized for any purpose. The utilization of that residual heat would require the installation of a heat exchanger using a low-potential cooling medium, i.e. a so called flue gas condenser.
  • the main reason why such flue gas condensers are not used consists in that the fuel, particularly coal, contains sulphur and may also contain HCl as well as water.
  • One of the combustion products is sulphur dioxide which would react with water.
  • US 4,489,679 discloses a control system for economic operation of a steam generator, where there is a closed system using a heat of flue gases to warm up a feedwater of the boiler. There is a temperature sensor in a flue gas stream and a system of valves that either enables the flue gases to escape or to enter a venturi to warm up a feedwater of the boiler. This patent does not solve a steam condensate that could have been used as cooling
  • US 4,660,511 discloses a method and apparatus for recovery of heat from the flue gas of a combustion furnace of a steam boiler or power generation plant which combined with a heat pump system.
  • the flue gas is passed through an economizer to preheat the boiler feed water.
  • the flue gas then passes to a direct contact gas cooler where a second stream of cooling water extracts heat from the flue gas.
  • US 4,340,572 discloses a process for recovering heat from stack or flue gas.
  • the gas stream is countercurrently contacted with a liquid medium in two stages in order to obtain a warmed liquid medium and a cooled gas stream.
  • the warmed liquid medium is passed in indirect heat exchange with eg. a process fluid.
  • This patent discloses how to use a heat from stack or flue gas, but a use of the heat of steam condensate used as a cooling water is not mentioned there.
  • WO 2010/149173 A2 discloses a method and system for cleaning of and heat recovery from hot gases. An exhaust gas is cooled in a gas cooler which produces a condensate that is further cooled in a condensate cooler which produces energy. This patent does not disclose exploitation of a condensate originating from a steam cycle during a generation of an electrical energy of a steam.
  • the system according to the invention comprises a direct-contact heat exchanger for extracting heat from the flue gases and transferring it to the process water
  • the flue-gas inlet of the direct-contact heat exchanger is connected to the flue-gas outlet of a solid fuel fired boiler and/or to that of an incineration plant producing flue gases that contain aggressive constituents, said flue gases being led through the direct-contact heat exchanger.
  • the water inlet is arranged for contact heat transfer between the flue gases and the process water.
  • the process-water outlet of the direct-contact heat exchanger is connected to the process-water inlet of the second heat exchanger for extracting heat from the process water and transferring it to the cooling water while the process-water outlet of the second heat exchanger is connected to the process-water inlet of the direct-contact heat exchanger.
  • the process-water circuit comprises the inlet for connecting an apparatus for replenishing alkali into the process water in order to maintain the pH value of the process water at a level enabling the corrosive effect of the acids, which are produced during the condensation of flue gases, to be neutralized.
  • the second heat exchanger is provided with a dedicated cooling water inlet connected to a steam condenser located downstream of the condensing section of a steam turbine and/or downstream of a steam turbine itself and/or downstream of a steam healing system, the cooling water being a steam condensate having a temperature ranging between 0 and 80°C, or between 0 and 70°C, or between 0 and 60°C, or between 0 and 50°C, or between 0 and 40 °C.
  • a cooling water outlet from the second heat exchanger is connected to a feedwater inlet of the steam boiler.
  • the direct-contact heat exchanger is equipped with a built-in structure for increasing the heat transfer efficiency, in particular for increasing the efficiency of the heat transfer between flue gases and process water, and/or for rinsing the interior surfaces of the exchanger and/or for increasing the efficiency of the neutralization the corrosive effect of the acids produced during the condensation of flue gases.
  • the flue-gas inlet which is connected to the flue-gas outlet of a solid fuel fired boiler and/or to that of another source of aggressive flue gases, is preferably arranged in the bottom portion of the direct-contact heat exchanger, while the process-water inlet for rinsing the interior surfaces of the direct-contact heat exchanger and for receiving the heat extracted from flue gases is arranged in the top portion of the direct-contact heat exchanger.
  • the heated-up condensate is used as feedwater for a steam boiler and/or for another heat source and/or for another heating circuit.
