CN204960999U - Coal -fired residual heat from flue gas system of two -stage organic rankine cycle of high -efficient circulation evaporation - Google Patents
Coal -fired residual heat from flue gas system of two -stage organic rankine cycle of high -efficient circulation evaporation Download PDFInfo
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Abstract
The utility model discloses a coal -fired residual heat from flue gas system of two -stage organic rankine cycle of high -efficient circulation evaporation is equipped with high temperature level evaporimeter, high temperature level pre -heater, low temperature level evaporimeter and low temperature level pre -heater in proper order in the flue, retrieve the flue gas waste heat through working medium circulation heat absorption. The system selects circulating evaporimeter for use, and the outer wall temperature of control low temperature level evaporimeter is higher than the water dew point, and the outer wall temperature of control high temperature level evaporimeter is higher than sour dew point. Low temperature level pre -heater adopts the good heat conduction plastics heat exchange tube of corrosion resistance, and the high temperature level is preheated in low temperature level pre -heater earlier before preheating, evaporate the required working medium of link entering high temperature level pre -heater, can avoid high temperature level pre -heater the situation that outer wall temperature is less than the water dew point also to appear. In addition, low temperature level evaporimeter and high temperature level evaporimeter use high flux heat exchange tube, boiling heat transfer in the enhanced tube. Can reduce outside of tubes wall temperature and evaporating temperature's difference on the one hand, do benefit to the regulation and control of system, on the other hand can reduce heat transfer area.
Description
Technical field
The utility model relates to a kind of two-stage efficient circulation evaporation organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system, belongs to fume afterheat power field.
Background technique
Technical problem
Coal fired boiler produces heat by coal combustion, and heat, after transforming, produces steam or hot water.But not all heat can effectively transform, still have many energy and fallen by flue gas loss.The temperature of exhaust fume of coal burning boiler of power station is probably between 120 DEG C ~ 140 DEG C, and the temperature of exhaust fume of industry coal-boiler is probably between 150 DEG C ~ 204 DEG C.The feature of this part energy is that quality is not high, but discharge amount is large.If can effectively recycle fire coal boiler fume used heat, for raising boiler fired coal utilization ratio, reduce coal-fired use amount, reduce pollutant discharge amount and be of great importance.
Organic Rankine bottoming cycle (ORC) system has that efficiency is higher, structure is simple, environmental friendliness, the advantage such as can to arrange nearby, effectively can recycle low temperature exhaust heat.As described in patent (CN203626908U), utilize organic Rankine bottoming cycle effectively can reclaim the low-temperature flue gas waste heat of 40 ~ 200 DEG C, make full use of the sensible heat in the flue gas of industrial boiler discharge and latent heat generating.But due in coal-fired flue-gas containing the composition such as sulfuric acid vapor, water vapor and flying dust, this just causes utilizing in the process of conventional organic rankine cycle system Mist heat recovering and there are problems:
(1), during double flash evaporation organic Rankine bottoming cycle Mist heat recovering, by evaporating temperature and the impact of reclaiming the degree of depth, make the outer wall temperature of most of heating surface lower than acid dew point, the sulfuric acid vapor in flue gas can condense, and produces cold end corrosion to heating surface.
(2) Temperature of Working in organic rankine cycle system warm very low (can be low to moderate 20 ~ 30 DEG C), low-temperature pre-heater outer wall temperature will lower than water dew point.When there is water condensation, can cold end corrosion be aggravated, thus affect the heat-exchange performance of heating surface.
(3) evaporator type that organic rankine cycle system often uses is similar to dry evaporator, i.e. preheating, evaporation and overheated 3 links are all carry out in same heat exchanger, equipment is simple, be beneficial to adjustment liquid supply rate, but its pipe internal-filling liquid amount is low, surface liquid wetness is low, causes its surface coefficient of heat transfer relatively low.And the outer wall range of temperature of this type vaporizer is large, thus difficulty is caused to the adjustment of pipe outer wall temperature, be unfavorable for the cold end corrosion problem avoiding or alleviate heating surface.
