CN101706106B - Recovering device for afterheat of garbage incineration furnace - Google Patents
Recovering device for afterheat of garbage incineration furnace Download PDFInfo
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- CN101706106B CN101706106B CN2009102523489A CN200910252348A CN101706106B CN 101706106 B CN101706106 B CN 101706106B CN 2009102523489 A CN2009102523489 A CN 2009102523489A CN 200910252348 A CN200910252348 A CN 200910252348A CN 101706106 B CN101706106 B CN 101706106B
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- 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
Abstract
The invention discloses a recovering device for afterheat of garbage incineration furnace, which is implemented to cooperate with the main furnace body and the fume passage connected to the main furnace body; an evaporator, a superheater and an economizer are arranged in the fume passage, wherein a heat exchanger is also arranged in the fume passage; the heat exchanger at the tail of the fume passage recovers the heat energy of the fume at the outlet of a afterheat furnace, so that the temperature of the fume at the outlet of the afterheat furnace decreases and is controlled more efficiently, fume discharge loss of the afterheat furnace is reduced, and the heat efficiency of the afterheat furnace is enhanced; water spray on the fume for lowering temperature is unnecessary, thus saving quantities of water resource; and meanwhile a water spray device independently arranged for lowering temperature is not required, thus simplifying fume processing system technique, improving reliability of the fume processing system and prolonging the service life of the fume processing system equipment.
Description
Technical field
The relevant a kind of garbage burning boiler of the present invention is meant a kind of recovering device for afterheat of garbage incineration furnace especially.
Background technology
Municipal refuse is more and more, depend landfill alone, compost comes disposal of refuse can not adapt to the demand for development of society, garbage power can disposal of refuse not cause secondary pollution, simultaneously by generating, heat supply could also produce economic benefit, so the garbage burning boiler waste heat recovery more and more receives the people's concern!
The waste gas of incineration recovery boiler of conventional garbage incineration plant has two kinds of arrangement forms, and a kind of is vertical, and another kind is horizontal.The heat recovery boiler of vertical layout, horizontal layout generally is single drum, natural circulation boiler with water pipe.
Vertical layout heat recovery boiler as shown in Figure 1, its first passage 11 bottoms are fire grate 2 and adiabatic furnace 3.The flue gas that produces after the waste incineration flows through first, second and third passage 11,12,13 successively, has been covered with fin panel casing 1 around first, second and third passage 11,12,13.Third channel 13 has been arranged convection current evaporimeter and three 4.The 4th flue 14 has been arranged economizer 5 and/or flue gas air preheater.Evaporimeter (not shown) and superheater 4 are arranged in the smoke inlet of third channel 13, and superheater 4, economizer 5 pipes all adopt horizontally disposed, are furnished with smoke processing system 6 and sack cleaner 7 afterwards again.
Horizontal layout heat recovery boiler as shown in Figure 2,10 rear portions are provided with the exhaust gases passes that vertical fin panel casing 1 is formed in the combustion chamber, first, second and third channel 11,12,13 are the cavity cooling duct, and superheater and evaporimeter 4, economizer 5 are arranged in the 4th horizontal channel 14.Evaporimeter and superheater 4 are suspended in the horizontal flue top, are furnished with smoke processing system 6 and sack cleaner 7 afterwards again.
The waste heat boiler of above-mentioned two kinds of layouts, flue gas through with each heating surface heat exchange after, temperature by 850 the degree more than reduce to about about 220--200 ℃, enter smoke processing system 6, lower the temperature and depickling after, greatly when 150 ℃ of left and right sides, by sack cleaner 7, remove the particulate matter in the flue gas.At present, the smoke processing system of domestic garbage incinerating power plant generally adopts semidry method or dry method deacidifying process, and main employing makes flue-gas temperature drop to cooling about 150 ℃ from about 220 ℃ directly in the mode of reaction tower (or cooling tower) water spray or lime white.
But there is following shortcoming in above-mentioned existing heat recovery boiler:
1, because the acidic materials concentration in the refuse incineration exhaust-heating boiler outlet flue gas is higher, consider the problem of metal erosion, general flue-gas temperature is below 220-200 ℃ the time, and the heat energy in the flue gas is not utilized.Make the flue gas loss of boiler higher.