  • the device according to the invention further comprises a sedimentation vessel for settling of the solid particles flushed out from the direct-contact heat exchanger, said vessel being arranged between the direct-contact heat exchanger and the second heat exchanger and preferably provided with a ploughing apparatus for removing sediments from the sedimentation vessel.
  • the device according to the invention further comprises a process water pump which is arranged between the sedimentation vessel for settling of the solid particles flushed out from the direct-contact heat exchanger and the second heat exchanger for extracting heat from the process water and transferring it to the cooling water.
  • the apparatus for replenishing alkali into the process water in order to maintain the pH value of the process water at a level enabling the corrosive effect of the acids, which are produced during the condensation of flue gases, to be neutralized is preferably adjusted to maintain the pH value of the process water at a level greater than 5.0, particularly greater than 6.5, more preferably greater than 6.9 and most preferably greater than 7.5.
  • the apparatus for replenishing alkali into the process water is preferably incorporated into the process-water circuit between the process-water inlet of the direct-contact heat exchanger and a process-water pump.
  • the device further comprises a third heat exchanger which is arranged between the flue-gas outlet of the heat source and the flue-gas inlet of the direct-contact heat exchanger.
  • the second heat exchanger is provided with the cooling water outlet, which is connected to the cooling water inlet of the third heat exchanger for extracting heat from the flue gases and transferring it to the cooling water, while the cooling water outlet of the third heat exchanger is connected to the feed tank of a heat source and/or to the heating circuit of a boiler and/or to another heating circuit.
  • the device according to the invention further comprises a branch which is arranged upstream of the flue-gas inlet of the direct-contact heat exchanger, said branch being provided with a regulating member and routed to the flue-gas outlet of the direct-contact heat exchanger.
  • the device according to the invention further comprises an apparatus for replenishing the supply of process water and/or for draining the latter, said apparatus being arranged between the process-water outlet of the second heat-exchanger and the process-water inlet of the direct-contact heat exchanger.
  • the cooling water outlet of the third heat exchanger and/or the cooling water outlet of the second heat exchanger are connected to a thermal circuit, in particular to a thermal circuit incorporating a boiler.
  • the cooling water outlet of the third heat exchanger and/or the cooling water outlet of the second heat exchanger are connected to the feedwater inlet of a steam boiler and/or another heat source and/or another heating circuit.
  • the above described device can be also used in case that the dew point is exceeded and acids are produced having a lower level of aggressiveness in comparison with the flue gases containing the sulphurous, sulphuric or hydrochloric acids.
  • Fig. 1 shows the first exemplary embodiment of the device according to the invention
  • Fig. 2 shows the second exemplary embodiment of the device according to the invention.
  • flue gases have a temperature, which exceeds their dew point, and contain aggressive constituents.
  • flue gases are particularly those discharged from solid fuel fired boilers, in particular by coal boilers and also biomass boilers.
  • the flue gases discharged from a heat source e.g. from a solid fuel fired boiler, are blown along the process water causing the thermal energy of the flue gases to be transferred to the process water in order to heat the latter at most up to the boiling temperature of the same under given ambient atmospheric and pressure conditions.
  • the pH value of the process water is adjusted to enable the neutralization of the corrosive action of the condensing flue gas constituents and is maintained at a level higher than 5, preferably at a level higher than 7.5.
  • the process water is heated up by the flue gases, its heat is transferred to the cooling water. Then, the cooled process water re-enters the flue gas flow in order to extract thermal energy from it.
  • the thermal energy of the flue gases which would otherwise escape into the outside environment, is transferred to the process water which flows in a opposite direction with respect to that of the flue gases, neutralizes the flue gases and is further heated up by the same.
  • the neutralized process water becomes a heat transport medium that prevents the corrosion of the heat-exchanging surfaces, particularly those of the second heat exchanger, from developing.
  • the process water flows along the outer surface of the built-in structure of the heat exchanger which means that a direct heat transfer from flue gas to process water takes place and heat does not permeate through the material of the built-in structure of the heat exchanger. Therefore, the direct-contact heat exchanger can be made of materials which are not typical for heat exchangers, i.e.