Summary of the invention
For the problems referred to above, propose a kind of two-stage efficient circulation evaporation organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system herein; Can cause difficulty because applying the outer wall temperature of traditional dry evaporator to regulation and control heat exchanging tube, system selects recirculation type evaporator, and evaporation working medium is first preheated to saturation state in preheater, after enter iterative cycles heat absorption evaporation in vaporizer.Because the preheating of the type vaporizer and evaporation two links are separated, by the method for the outer wall temperature of segmentation regulating tube to alleviate the cold end corrosion problem of system, namely by regulating low-temperature level evaporating temperature to control low-temperature level vaporizer outer wall temperature higher than water dew point, this section adopts anticorrosive steel ND steel; By regulating high-temperature level evaporating temperature to control the outer wall temperature of high-temperature level vaporizer higher than acid dew point, this section can adopt common steel, reduces heat exchanger cost.Recirculation type evaporator circulating ratio can reach 2 ~ 5, and inner surface of pipeline can soak all the time, and surface coefficient of heat transfer comparatively dry evaporator is high.Meanwhile, the low-temperature level vaporizer of system and high-temperature level vaporizer use high-flux heat exchange, and namely high-flux heat exchange is sinter one deck porous layer at inner tube wall, the artificial increase nucleus of boiling, evaporation working medium the boiling in ducts coefficient of heat transfer comparatively light pipe can improve 2 ~ 3 times.Can realize on the one hand evaporating the less different transfer of heat between working medium and tube wall by application while recirculation type evaporator and high-flux heat exchange, be more conducive to the regulation and control of system, can heat exchange area be reduced on the other hand.Because double flash evaporation organic rankine cycle system warm Temperature of Working is very low, its outer wall temperature can lower than water dew point, thus have a large amount of water condensations, aggravate the cold end corrosion of this section of heat exchanger, for this reason, the heat-conducting plastic heat exchanging tube that this section adopts, heat-conduction plastic pipe utilizes heat filling to carry out uniform filling to macromolecule matrix material, and to improve its heat-conducting property, it occurs with soda acid to send out hardly answers, there is good corrosion resistance, effectively solve this section of cold end corrosion problem.Before needed for high-temperature level preheating, evaporation link, working medium enters high-temperature level preheater, first preheating in low-temperature level preheater, thus working medium can be avoided directly to draw (now Temperature of Working is low) from liquid container and cause high-temperature level preheater also to occur the situation of outer wall temperature lower than water dew point, high-temperature level preheater adopts anticorrosive steel ND steel.
Technological scheme: for achieving the above object, the technical solution adopted in the utility model is:
Two-stage efficient circulation evaporation organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system is provided with high-temperature level vaporizer successively in flue, high-temperature level preheater, low-temperature level vaporizer and low-temperature level preheater, the import of described low-temperature level preheater is connected with low-temperature level working medium delivery side of pump, one outlet of described low-temperature level preheater is connected with the first import of low-temperature level drum, another outlet of described low-temperature level preheater is connected with high-temperature level working medium pump, the outlet of described low-temperature level vaporizer is connected with the second import of low-temperature level drum, first outlet of described low-temperature level drum is connected with the gas supplementing opening of hot merit power-converting machinery, second outlet of described low-temperature level drum is connected with low-temperature level evaporator.
Described high-temperature level working medium delivery side of pump is connected with the import of high-temperature level preheater, the outlet of described high-temperature level preheater is connected with the first import of high-temperature level drum, the outlet of described high-temperature level vaporizer is connected with the second import of high-temperature level drum, first outlet of described high-temperature level drum is connected with the suction port of thermal technology's power-converting machinery, and the second outlet of described high-temperature level drum is connected with the import of high-temperature level vaporizer.
The outlet of described thermal technology's power-converting machinery is connected with the import of condenser, and the outlet of described condenser is connected with the import of working medium liquid container, and the outlet of described working medium liquid container is connected with the import of low-temperature level working medium pump.
Further, described high-temperature level vaporizer and low-temperature level vaporizer are recirculation type evaporator, and in its pipe, iterative cycles heat absorption evaporation is until vaporize completely for evaporation working medium for described recirculation type evaporator, and its preheating and evaporation two links are separated.
Further, described high-temperature level vaporizer and low-temperature level vaporizer use high-flux heat exchange, and described high-flux heat exchange is the inner tubal wall surface sintering one deck porous layer at heat exchanging tube, the artificial increase nucleus of boiling, enhanced boiling heat transfer.