2, owing to normally adopt the mode that directly cools with water, be cooled to promptly can make the acidic materials in the flue gas to be easy to react flue gas with deacidification agent, the dew-point temperature that is higher than flue gas again can be disposed in the temperature that the sack cleaner 7 of back is accepted, and is generally about 150 ℃.In this process, a large amount of water to be consumed, in some flue gas purifying technique, even demineralized water will be used.Waste more water resource and energy consumption, increased the cost that flue gas is handled.Handle certain the factory's ruuning situation that adopts semidry process according to flue gas and analyze, the required water yield that is used for the flue gas processing of one ton of rubbish of every processing is about about 120 kg.With at present domestic medium-scale, day output is that 1000 tons incineration treatment of garbage factory is an example, is used for flue gas every day and handles the water that is consumed and be about 120 tons, consumes 40,000 tons of water in 1 year.Under the situation that the various places water resource is comparatively deficient at present, this situation should be improved to some extent.
3, owing to adopt the mode that directly cools with water, when the water spraying atomization device breaks down, cause the inlet temperature superelevation owing to sack cleaner easily, sack cleaner bypass valve interlocking is opened, and environmental pollution accident takes place.
4, be easy to take place cause flue gas processing device fouling and corrosion situation owing to reasons such as the water spraying atomization effect are bad.
Summary of the invention
The purpose of this invention is to provide a kind of recovering device for afterheat of garbage incineration furnace, it can reduce and is used for flue gas handles needed water resources consumption amount in garbage burning factory, reduce the flue gas loss of waste heat boiler, improve the thermal efficiency of refuse incineration exhaust-heating boiler, reduce the fault rate of smoke processing system simultaneously.
For achieving the above object, solution of the present invention is:
A kind of recovering device for afterheat of garbage incineration furnace is matched with boiler body and is connected in the exhaust gases passes on the boiler body and implements; Be provided with evaporimeter, superheater and economizer in the exhaust gases passes; Wherein: be provided with heat-exchanger rig in the exhaust gases passes.
Described heat-exchanger rig is provided in a side of flue-gas temperature 220-200 ℃ of rear portion of exhaust gases passes.
Described heat-exchanger rig is a feed-water heater.
Described feed-water heater connects the deaerator feedwater case, and the low pressure supply-water pump is sent into the low-pressure feed heater of being made up of the pipe row to the hot water in the deaerator storage tank, by behind the waste heat in the feed-water heater absorption flue gas water being returned to water tank.
Described heat-exchanger rig is the condensate water heater.
A branch of the outlet of low-temperature heater is taken from described condensate water heater water side entrance, and condensate water is boosted through condensate pump, behind low-temperature heater, enters the condensate water heater, carry out heat exchange with flue gas after, enter oxygen-eliminating device.
Described low-temperature heater is equipped with the automatic control and adjustment valve in order to the flow that enters the condensate water heater by control in the branch road of condensate water heater.
Described heat-exchanger rig is the hot-water heater of air preheater.
Condensate water in the described air preheater, be pooled to the hydrophobic expansion tank that is installed in the air preheater bottom, through the hot water booster, enter the air preheater hot-water heater, behind the heat temperature raising, get back to air preheater, lower the temperature with a secondary wind heat exchange, condensate water is got back to hydrophobic expansion tank, forms a closed cycle heat-exchange system.
The moisturizing of described this cycle heat exchange system can be adopted deaerator feedwater case automatic water supplement.
Described heat-exchanger rig is the synergic system heat power supply device.
The water side entrance of described synergic system heat power supply device connects a branch road that adds the condensate water of outlet from low, after condensate water enters the synergic system heat power supply device, entered full factory synergic system heat exchange station again by the flue gas heat temperature raising or enter lithium bromide unit refrigeration, the condensate water of cooling cooling is got back to full factory drain tank and is recycled.
After adopting such scheme, the present invention is by being installed in the heat-exchanger rig of flue afterbody, and the heat energy in the recovery waste heat boiler export flue gas makes the flue-gas temperature reduction of heat boiler outlet and obtained more effectively control, reduce the flue gas loss of waste heat boiler, improved the waste heat boiler thermal efficiency; Flue gas does not need to spray water for cooling, has saved great amount of water resources; Simultaneously do not need to have simplified smoke processing system technology, improved the reliability of smoke processing system, prolonged the service life of smoke processing system equipment for cooling is provided with water injector separately.
