CN102168590A - Gas turbine generating system using flue gas waste heat organic hydrocarbon mixture - Google Patents
Gas turbine generating system using flue gas waste heat organic hydrocarbon mixture Download PDFInfo
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- CN102168590A CN102168590A CN2011100619959A CN201110061995A CN102168590A CN 102168590 A CN102168590 A CN 102168590A CN 2011100619959 A CN2011100619959 A CN 2011100619959A CN 201110061995 A CN201110061995 A CN 201110061995A CN 102168590 A CN102168590 A CN 102168590A
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- flue gas
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Abstract
The invention discloses a gas turbine generating system using a flue gas waste heat organic hydrocarbon mixture (such as n-pentane, isopentane, butane and the like). The system is characterized by comprising an organic hydrocarbon mixture-flue gas heat exchanger, an organic hydrocarbon mixture turbine engine, a power generator, a steam condenser and an organic hydrocarbon mixture condensing pump, wherein a working medium of the turbine engine is the organic hydrocarbon mixture; an organic working medium discharged from the organic hydrocarbon mixture turbine engine passes through a booster pump after being condensed and cooled in the steam condenser; and the organic working medium is pumped into the heat exchanger to be heated and evaporated and then enters the turbine engine to finish a closed circulation. The heat energy of the exhaust smoke is sufficiently used to reduce heat emission for atmosphere. After the temperature of the flue gas at an entrance of a desulfurization absorption tower is reduced, the evaporated water in the absorption tower is reduced and water consumption of a desulfurization process is correspondingly saved so that the purpose of saving water can be achieved.
Description
Technical field
The present invention relates to power generation system, especially a kind of fume afterheat organic carbon hydrogen mixture turbine generating system that utilizes.
Background technique
Flue gas loss is a most important thermal loss in the boiler operatiopn, all there is the situation above design load in a lot of exhaust gas temperatures of Power Plant in China, to the exhaust gas temperature design load of burning anthracite, meager coal, bituminous coal usually about 120～125 ℃, its temperature of exhaust fume design load of boiler of burning brown coal is usually about 155 ℃, and exhaust gas volumn is very big, can reach (300～400) * 10 usually to separate unit 600MW unit induced draught fan outlet exhaust gas volumn
4m
3/ h.In order to reduce flue gas loss, reduce temperature of exhaust fume, energy saving, improve the Economy of power plant, have at present and adopt low-level (stack-gas) economizer to manage to improve the situation of the utilization ratio of high-temperature flue gas, Fig. 1 is that the system of low-level (stack-gas) economizer connects signal, from certain low-pressure heater extension or whole condensed water, is sent to low-level (stack-gas) economizer usually.
The arrangement of organic carbon hydrogen mixture-flue gas heat exchange device (hereinafter to be referred as the flue gas heat exchange device):
As shown in Figure 3, the arrangement of organic carbon hydrogen mixture-flue gas heat exchange device (hereinafter to be referred as the flue gas heat exchange device) has two kinds of selections: after scheme one is arranged in air preheater, before the electric cleaner; After scheme two is arranged in induced draught fan, before the desulfurizer.
Prior art: scheme one: after being arranged in air preheater, before the electric cleaner
Many large thermal power plants of Japan, all there are similar arrangements in that jade-like stone power plant (1000MW) of land as usual and Tomato-Atsuma power plant (700MW) etc.The GGH flue gas heat release section of tubular type is arranged between air preheater and the deduster.Tubular type GGH is reduced to flue-gas temperature about 90 ℃, and adopts low low temperature electric precipitator.So-called low cold precipitator is meant that entrance flue gas temperature is at the deduster below 100 ℃.To this kind arrangement, in view of present domestic situation,, to reduce risks for reducing the possibility of flue gas heat exchange device corrosion, suggestion flue gas heat exchange device outlet cigarette temperature is higher than above 5 ℃ of flue gas acid dew point.