Further, described low-temperature level preheater is the heat-conducting plastic heat exchanging tube reacted with soda acid hardly.
Further, control low-temperature level vaporizer and high-temperature level preheater outer wall temperature are respectively higher than water dew point, the outer wall temperature of high-temperature level vaporizer is higher than acid dew point, then ND steel selected by described low-temperature level vaporizer and high-temperature level preheater, and common iron selected by described high-temperature level vaporizer.
Beneficial effect: compared with the prior art, advantage is the utility model:
(1) low-temperature level is evaporated preheating and the separation of evaporation link of link by the form of circulating and evaporating.The plastic heat exchanger tube occurring with soda acid hardly to answer selected by low-temperature level preheater, effectively solves this section of cold end corrosion problem.Simultaneously by controlled medium low-temperature level evaporating temperature, realize low-temperature level evaporator section outer wall temperature higher than water dew point.
(2) high-temperature level is evaporated preheating and the separation of evaporation link of link by the form of circulating and evaporating, and by controlling high-temperature level vaporizer outer wall temperature higher than acid dew point, this section can not use anticorrosive steel, saves cost.
(3) high-flux heat exchange selected by low-temperature level vaporizer and high-temperature level vaporizer, realizes the high-efficiency evaporating heat exchange in pipe.The boiling in ducts coefficient of heat transfer can improve 2 ~ 3 times, and total heat exchange area can reduce 5 ~ 10%.In addition, use the difference greatly reducing working medium evaporating temperature and pipe outer wall temperature while circulating and evaporating and high-flux heat exchange, be beneficial to the accuracy controlling to pipe outer wall temperature.
(4) select at low-temperature level preheater outlet manifold, high-temperature level preheater can be avoided also to occur the situation of outer wall temperature lower than water dew point.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Figure comprises: low-temperature level preheater 1, low-temperature level vaporizer 2, high-temperature level preheater 3, high-temperature level vaporizer 4, high-temperature level drum 5, high-temperature level drum first import 5-A, high-temperature level drum second import 5-B, high-temperature level drum first exports 5-1, high-temperature level drum second exports 5-2, low-temperature level drum 6, low-temperature level drum first import 6-A, low-temperature level drum second import 6-B, low-temperature level drum first exports 6-1, low-temperature level drum second exports 6-2, hot merit power-converting machinery 7, generator 8, condenser 9, working medium liquid container 10, low-temperature level working medium pump 11, high-temperature level working medium pump 12.
Embodiment
Below in conjunction with accompanying drawing, the utility model is further described.
As shown in Figure 1, a kind of two-stage efficient circulation evaporation organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system, high-temperature level vaporizer 4 is provided with successively in flue, high-temperature level preheater 3, low-temperature level vaporizer 2 and low-temperature level preheater 1, the import of described low-temperature level preheater 1 is connected with the outlet of low-temperature level working medium pump 11, one outlet of described low-temperature level preheater 1 is connected with the first import 6-A of low-temperature level drum 6, another outlet of described low-temperature level preheater 1 is connected with high-temperature level working medium pump 12, second outlet 6-2 of described low-temperature level drum 6 is connected with the import of low-temperature level vaporizer 2, the outlet of described low-temperature level vaporizer 2 is connected with the second import 6-B of low-temperature level drum 6, first outlet 6-1 of described low-temperature level drum 6 is connected with the gas supplementing opening of hot merit power-converting machinery 7.
The outlet of described high-temperature level working medium pump 12 is connected with the import of high-temperature level preheater 3, the outlet of described high-temperature level preheater 3 is connected with the first import 5-A of high-temperature level drum 5, second outlet 5-2 of described high-temperature level drum 5 is connected with the import of high-temperature level vaporizer 4, the outlet of described high-temperature level vaporizer 4 is connected with the second import 5-B of high-temperature level drum 5, and the first outlet 5-1 of described high-temperature level drum 5 is connected with the suction port of thermal technology's power-converting machinery 7.
The outlet of described thermal technology's power-converting machinery 7 is connected with the import of condenser 9, and the outlet of described condenser 9 is connected with the import of working medium liquid container 10, and the outlet of described working medium liquid container 10 is connected with the import of low-temperature level working medium pump 11.