Description of drawings
Fig. 1 is the structural representation of prior art vertical boiler;
Fig. 2 is the structural representation of prior art horizontal boiler;
Fig. 3 is embodiment 1 structural representation of vertical boiler of the present invention;
Fig. 4 is embodiment 1 structural representation of horizontal boiler of the present invention;
Fig. 5 A is embodiment 2 structural representations of vertical boiler of the present invention;
Fig. 5 B is embodiment 2 structural representations of horizontal boiler of the present invention;
Fig. 6 A is embodiment 3 structural representations of vertical boiler of the present invention;
Fig. 6 B is embodiment 3 structural representations of horizontal boiler of the present invention;
Fig. 7 A is embodiment 4 structural representations of vertical boiler of the present invention;
Fig. 7 B is embodiment 4 structural representations of horizontal boiler of the present invention;
Fig. 8 A is embodiment 5 structural representations of vertical boiler of the present invention;
Fig. 8 B is embodiment 5 structural representations of horizontal boiler of the present invention.
The specific embodiment
Cooperate shown in Fig. 3 to Fig. 8 B the exhaust gases passes that a kind of recovering device for afterheat of garbage incineration furnace that the present invention discloses, this burning boiler comprise mainly the boiler body that is made of fire grate 2 and adiabatic furnace 3 and be connected on the boiler body and formed by water-cooling wall 1; In exhaust gases passes, be provided with evaporimeter, superheater 4 and economizer 5; Key of the present invention is: also be provided with heat-exchanger rig 8 in the exhaust gases passes.
Shown in Fig. 3,5A, 6A, 7A, 8A, in the vertical garbage burning boiler of the present invention, this heat-exchanger rig 7 is the afterbodys that are arranged in flue, after flue-gas temperature 220-200 ℃.The flue gas that burns is through the water-cooled cavity or the heating surface (superheater 4, economizer 5) of first, second, third and fourth passage 11,12,13,14, the heat-exchanger rig 7 that is set at the flue afterbody absorbs the waste heat in the flue gases, make flue-gas temperature from 220-200 ℃, reduce to about 170-140 ℃.This heat-exchanger rig 8 can be feed-water heater (shown in Fig. 5 A), condensate water heater (as shown in Figure 6A), is used for the hot-water heater (shown in Fig. 7 A) or the synergic system low-pressure steam thermal source of elementary air preheater, as the winter heating heat supply, provide (as Fig. 8 As shown in) such as thermals source for lithium bromide refrigerator summer.
Shown in Fig. 4,5B, 6B, 7B, 8B, in the horizontal garbage burning boiler of the present invention, evaporimeter and superheater 4 and economizer 5 are arranged in the 4th horizontal flue 14, and in the 4th horizontal flue 14, after flue-gas temperature 220-200 ℃, are provided with heat-exchanger rig 8.The waste heat that heat-exchanger rig 8 absorbs in the flue gas makes flue-gas temperature from 220-200 ℃, reduces to about 170-140 ℃.This heat-exchanger rig 7 can be feed-water heater (shown in Fig. 5 B), condensate water heater (shown in Fig. 6 B), is used for the hot-water heater (shown in Fig. 7 B) or the synergic system low-pressure steam thermal source of elementary air preheater, as the winter heating heat supply, provide (as Fig. 8 Bs shown in) such as thermals source for lithium bromide refrigerator summer.
Shown in Fig. 5 A, 5B, of the present invention vertical/first kind of heat-exchanger rig 8 of horizontal garbage burning boiler is low-pressure feed heater, deaerator feedwater case 81 is taken from the water source of feed-water heater, through low pressure supply-water pump 82, is temperature in the feed-tank 81 that 126-129 ℃ hot water is sent into the low-pressure feed heater of being made up of the pipe row, behind the waste heat in the feed-water heater absorption flue gas, be warming up to 150-170 ℃, return to water tank 81.
Press the pressure in the deaerator feedwater case to be about 0.24-0.26Mpa in general, the water temperature in the feed-tank should be 126-129 ℃ at this moment, and the fume side temperature of low-pressure feed heater is about 220-140 ℃, and tube wall temperature is higher than acid dew-point temperature, is difficult for taking place cold end corrosion.
Shown in Fig. 6 A, 6B, of the present invention vertical/second kind of heat-exchanger rig 8 of horizontal garbage burning boiler is the condensate water heater.A branch of the outlet of low-temperature heater 83 is taken from the condensate water heater water side entrance that is installed in the flue afterbody.Condensate water is boosted through condensate pump 84, behind low-temperature heater 83, temperature rise to 110 the degree, enter the condensate water heater, carry out heat exchange with flue gas after, be warming up to about the 130-150 degree, enter oxygen-eliminating device 85.