  • plastic materials having poor thermal conductivity in particular plastic materials, such as polypropylene, polyethylene, PVDF etc., the above listing being not exhaustive. Such materials are cheap and exist in an unlimited number of types. Besides that, such plastic materials may be used for the fabrication of a louver-type or tubular built-in structure that enlarges the overall contact surface areas of the heat exchanger, thus increasing the efficiency of the flue-gases to process water thermal energy conversion. Since the process water flows through the built-in structure of the heat exchanger over a prolonged time, it has increased time for absorbing the heat and neutralizes the flue gases more efficiently.
  • plastic materials such as polypropylene, polyethylene, PVDF etc.
  • treated processed water with a higher pH value it would be possible to use ordinary metallic materials for the built-in structure of the heat exchanger, particularly for a louver-type one.
  • the process water would flow along such metal surfaces and continuously neutralize the acids produced during the condensation of flue gases, thus protecting those surfaces from corrosion.
  • the flue gases cause the built-in metal structure of the heat exchanger to be heated up from below, thus allowing the thermal energy to be directly transferred to the process water flowing along the built-in metal structure of the heat exchanger. In this way, the process water can absorb additional heat to that gained through the blowing action of the flue gases.
  • Fig. 1 shows a schematical view of an exemplifying embodiment of a device for the utilisation of the residual heat of flue gases according to the invention.
  • the device comprises a direct-contact heat exchanger 1 for extracting heat from the flue gases and transferring it to the process water and a second heat exchanger 6 for extracting heat from the process water and transferring it into the cooling water.
  • the direct-contact heat exchanger 1 comprises a flue-gas inlet 8 , a process water inlet 7 and a process water outlet 14 .
  • the process water inlet 7 of the direct-contact heat exchanger 1 is connected to the process water outlet 9 of the second heat exchanger 6 while the process water outlet 14 of the direct-contact heat exchanger 1 is connected to the first process water inlet 10 of the second heat exchanger 6 ,
  • the device further comprises the apparatus 5 for replenishing alkali into the process water in order to maintain the pH value of the process water at a level enabling to neutralize the corrosive effect of the acids, which are produced during the condensation of flue gases.
  • the apparatus 5 is connected to the process-water circuit through the sedimentation vessel 3 .
  • the direct-contact heat exchanger 1 is equipped with the built-in structure 2 for increasing the heat transfer efficiency.
  • the built-in structure 2 may be e.g.
  • the built-in structure 2 is also useful for increasing the efficiency of the heat transfer between flue gases and process water or, as the case may be, for increasing the efficiency of the neutralization the corrosive effect of the acids produced during the condensation of flue gases. Nevertheless, the built-in structure does not necessarily be a honeycomb one. Instead, a tubular built-in structure or a another structure acting similarly to a honeycomb one may be used.
  • the cooling water is typically the condensate produced in a steam condenser located downstream of the condensing section of a steam turbine and/or downstream of a steam turbine itself and/or downstream of a steam heating system, and having a temperature ranging between 0 and 80°C. or preferably between 0 and 50°C, or more preferably between 0 and 40°C.
  • the heated-up condensate may be then used as feedwater for a steam boiler and/or for another heat source and/or for another heating circuit.
  • the device further comprises the sedimentation vessel 3 for settling of the solid particles flushed out from the direct-contact heat exchanger 1 , said vessel being arranged between the direct-contact heat exchanger 1 and the second heat exchanger 6 and connected to the same.
  • the device further comprises the apparatus 5 for replenishing alkali into the process water in order to maintain the pH value of the process water at a level enabling the corrosive effect of the acids, which are produced during the condensation of flue gases, to be neutralized.
  • the apparatus 5 is connected to the process-water circuit through the sedimentation vessel 3.
  • the sedimentation vessel 3 is further provided with the pH meter 27 and with the ploughing apparatus 16 for removing sediments from the sedimentation vessel 3.
  • the apparatus 5 for replenishing alkali into the process water is connected to the sedimentation vessel 3.
  • the device further comprises the first process water pump 4 which is arranged between the first process-water outlet 17 of the sedimentation vessel 3 and the first process water inlet 10 of the second heat exchanger 6 .