The risk of this arrangement maximum is burn into dust stratification, wearing and tearing.Flue gas heat exchange device outlet cigarette temperature more than the flue gas flue gas acid dew point 5 ℃ will be hanged down 3～4 ℃ through inlet flue gas temperature behind the induced draught fan behind flue, the deduster, near acid dew point, to all flues, induced draught fan will be considered the anti-low-temperature corrosion measure behind the flue gas heat exchange device.Flue gas heat exchange device outlet flue gas running temperature is a little more than acid dew-point temperature, through flue before the deduster and deduster, in deduster tail flue gas temperature also near acid dew point, harm to the electric cleaner maximum is metal constructions such as long-pending dew of flue gas and corrosion electric cleaner housing, the long-pending dew of electroceramics spare (insulator, porcelain axle) is creepage and then discharge smashes, the generation accident influences the safe operation and the life-span of electric cleaner.Therefore in the time of before the flue gas heat exchange device is arranged electric cleaner, need to consider the influence of these factors, mainly contain the following aspects:
1) electric cleaner is carried out preservative treatment.To the consulting of relevant deduster producer, mainly concentrate on the following aspects:
(1) sealing.Electric cleaner should have and well prevents the measure of leaking out, what electric cleaner was too much leaks out, it is excessive to cause the interior cigarette temperature of electric cleaner to descend on the one hand, and the aggravation flue gas amasss to reveal and works the mischief, and near leaking out a little, because flue-gas temperature is very low, must have long-pending revealing to produce, this place will produce corrosion in short-term, and the time has been grown corrosion area expansion and finally caused electric cleaner normally to use, and leaking out of electric cleaner a little mainly is to pass the electric cleaner hole, and promptly manhole door, rapping perforation, negative electrode are hung etc.
(2) insulation.In order fully to keep flue gas temperature in electric cleaner, objectively increase insulation layer thickness or select the littler thermal insulating material of thermal conductivity that the low temperature electric cleaner is carried out the INSULATION DESIGN construction.
(3) insulator is carried out hot-air blowing.The electric cleaner insulator is industrial electroceramics, its inwall is in the electric field flue gas environment, because the cigarette temperature is low excessively, internal surface is easy to generate long-pending revealing and quilt band dust pollution, all insulators are carried out effective heat tracing make its temperature more than flue gas acid dew point, carry out the forced air purging to its internal surface in 10～15 ℃, guarantee to hang insulator surface from measure and do not produce long-pending dew phenomenon, and keep its cleaning, thereby guarantee that insulator not by the fertile electrical breakdown of long-pending dew, makes its safe operation.
(4) prevent that printed line is stained with ash.Because flue-gas temperature reduces, and has increased grey viscosity, thereby must suitably improve the vibration acceleration of printed line, suitably improve the rapping frequency on the other hand, the sticking ash of prevention printed line for the electric cleaner of this moment.Adopt easy-to-clean ash uncorruptible material as stainless steel helix or stainless steel discharge prickle etc. for cathode line.
(5) consider sour gas because long-pending corrosion of revealing to housing, the housing of electric cleaner adopt anticorrosive preferred metal material as: examine time steel or acid-proof coating, to prolong the working life of electric cleaner.
More than be some the specific aim measures to low temperature electric cleaner safe and reliable operation, keep suitably high flow velocity for such electric cleaner electric field planted agent, it is disadvantageous that low excessively flue gas flow rate keeps cigarette temperature in the electric field.Therefore, the deduster behind the flue gas heat exchange device is under same examination condition, and when electric precipitation bulk volume, specific collection area etc. are not considered the situation of input gas temperature reduction, the conventional temperature electric cleaner of the output investment ratio of electric cleaner will increase to some extent.
2) the easy dust stratification of heat exchange pipeline in the flue gas heat exchange device, maintenance cost is higher.Flue gas is not owing to gather dust through electric cleaner, and the ash content in the flue gas is higher, and when by low-level (stack-gas) economizer, very easily dust stratification influences the heat exchange effect.Therefore need in the flue gas heat exchange device, be provided with and effectively blow grey measure, to reduce the influence of dust stratification.
3) because flue gas is not gathered dust, easily the heat exchange pipeline in the flue gas heat exchange device is caused wearing and tearing, operation risk is big.
4) to all flue, induced draught fan will be considered the anti-low-temperature corrosion measure behind the flue gas heat exchange device.For induced draught fan, need to consider the preservative treatment of induced draught fan blade and flow passage component, the manufacturer of domestic induced draught fan does not still have this design experiences.It is longer to carry out antiseptic flue length, until the flue of desulfurizer inlet all needs to carry out the preservative treatment of the clean flue of similar desulfurization, expense is higher from the outlet of flue gas heat exchange device.
5) the heat exchanging tube material of flue gas heat exchange device is chosen the corrosion that should consider that the flue gas running temperature causes about dew point temperature, considers flue gas again not by the wearing and tearing of gathering dust and causing, and domestic existing material is difficult to adapt to rugged environment like this.Conclusion:
At present technical situation, the problem of scheme one maximum is burn into dust stratification, wearing and tearing,
Except that above problem, arrangement one can't utilize the temperature rise of flue gas by induced draught fan, and income is relatively poor.