The branch road from low-temperature heater 83 to the condensate water heater, automatic control and adjustment valve 86 is installed, in order to enter the flow of condensate water heater by control, realize the exit gas temperature of control condensate water heater, make the flue-gas temperature of condensate water heater outlet keep constant substantially.
Shown in Fig. 7 A, 7B, of the present invention vertical/the third heat-exchanger rig 8 of horizontal garbage burning boiler is the hot-water heater of air preheater.One auxiliary air preheating of present conventional incinerator generally is divided into secondary, and the one-level heater is generally drawn gas by steam turbine or the station-service low-pressure steam is done the vapour source.The present invention utilizes waste heat in the incinerator flue tail flue gas as thermal source, and to the condensate water heating of air preheater 87, promptly the condensate water with air preheater 87 is a medium, the waste heat in the flue gas, imports the hot-water heater of air preheater.The flow process of water side is in the air preheater 87: be about 110-120 ℃ air preheater condensate water, be pooled to the hydrophobic expansion tank 88 that is installed in the air preheater bottom, through hot water booster 89, enter the air preheater hot-water heater, heat to 150-160 ℃, get back to air preheater 87, lower the temperature with a secondary wind heat exchange, condensate water is got back to hydrophobic expansion tank 88, forms a closed cycle heat-exchange system.The moisturizing of this circulatory system can be adopted oxygen-eliminating device 80 feed-tank automatic water supplements, or other suitable water supplementing method.
Shown in Fig. 8 A, 8B, of the present invention vertical/the 4th kind of heat-exchanger rig 8 of horizontal garbage burning boiler is the synergic system thermal source.At present the winter heating of power plant, summer the lithium bromide refrigerating unit thermal source generally take from the low-pressure pumping steam of steam turbine, consumed certain heat.And, at refuse-burning plant, because the variation of refuse thermal value, pressure that steam turbine draws gas and flow are all stable inadequately, particularly under the situation of steam turbine underrun, pressure that draws gas and flow generally can not satisfy the requirement of synergic system with vapour, need to adopt other high-quality steam as additional vapour source, have reduced the economy of full factory therrmodynamic system.
Synergic system heat power supply device of the present invention has absorbed the waste heat of waste heat boiler tail flue gas, produces about 130-150 ℃ steam, enters full factory synergic system heat exchange station or directly enters lithium bromide unit 802 refrigeration.The water side entrance of this synergic system heat power supply device connects a branch road that adds the condensate water of about 110 ℃ of outlets from low, after condensate water enters the synergic system heat power supply device,, entered full factory synergic system heat exchange station again or enter lithium bromide unit 802 refrigeration to about 130-150 ℃ by the flue gas heat temperature raising.Condensate water through the cooling cooling is got back to full factory drain tank 801, recycles.
Show that according to related data the acidic materials dew point of refuse incineration exhaust-heating boiler outlet flue gas is generally at 110-120 ℃, in the above-mentioned four kinds of heat-exchanger rigs of the present invention, the temperature of water inlet is minimum about 110 ℃.Therefore, will be according to the temperature of tube wall, the specified temp and the needed hot water temperature of heat-exchanger rig outlet flue gas, heat-exchanger rig is arranged to following current layout or counter-flow arrangement, the material of heat exchanger also can be selected the conventional boiler tube material according to tube wall temperature, perhaps partly or entirely adopts corrosion-resistant steel pipe.
Be to strengthen the heat exchange efficiency of heat-exchanger rig, heat exchanger can adopt all kinds efficient heat-exchanging pipe, as the fin heat pipe etc., to increase the heat exchange effect.
Flue-gas temperature behind above-mentioned four kinds of heat-exchanger rigs all can be by being installed in the water regulating valve gate control on the various heat-exchanger rig inlet pipelines, thereby the exit gas temperature that has guaranteed waste heat boiler remains on needed specified temp in the 140-170 ℃ of scope.
After being provided with any above-mentioned heat-exchanger rig, in the smoke processing system technology behind stove following improvement application can be arranged:
For the deacidifying process of rotating spraying semidry method, following several improvement project can be arranged:
The heat boiler outlet temperature can be set in section higher between 140-170 ℃, cancels the desuperheating water system that is provided with separately for cooling, keeps rotary atomization device and lime white and prepares supply system; The concentration of lime white can bring up to can guarantee that lime fully dissolves and can be by atomizing effectively, the temperature of flue gas in reaction tower dropped to be higher than the degree of about 20 ℃ of flue gas acid dew points after the depickling again.Like this, simplify flue gas treating process, owing to improved lime white concentration, can also suitably dwindle the specification of equipment that lime white prepares supply system simultaneously, reduced the workload of equipment investment and equipment repair and maintenance.