  • the apparatus 5 for replenishing alkali into the process water may be incorporated into the process water circuit between the process water outlet 14 of the direct-contact heat exchanger 1 and the first process water pump 4 , the outlet of the latter being in turn connected to the first process water inlet 10 of the second heat exchanger 6 ,
  • the apparatus 5 for replenishing alkali into the process water maintains the pH value of the process water at a level enabling the corrosive effect of the acids produced during the condensation of flue gases to be neutralized.
  • a sufficient level may correspond to a pH value greater than 5.0, under different circumstances a pH value greater than 6.5 or 6.6 may be required.
  • a pH value greater than 7.5 is considered most favourable for the operation of the device.
  • the device according to the invention further comprises the third heat exchanger 18 which is arranged between the flue-gas outlet of the heat source and the flue-gas inlet 8 of the direct-contact heat exchanger 1.
  • the second heat exchanger 6 is provided with the cooling water inlet 19 and the cooling water outlet 20, which is connected to the cooling water inlet 21 of the third heat exchanger 18 for extracting heat from the flue gases and transferring it to the cooling water.
  • the cooling water outlet 22 of the third heat exchanger 18 is connected to the feed tank of a heat source and/or to the heating circuit of a boiler and/or to another heating circuit.
  • the third heat exchanger 18 does not suffer from corrosion because the temperature of its heated-up inlet water exceeds the dew point of the flue gases. Thus, the flue gases do not condense on the surface of the third heat exchanger 18 along which they are blown and no acids are produced.
  • the device according to the invention further comprises the branch 24 which is arranged upstream of the flue-gas inlet 8 of the direct-contact heat exchanger 1, said branch being provided with the regulating member 23 and routed to the flue-gas outlet 25 of the direct-contact heat exchanger 1 which may optionally comprise the regulating flap 26 .
  • the device according to the invention further comprises the apparatus 29 for replenishing the supply of process water and/or for draining the latter, said apparatus being arranged between the process-water outlet 9 of the second heat-exchanger 6 and the process-water inlet 7 of the direct-contact heat exchanger 1 .
  • the flue gases When the latter apparatus is in operation, the flue gases have the initial temperature T1 upon entering the third heat exchanger 18 and the temperature T2 upon leaving the third heat exchanger 18 .
  • the temperature T2 is then the initial one of the flue gases upon entering the direct-contact heat exchanger 1 .
  • the flue gases having the temperature T3 Upon leaving the direct-contact heat exchanger 1 the flue gases having the temperature T3 are discharged into the ambient atmosphere. This means that if the flue gases pass through the heat exchangers 18 and 1 , their temperature will decrease from T1 over T2 up to T3. Since the temperature T2 still exceeds the dew point of the flue gases, the third heat exchanger 18 can be made of a material without any special requirements regarding corrosion resistance.
  • the temperature of the flue gases is dropping below the dew point of the flue gases but the acids produced in the built-in structure 2 of the direct-contact heat exchanger 1 are immediately neutralized by the process water that has a suitably adjusted pH value and continuously flows along the surfaces of the built-in structure 2.
  • the flue gases being discharged into the ambient atmosphere are cooled below their dew point and cannot cause the corrosion of the heat-exchanging surfaces to develop.
  • the process water is fed to the process-water inlet 7 in the upper portion of the direct-contact heat exchanger 1, flows down along the surfaces of the built-in structure 2 of the direct-contact heat exchanger 1, where it encounters the flue gases being blown in the opposite direction and is heated up by the same, then it flows down through the process-water outlet 14 of the direct-contact heat exchanger 1 into the sedimentation vessel 3 where solid particles which have been flushed out from the direct-contact heat exchanger 1 settle. Subsequently, these sediments are removed by the ploughing apparatus 16 from the sedimentation vessel 3 and thus eliminated from further circulation.
  • the process water is pumped by the first process water pump 4 from the first process-water outlet 17 of the sedimentation vessel 3 into the first process-water-inlet 10 of the second heat exchanger 6 .
  • the thermal energy of the process water is transferred to the cooling water, the latter entering the second heat exchanger 6 through its first cooling water inlet 19 and having the initial temperature t1 typically ranging between about 35 and 40 °C.
  • the cooling water Upon leaving the outlet 20 , the cooling water has the temperature t2 typically ranging between 90 and 95°C.