Summary of the invention
The low-level (stack-gas) economizer scheme is to improve heat regenerative system efficient with the flue gas heating water of condensation, is there there the system that does not directly utilize the fume afterheat generating? we study and have designed a cover fume afterheat power generation system, both can be used for the thermal power plant, also can be used for the occasion that industries such as iron and steel, chemical industry have heat loss due to exhaust gas.As shown in Figure 2, comprise organic hydrocarbon mixture-flue gas heat exchange device, organic carbon hydrogen mixture steam turbine, generator, the organic carbon hydrogen mixture pump that condenses.The medium of doing manual work in the steam turbine be the organic carbon hydrogen mixture (as just, isopentane, butane), the organic working medium of discharging from steam turbine will enter vapour condenser (air cooling or clammy) and condense after the cooling, pass through booster pump, once more organic working medium is pumped into heat exchanger and heat, evaporate and enter steam turbine again, finish closed cycle.
The characteristics of this system are to heat low boiling working fluid with fume afterheat, make it heat in heat exchanger, evaporate and enter steam turbine, and smoke evacuation heat energy is made full use of, and reduce the atmospheric heat discharging.
After flue gas heat exchange device of the present invention is arranged in induced draught fan, before the desulfurizer:
To this kind arrangement, flue gas can utilize the temperature rise after flue gas passes through induced draught fan after passing through deduster front and back flue and deduster.
Adopt this arrangement advantage to be, electric cleaner, induced draught fan do not need to carry out preservative treatment, and flue-gas temperature can drop to very low reaching about 60 ℃ behind the flue gas heat exchange device, can adopt the electric cleaner and the induced draught fan of domestic routine, and technology maturation is reliable; Flue gas is utilized by the temperature rise of induced draught fan, and income is obvious; The wearing and tearing of the interior heat exchange pipeline of flue gas heat exchange device are less, and dust stratification is few, and operation risk greatly reduces.The shortcoming that adopts this arrangement is the raising electric cleaner efficient that can't utilize the flue-gas temperature reduction to bring, the benefit that reduces induced draught fan power.
Comprehensive relatively, present stage the flue gas heat exchange device the plan of establishment, employing scheme two.
In sum, owing to adopted technique scheme, the invention has the beneficial effects as follows:
1, this programme adopts fume afterheat heating low boiling working fluid (organic carbon hydrogen mixture), make it in heat exchanger, heat, evaporate and enter steam turbine, drive steam turbine, and then the pushing generator generating, smoke evacuation heat energy is made full use of, reduce the atmospheric heat discharging.
2, after the desulfuration absorbing tower entrance flue gas temperature reduced, evaporated water reduced in the absorption tower, and the corresponding saving of sulfur removal technology water consumption can be played water-saving purpose.
3, by present stage electric cleaner and induced draught fan material and state-of-art, advanced more, the science of the present stage arrangement two of flue gas heat exchange device.
Description of drawings
The present invention will illustrate by example and with reference to the mode of accompanying drawing, wherein:
System's connection diagram of Fig. 1 low-level (stack-gas) economizer.
Fig. 2 is that the present invention utilizes fume afterheat organic carbon hydrogen mixture turbine generating system.
Fig. 3 flue gas heat exchange device arrangement (last figure is a prior art scheme one, and figure below is the present invention program two)
Embodiment
Disclosed all features in this specification, or the step in disclosed all methods or the process except mutually exclusive feature and/or step, all can make up by any way.
Disclosed arbitrary feature in this specification (comprising any accessory claim, summary and accompanying drawing) is unless special narration all can be replaced by other equivalences or the alternative features with similar purpose.That is, unless special narration, each feature is an example in a series of equivalences or the similar characteristics.
As shown in Figure 2, comprise organic hydrocarbon mixture-flue gas heat exchange device, organic carbon hydrogen mixture steam turbine, generator, the organic carbon hydrogen mixture pump that condenses.The medium of doing manual work in the steam turbine be the organic carbon hydrogen mixture (as just, isopentane, butane), the organic working medium of discharging from steam turbine will enter vapour condenser (air cooling or clammy) and condense after the cooling, pass through booster pump, once more organic working medium is pumped into heat exchanger and heat, evaporate and enter steam turbine again, finish closed cycle.