The heat boiler outlet temperature can be set in section lower between 140-170 ℃, desuperheating water system that cancellation is provided with separately for cooling and rotary atomization device and lime white prepare supply system, replace that strength is carried or alternate manner sprays into reaction tower with pulverized limestone.The temperature of flue gas in reaction tower dropped to about 135 ℃.Can farthest simplify deacidifying flue gas system process equipment like this, improve the reliability of equipment, reduce and build and operation cost.
Flue gas treating process for " cooling tower (spray cooling)+reaction tower (spray pulverized limestone) " can adopt the cancellation cooling tower, perhaps only keeps cooling tower in order to answer quench under the accident conditions.Keep reaction tower.The flue-gas temperature of reaction tower can be arranged on about 140 ℃, make flue gas in reaction tower with the direct haptoreaction of drystone ashes, reach the purpose of removing the acidic materials in the flue gas.Like this, simplify flue gas treating process largely, reduced floor space, saved engineering and equipment investment.
Flue gas treating process for employing NID system because the reaction tower inlet flue gas temperature is lower, can not add any water spray in the reuse ash, has avoided owing to load variations is untimely with the water spray adjusting problem that the reaction tower that causes stops up or corrodes.Simultaneously,, can cancel a whole set of spray cooling device, simplify flue gas treating process because do not need water spray.
Therefore, recovering device for afterheat of garbage incineration furnace of the present invention has following beneficial effect:
1) the present invention is installed in the heat-exchanger rig of flue afterbody, and the heat energy in the recovery waste heat boiler export flue gas makes the flue-gas temperature reduction of waste heat boiler outlet and obtained more effectively control, has reduced the flue gas loss of waste heat boiler, improves the waste heat boiler thermal efficiency;
2) because the present invention has installed heat-exchanger rig at the flue afterbody, the outlet cigarette temperature of waste heat boiler is dropped between 140-170 ℃, flue gas does not need to spray water for cooling, has saved a large amount of water resources.
3) because waste heat boiler flue afterbody outlet cigarette temperature can be controlled at needed temperature range reliably by heat-exchanger rig, do not need in the flue gas treatment system for cooling water injector to be set separately, simplify flue gas treatment system technology, improved the reliability of flue gas treatment system.
4) because heat-exchanger rig of the present invention, make the temperature reduction of waste heat boiler outlet flue gas and obtained reliable control, flue gas is processed no longer needs water spray, reduced owing to the flue gas treatment system fouling of water spray initiation or the probability of corrosion, prolonged the service life of flue gas treatment system equipment.
Claims (3)
1. recovering device for afterheat of garbage incineration furnace is matched with boiler body and is connected in the exhaust gases passes on the boiler body and implements; Be provided with evaporimeter, superheater and economizer in the exhaust gases passes; Be provided with heat-exchanger rig in the exhaust gases passes; It is characterized in that: heat-exchanger rig is the hot-water heater of air preheater; Condensate water in the air preheater, be pooled to the hydrophobic expansion tank that is installed in the air preheater bottom, through the hot water booster, enter the hot-water heater of air preheater, behind the heat temperature raising, get back to air preheater, lower the temperature with the primary and secondary air heat exchange, condensate water is got back to hydrophobic expansion tank, forms a closed cycle heat-exchange system.
2. recovering device for afterheat of garbage incineration furnace as claimed in claim 1 is characterized in that: heat-exchanger rig is provided in a side of flue-gas temperature 220-200 ℃ of rear portion of exhaust gases passes.