  • the cooling water is led into the cooling water inlet 21 of the third heat exchanger 18 for extracting heat from the flue gases and transferring it to the cooling water.
  • the cooling water having the temperature t3, typically between 105 - 135°C leaves the cooling water outlet 22 of the third heat exchanger 18 and flows to the feed tank of a heat source and/or to the heating circuit of a boiler and/or to another heating circuit.
  • the branch 24 which is arranged upstream of the flue-gas inlet 8 of the direct-contact heat exchanger 1 , is provided with the regulating member 23 and routed to the flue-gas outlet 25 of the direct-contact heat exchanger 1, thus allowing a certain amount of flue gas to be directly discharged into the ambient atmosphere after passing through the third heat exchanger 18.
  • the flue-gas outlet 25 of the direct-contact heat exchanger 1 is routed into the ambient atmosphere through the regulating flap 26.
  • the temperature of the cooling water can be decreased through partly opening the regulating member 23 and throttling the regulating flap 26.
  • a certain amount of the flue gases can be discharged from the third heat exchanger 18 directly into the ambient atmosphere without having to pass through the direct-contact heat exchanger 1 and without losing any part of the thermal energy which would be otherwise transferred to the process water.
  • Fig. 2 shows another exemplifying embodiment of the device according to the invention.
  • the flue-gas circuit is identical to that of the device shown in Fig, 1 .
  • the section of the process-water circuit, in which the process water flows from the sedimentation vessel 3 through the second heat exchanger 6 into the process-water inlet 7 of the direct-contact heat exchanger 1 is complemented by the parallel section leading from the second process-water outlet 11 of the sedimentation vessel 3 through the second process water pump 28 into the process-water inlet 12 of the fourth heat exchanger 13 and then from the fourth heat exchanger 13 into the second process-water inlet 15 of the second heat exchanger 6.
  • the process water After passing through the fourth heat exchanger 13 and the second heat exchanger 6 the process water is cooled and its temperature drops to tp3 (typically 61°C) and tp2 (typically 40°C). respectively.
  • tp3 typically 61°C
  • tp2 typically 40°C
  • the process water is reheated and its temperature is increased to tp1, typically ranging between 90 and 95°C.
  • tp1 typically ranging between 90 and 95°C.
  • there are also two cooling water circuit the first one being identical with that described with reference to Fig. 1 and the second one containing e.g. circulating water of a heating system.
  • the condensate may be the cooled one returning from the heating circuit of a drying plant, e.g. a malt drying kiln, wherein such returning condensed water may be aftercooled by a stream of drying air entering the malt drying kiln on order that the temperature of the same drops to about 40°C.
  • the condensate is heated in the second heat exchanger 6 up to 90°C and then, during the passage through the third heat exchanger 18 up to 105°C.
  • the condensate flows into a boiler feed tank from where it is be supplied into a boiler in which it turns to steam.
  • Such steam is fed into a steam-to-air heat exchanger of the drying plant where it turns to condensed water.
  • the latter is aftercooled by the air taken into the drying plant.
  • the temperature of the condensed water drops to about 40°C and the complete cycle will be repeated.
  • this water may be led a hot-water boiler where its temperature is further increased, e.g. to 150°C.
  • Such boiler may supply a municipal heating system with hot water.
  • the invention may be particularly useful in block-type thermal power stations where electrical energy is generated by means of steam condensing turbines, preferably by means of double-extraction condensing steam turbines, and where low-potential cooling media are used, such as condensates produced in condensing steam turbo-sets which are supplied by solid fuel filed boilers or gas fired boilers.
  • low-potential cooling media such as condensates produced in condensing steam turbo-sets which are supplied by solid fuel filed boilers or gas fired boilers.
  • the advantages of the invention are especially considerable in those turbo-sets where the heat-exchanging surfaces of the condensers are more or less subject to corrosion attacks.