Technological process is as follows: the concentrated ammonia liquor in the concentrated ammonia liquor storage tank through concentrated ammonia liquor booster pump line transportation to heat exchanger heat, evaporation, gas-liquid separation, gas is inhaled into steam turbine, liquid flows into the weak aqua ammonia storage tank, ammonia after doing manual work in steam turbine is delivered to jet pump with being recycled to the concentrated ammonia liquor storage tank from the weak aqua ammonia behind the weak aqua ammonia booster pump through the steam turbine outlet pipe, thereby formation closed loop, smoke evacuation heat energy is made full use of, reduce the atmospheric heat discharging.
The present invention is not limited to aforesaid embodiment.The present invention expands to any new feature or any new combination that discloses in this manual, and the arbitrary new method that discloses or step or any new combination of process.
Claims (4)
1. one kind is utilized fume afterheat organic carbon hydrogen mixture turbine generating system, it is characterized in that comprising organic hydrocarbon mixture-flue gas heat exchange device, organic carbon hydrogen mixture steam turbine, generator, gas condensating device, the organic carbon hydrogen mixture pump that condenses; The medium of doing manual work in the steam turbine is the organic carbon hydrogen mixture, the organic working medium of discharging from described organic carbon hydrogen mixture steam turbine will enter described gas condensating device and condense after the cooling, by booster pump, once more organic working medium is pumped into heat exchanger and heat, evaporate and enter steam turbine again, finish closed cycle.
2. the fume afterheat organic carbon hydrogen mixture turbine generating system that utilizes according to claim 1 is characterized in that described organic carbon hydrogen mixture or pentane or isopentane or butane.
3. the fume afterheat organic carbon hydrogen mixture turbine generating system that utilizes according to claim 1, the working method that it is characterized in that described gas condensating device is an air cooling or clammy.
4. the fume afterheat organic carbon hydrogen mixture turbine generating system that utilizes according to claim 1 is characterized in that described organic carbon hydrogen mixture--after-flue gas heat exchange device is arranged on induced draught fan, before the desulfurizer.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011100619959A CN102168590A (en) | 2011-03-15 | 2011-03-15 | Gas turbine generating system using flue gas waste heat organic hydrocarbon mixture |
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| CN2011100619959A CN102168590A (en) | 2011-03-15 | 2011-03-15 | Gas turbine generating system using flue gas waste heat organic hydrocarbon mixture |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102337934A (en) * | 2011-09-13 | 2012-02-01 | 上海盛合新能源科技有限公司 | Combined cycle generating system for improving heat source usage efficiency |
Citations (6)
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| US4262485A (en) * | 1977-12-02 | 1981-04-21 | Hitachi, Ltd. | Low boiling point medium power plant |
| IL81265A (en) * | 1986-03-05 | 1992-03-29 | Hisaka Works Ltd | Evaporating apparatus |
| DE102006057448A1 (en) * | 2006-12-06 | 2008-06-12 | Ibb Technology Gmbh | Method for increasing performance and efficiency in the ORC power plant process |
| CN201251371Y (en) * | 2008-10-17 | 2009-06-03 | 华润电力投资有限公司 | Flue gas pre-cooling system with highly-effective water and energy conservation |
| CN101788233A (en) * | 2010-02-25 | 2010-07-28 | 首钢总公司 | Heating-furnace cogeneration system and method thereof |
| CN102121405A (en) * | 2011-02-28 | 2011-07-13 | 无锡三达环保科技有限公司 | Low-grade smoke organic rankine cycle waste heat generating system of heating furnace in steel rolling plate plant |
-
2011
- 2011-03-15 CN CN2011100619959A patent/CN102168590A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4262485A (en) * | 1977-12-02 | 1981-04-21 | Hitachi, Ltd. | Low boiling point medium power plant |
| IL81265A (en) * | 1986-03-05 | 1992-03-29 | Hisaka Works Ltd | Evaporating apparatus |
| DE102006057448A1 (en) * | 2006-12-06 | 2008-06-12 | Ibb Technology Gmbh | Method for increasing performance and efficiency in the ORC power plant process |
| CN201251371Y (en) * | 2008-10-17 | 2009-06-03 | 华润电力投资有限公司 | Flue gas pre-cooling system with highly-effective water and energy conservation |
| CN101788233A (en) * | 2010-02-25 | 2010-07-28 | 首钢总公司 | Heating-furnace cogeneration system and method thereof |
| CN102121405A (en) * | 2011-02-28 | 2011-07-13 | 无锡三达环保科技有限公司 | Low-grade smoke organic rankine cycle waste heat generating system of heating furnace in steel rolling plate plant |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102337934A (en) * | 2011-09-13 | 2012-02-01 | 上海盛合新能源科技有限公司 | Combined cycle generating system for improving heat source usage efficiency |
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Application publication date: 20110831 |