3. recovering device for afterheat of garbage incineration furnace as claimed in claim 1 or 2 is characterized in that: deaerator feedwater case automatic water supplement is adopted in the moisturizing of this cycle heat exchange system.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009102523489A CN101706106B (en) | 2009-11-26 | 2009-11-26 | Recovering device for afterheat of garbage incineration furnace |
| HK10110273.5A HK1143853A1 (en) | 2009-11-26 | 2010-11-03 | Recovering device for afterheat of garbage incineration furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009102523489A CN101706106B (en) | 2009-11-26 | 2009-11-26 | Recovering device for afterheat of garbage incineration furnace |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101706106A CN101706106A (en) | 2010-05-12 |
| CN101706106B true CN101706106B (en) | 2011-09-21 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2009102523489A Expired - Fee Related CN101706106B (en) | 2009-11-26 | 2009-11-26 | Recovering device for afterheat of garbage incineration furnace |
Country Status (2)
| Country | Link |
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| CN (1) | CN101706106B (en) |
| HK (1) | HK1143853A1 (en) |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101936533A (en) * | 2010-09-26 | 2011-01-05 | 安徽金鼎锅炉股份有限公司 | Waste incineration exhaust heat boiler |
| CN101943412A (en) * | 2010-09-26 | 2011-01-12 | 安徽金鼎锅炉股份有限公司 | Waste incineration exhaust-heat boiler |
| CN103398591B (en) * | 2013-08-18 | 2015-07-01 | 广东工业大学 | Waste heat utilization system for aluminium melting furnace |
| CN104912755A (en) * | 2015-06-10 | 2015-09-16 | 中国华电工程(集团)有限公司 | Fresnel type solar photo-thermal and natural gas combined power generating system |
| CN106678772A (en) * | 2016-12-27 | 2017-05-17 | 安徽海螺川崎工程有限公司 | Waste heat boiler system for electricity generation through waste incineration |
| CN107062296A (en) * | 2017-03-29 | 2017-08-18 | 江联重工集团股份有限公司 | One kind prevents station boiler low-temperature corrosion system |
| CN107166350B (en) * | 2017-05-24 | 2018-10-26 | 东华工程科技股份有限公司 | A kind of process of the vertical water-cooling wall waste heat boiler steam production of control |
| CN107828449A (en) * | 2017-11-08 | 2018-03-23 | 中科合肥煤气化技术有限公司 | A kind of device for reclaiming gasification furnace coal gas of high temperature heat |
| CN108561886A (en) * | 2018-06-29 | 2018-09-21 | 许义保 | A kind of horizontal domestic waste incineration |
| CN109764338A (en) * | 2019-01-16 | 2019-05-17 | 广州环投设计研究院有限公司 | A kind of garbage incinerating power plant is exhaust heat stepped to utilize method |
| CN111219720A (en) * | 2020-01-20 | 2020-06-02 | 山东电力工程咨询院有限公司 | Flue gas waste heat utilization system and method for waste incineration power plant |
| CN113289484A (en) * | 2021-05-06 | 2021-08-24 | 泸州市兴泸环保发展有限公司 | Waste incineration flue gas deacidification system and deacidification method |
| CN113413756A (en) * | 2021-06-23 | 2021-09-21 | 杭州新世纪能源环保工程股份有限公司 | Flue gas purification process for synergetic catalysis of denitration and deacidification and dioxin pyrolysis |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86105222A (en) * | 1986-08-14 | 1987-06-24 | 西安交通大学 | Utilize the low-pressure energy-saving hybrid system of smoke discharging residual heat |
| CN101372905A (en) * | 2006-10-14 | 2009-02-25 | 戴克发 | Energy-saving improvement (comprehensive utilization of heat energy) of thermal power station conventional heat engineering system |
| CN201310896Y (en) * | 2008-11-20 | 2009-09-16 | 北京国电龙源杭锅蓝琨能源工程技术有限公司 | Biomass incinerator of high temperature and high pressure circulating fluidized bed |
-
2009
- 2009-11-26 CN CN2009102523489A patent/CN101706106B/en not_active Expired - Fee Related
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2010
- 2010-11-03 HK HK10110273.5A patent/HK1143853A1/en not_active IP Right Cessation
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86105222A (en) * | 1986-08-14 | 1987-06-24 | 西安交通大学 | Utilize the low-pressure energy-saving hybrid system of smoke discharging residual heat |
| CN101372905A (en) * | 2006-10-14 | 2009-02-25 | 戴克发 | Energy-saving improvement (comprehensive utilization of heat energy) of thermal power station conventional heat engineering system |
| CN201310896Y (en) * | 2008-11-20 | 2009-09-16 | 北京国电龙源杭锅蓝琨能源工程技术有限公司 | Biomass incinerator of high temperature and high pressure circulating fluidized bed |
Non-Patent Citations (1)
| Title |
|---|
| JP特开2002-5402A 2002.01.09 |
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| Publication number | Publication date |
|---|---|
| CN101706106A (en) | 2010-05-12 |
| HK1143853A1 (en) | 2011-01-14 |
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