  • the invention is useful whenever a low-potential medium can be found that requires to be heated up to the boiling temperature of the process liquid of a direct-contact heat exchanger under given ambient atmospheric and pressure conditions.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chimneys And Flues (AREA)

Claims (13)

  1. Ein System, umfassend eine Anlage zur Rückgewinnung der Wärme aus Abgasen, deren Temperatur deren Taupunkt überschreitet und die aggressive Bestandteile enthalten, insbesondere aus Abgasen, die aus Kesseln zur Verbrennung von festen Brennstoffen abgelassen werden, welche Anlage einen Dampfkessel zur Erzeugung von Dampf für eine Dampfturbine und/oder eine Kondensationsdampfturbine, einen Direktkontakt-Wärmetauscher (1) zur Wärmeübertragung von den Abgasen und auf Prozesswasser, wobei der Direktkontakt-Wärmetauscher (1) einen Abgaseinlass (8), der mit einem Abgasauslass des zur Verbrennung von festen Brennstoffen vorgesehenen Kessels und/oder mit einem Abgasauslass einer aggressive Bestandteile enthaltenden Abgase ablassenden Verbrennungsanlage verbunden ist, wobei die Abgase durch den Direktkontakt-Wärmetauscher (1) geführt werden, sowie einen Prozesswassereinlass umfasst, der am gegenüberliegenden Ende angeordnet und zur Kontaktwärmeübergabe zwischen den Abgasen und dem innerhalb des Direktkontakt-Wärmetauschers (1) befindlichen Prozesswasser vorgesehen ist, wobei die Anlage ferner einen zweiten Wärmetauscher (6) umfasst, wobei der Prozesswasserauslass (14) des Direktkontakt-Wärmetauschers (1) mit dem ersten Prozesswassereinlass (10) des zweiten Wärmetauschers (6) zur Wärmeübertragung von dem Prozesswasser auf Kühlwasser verbunden ist, wobei der Prozesswasserauslass (9) des zweiten Wärmetauschers (6) mit dem Prozesswassereinlass (7) des Direktkontakt-Wärmetauschers (1) verbunden ist, wobei das System ferner einen Dampfkondensator sowie eine Dampfturbine und/oder eine Kondensationsdampfturbine umfasst, der bzw. die mit dem Dampfkessel verbunden ist, dadurch gekennzeichnet, dass das System ferner eine Vorrichtung (5) zur Zugabe von Alkalisierungsmitteln dem Prozesswasser umfasst, wobei der Prozesswasserkreislauf ferner einen Einlass zum Anschließen der Vorrichtung (5) zur Zugabe von Alkalisierungsmitteln dem Prozesswasser umfasst, um den pH-Wert des Prozesswassers auf einer Ebene zu halten, die es möglich macht, korrosive Einwirkungen der sich während der Kondensation der Abgase bildenden Säuren zu neutralisieren, wobei der zweite Wärmetauscher (6) mit einem Kühlwassereinlass (19) versehen ist, der mit dem stromab der Kondensationsstufe der Dampfturbine und/der stromab der eigentlichen Dampfturbine angeordneten Dampfkondensator verbunden ist, wobei Kühlwasser das aus dem Dampfkondensator bezogene Dampfkondensat ist, dessen Temperatur zwischen 0 und 80 °C oder zwischen 0 und 80 °C oder zwischen 0 und 60 °C oder zwischen 0 und 50 °C oder zwischen 0 und 40 °C liegt, wobei der Kühlwasserauslass (20) des zweiten Wärmetauschers (6) mit dem Speisewassereinlass des Dampfkessels verbunden ist.
  2. Das System nach Anspruch 1, dadurch gekennzeichnet, dass der Kühlwasserauslass (20) des zweiten Wärmetauschers (6) mit einem Kühlwassereinlass (21) eines dritten Wärmetauschers (18) zur Wärmeübertragung von den Abgasen auf Kühlwasser verbunden ist, wobei der dritte Wärmetauscher (18) zwischen dem Abgasauslass einer Wärmequelle und dem Abgaseinlass (8) des Direktkontakt-Wärmetauschers (1) angeordnet ist, wobei ein Kühlwasserauslass (22) des dritten Wärmetauschers (18) mit dem Einspeisebehälter der Wärmequelle und/oder mit einem Heizkreis des Kessels und/oder mit einem anderen Heizkreis verbunden ist, wobei die Anlage ferner eine stromauf hinsichtlich dem Abgaseinlass (8) des Direktkontakt-Wärmetauscher (1) angeordnete Abzweigleitung (24) umfasst, die mit einem Regelglied (23) versehen und zu dem Abgasauslass (25) des Direktkontakt-Wärmetauschers (1) geführt ist, um die Auslasstemperatur der Abgase zu steigern und/oder um die Regelung der Endtemperatur der Abgase möglich zu machen und/oder um die Regelung der von dem Auslass zu den Wärmetäuschern (1, 6, 18) zu übertragender Wärmemenge möglich zu machen.
  3. Das System nach Anspruch 2, dadurch gekennzeichnet, dass es ferner eine Regelklappe (26) umfasst, die in dem Abgasauslass (25) des Direktkontakt-Wärmetauschers (1) angeordnet ist, um die Auslasstemperatur der Abgase zu steigern und/oder um die Regelung der Endtemperatur der Abgase möglich zu machen und/oder um die Regelung der von dem Auslass zu den Wärmetäuschern (1, 6, 18) zu übertragender Wärmemenge möglich zu machen.
  4. Das System nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, dass die Vorrichtung (5) zur Zugabe von Alkalisierungsmitteln dem Prozesswasser, um den pH-Wert des Prozesswassers auf einer Ebene zu halten, die es möglich macht, korrosive Einwirkungen der sich während der Kondensation der Abgase bildenden Säuren zu neutralisieren, mit dem Prozesswasserkreislauf mittels eines Absetzbehälters (3) verbunden ist.
  5. Das System nach Anspruch 1, dadurch gekennzeichnet, dass der Direktkontakt-Wärmetauscher (1) mit einer eingebauten Struktur (2) zur Steigerung des Wirkungsgrads der Wärmeübertragung, insbesondere zur Steigerung des Wirkungsgrads der Wärmeübertragung zwischen den Abgasen und dem Prozesswasser, und/oder zur Spülung der inneren Oberflächen des Direktkontakt-Wärmetauschers (1) und/oder zur Steigerung des Wirkungsgrads der Neutralisierung der sich während der Kondensation der Abgase bildenden Säuren ausgestattet ist.
  6. Das System nach Anspruch 1, dadurch gekennzeichnet, dass der Abgaseinlass (8) des Direktkontakt-Wärmetauschers (1) in dem unteren Abschnitt des Direktkontakt-Wärmetauschers (1) angeordnet ist, wohingegen der Prozesswassereinlass (7) zur Spülung der inneren Oberflächen des Direktkontakt-Wärmetauschers (1) und zur Zuführung der aus den Abgasen ausgekoppelten Wärme in dem oberen Abschnitt des Direktkontakt-Wärmetauschers (1) angeordnet ist.
  7. Das System nach Anspruch 1, dadurch gekennzeichnet, dass es ferner einen Absetzbehälter (3) zur Absetzung der aus dem Direktkontakt-Wärmetauscher (1) ausgespülten festen Partikeln umfasst, wobei der besagte Absetzbehälter zwischen dem Direktkontakt-Wärmetauscher (1) und dem zweiten Wärmetauscher (6) angeordnet und mit den beiden Wärmetauschern verbunden ist.
  8. Das System nach Anspruch 7, dadurch gekennzeichnet, dass der Absetzbehälter (3) zur Absetzung der aus dem Direktkontakt-Wärmetauscher (1) ausgespülten festen Partikeln mit einer Wegräumvorrichtung (16) versehen ist, die zum Entfernen von abgesetzten Ablagerungen aus dem Absetzbehälter (3) vorgesehen ist.
  9. Das System nach Anspruch 1, dadurch gekennzeichnet, dass die Vorrichtung (5) zur Zugabe von Alkalisierungsmitteln dem Prozesswasser, um den pH-Wert des Prozesswassers auf einer Ebene zu halten, die es möglich macht, korrosive Einwirkungen der sich während der Kondensation der Abgase bildenden Säuren zu neutralisieren, zum Halten des pH-Wertes des Prozesswassers auf einer Ebene angepasst ist, die höher ist als 5,0, insbesondere als 6,5, vorzugsweise als 6,9 und am meisten bevorzugt als 7,5.
  10. Das System nach Anspruch 7, dadurch gekennzeichnet, dass es ferner eine erste Prozesswasserpumpe (4) umfasst, die zwischen dem Absetzbehälter (3) zur Absetzung der aus dem Direktkontakt-Wärmetauscher (1) ausgespülten festen Partikeln und dem zweiten Wärmetäuscher (6) zur Wärmeübertragung von dem Prozesswasser auf Kühlwasser angeordnet ist.
  11. Das System nach Anspruch 1, dadurch gekennzeichnet, dass es ferner eine Vorrichtung (29) zur Ergänzung des Vorrats vom Prozesswasser und/oder zum Ablassen des letzteren umfasst, wobei die besagte Vorrichtung zwischen dem Prozesswasserauslass (9) des zweiten Wärmetauschers (6) und dem Prozesswassereinlass (7) des Direktkontakt-Wärmetauschers (1) angeordnet ist.
  12. Das System nach Anspruch 2, dadurch gekennzeichnet, dass der Kühlwasserauslass (22) des dritten Wärmetauschers (18) und/oder der Kühlwasserauslass (20) des zweiten Wärmetauschers (6) mit dem Speisewassereinlass des Dampfkessels und/oder einer anderen Wärmequelle und/oder eines anderen Heizkreises verbunden sind.
  13. Das System nach Anspruch 2, dadurch gekennzeichnet, dass der Kühlwasserauslass (22) des dritten Wärmetauschers (18) und/oder der Kühlwasserauslass (20) des zweiten Wärmetauschers (6) mit einem Wärmekreislauf verbunden sind, insbesondere mit einem Wärmekreislauf, der einen Kessel umfasst.
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CN108798813A (zh) * 2018-09-10 2018-11-13 技新（浙江）节能技术有限公司 一种钢厂烟气余热发电装置
CN109539222A (zh) * 2018-11-30 2019-03-29 江苏威特斯锅炉制造有限公司 一种冷凝蒸汽锅炉
CN110274491A (zh) * 2019-07-15 2019-09-24 中能服能源科技股份有限公司 一种用于烟道接触式烟气换热装置
CN113952752A (zh) * 2021-10-28 2022-01-21 镇海石化工程股份有限公司 酸性水汽提装置塔顶防腐蚀冷凝方法
CN115077281A (zh) * 2021-12-16 2022-09-20 程子剑 一种工业余热发电系统和方法

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CS136410B5 (de) * 1968-09-06 1970-05-15
US4340572A (en) * 1978-05-19 1982-07-20 Woodside Construction, Inc. Process for recovering heat from stack or flue gas
US4489679A (en) * 1983-12-12 1984-12-25 Combustion Engineering, Inc. Control system for economic operation of a steam generator
US4491093A (en) * 1984-03-26 1985-01-01 Hoekstra I Arthur Energy and water recovery from flue gases
DE3606681A1 (de) * 1986-02-27 1986-10-09 Mannesmann AG, 4000 Düsseldorf Verfahren und vorrichtung zur rueckgewinnung von abwaermeenergie
US4660511A (en) * 1986-04-01 1987-04-28 Anderson J Hilbert Flue gas heat recovery system
DE3809893A1 (de) * 1988-03-24 1989-10-12 Steag Fernwaerme Anordnung zur uebergabe von fernwaerme an eine wassererwaermungsanlage
GB8928621D0 (en) * 1989-12-19 1990-02-21 Emvertec Ltd Condensing economisers
DE4308310A1 (de) * 1993-03-16 1993-09-30 Tilo Dipl Ing Dolata Rauchgaswäscher mit Wärmerückgewinnung
DE19543449A1 (de) * 1995-11-22 1997-05-28 Deutsche Forsch Luft Raumfahrt Verfahren und Vorrichtung zur Nutzung der restlichen fühlbaren und der latenten Wärme eines Abgases einer Feuerungsanlage
SE9702830D0 (sv) * 1997-07-31 1997-07-31 Nonox Eng Ab Environment friendly high efficiency power generation method based on gaseous fuels and a combined cycle with a nitrogen free gas turbine and a conventional steam turbine
BRPI1013793A2 (pt) * 2009-06-26 2016-04-05 Dall Energy Holding Aps método e sistema para limpeza e recuperação de calor de gases quentes.

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None *

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