Described hot merit power-converting machinery 7 is steam turbine or decompressor.This system also comprises generator 8, and generator 8 is connected with hot merit power-converting machinery 7.
Described high-temperature level vaporizer 4 and low-temperature level vaporizer 2 for use recirculation type evaporator in the utility model, and iterative cycles heat absorption evaporation is until vaporize completely in pipe for the evaporation working medium of described recirculation type evaporator, and its preheating and evaporation two links are separated.Described high-temperature level vaporizer 4 and low-temperature level vaporizer 2 adopt high-flux heat exchange in the utility model, described high flux heat exchanger is the inner tubal wall surface sintering one deck porous layer at heat exchanger, the nucleus of boiling stable in a large number can be provided, enhanced boiling heat transfer, realizes the high-efficiency evaporating heat exchange in pipeline.Described low-temperature level preheater 1 is the plastic heat exchanger tube occurring with soda acid hardly to answer.ND steel selected by described low-temperature level vaporizer 2 and high-temperature level preheater 3, and common iron selected by described high-temperature level vaporizer 4.
The operation method of two-stage efficient circulation evaporation organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system, during system cloud gray model, fire coal boiler fume by high-temperature level vaporizer 4, high-temperature level preheater 3, low-temperature level vaporizer 2 and low-temperature level preheater 1, realizes heat exchange successively.
Simultaneously through the working medium of condensation, after low-temperature level working medium pump 11 pressurizes, enter low-temperature level preheater 1 preheating, reach capacity state.
A wherein road of the working medium of the state that reaches capacity enters into low-temperature level drum 6 from the outlet of low-temperature level preheater 1, enter low-temperature level vaporizer 2 through low-temperature level drum 6 to evaporate, vehicle repair major working medium after evaporation returns in low-temperature level drum 6 carries out gas-liquid separation, wherein, working substance steam enters hot merit power dress and changes in mechnisiam gas supplementing opening, and liquid phase working fluid enters low-temperature level vaporizer 2 circulating and evaporating again.
Another road of the working medium of the state that reaches capacity enters high-temperature level working medium pump 12 from low-temperature level preheater 1 continues pressurization, and the working medium after pressurization enters in high-temperature level preheater 3 high-temperature level drum 5 and high-temperature level vaporizer 4 process completing second time preheating and circulating and evaporating successively.
The working medium completing second time preheating and evaporation enters in high-temperature level drum 5 carries out gas-liquid separation, and wherein, working substance steam enters hot merit power-converting machinery 7 expansion work, and liquid phase working fluid is back to high-temperature level vaporizer 4 and carries out new round evaporation.
Exhaust steam after hot merit power-converting machinery 7 expansion work enters condenser 9 and is condensed into saturated liquids, flows in working medium liquid container 10, completes whole working medium circulation.
When adopting the utility model to reclaim coal-fired low-temperature flue gas waste heat, can arrange nearby, the original line arrangement of boiler and purging system etc. all can remain unchanged, only need the part flue before to wet desulphurization device after deduster to transform heat recovery heat exchanger is installed, and isothermal holding is carried out to pipeline.Simultaneously can according in actual moving process, the acid dew point of flue gas and water dew point size, regulate high and low temperature level evaporating temperature, ensure the safe operation of system.
Application example one, thermal source is the coal fired boiler low-temperature flue gas of 125 DEG C, flue gas flow 506.56m
3/ s, acid dew point 92 DEG C, water dew point 50 DEG C.Described low boiling working fluid is R123, double flash evaporation, flue gas exit temperature 78 DEG C.Result of calculation is as shown in the table:
| Conventional dry vaporizer | Recirculation evaporator | Recirculation evaporator (high flux) | |
| Flue gas inlet temperature, DEG C | 125 | 125 | 125 |
| Flue gas exit temperature, DEG C | 78 | 78 | 78 |
| Flue gas flow, m 3/s | 506.56 | 506.56 | 506.56 |
| Working fluid condenses temperature, DEG C | 32 | 32 | 32 |
| Cooling water temperature, DEG C | 20 | 20 | 20 |
| The high-temperature level folder point temperature difference, DEG C | 10 | 10 | 10 |
| The low-temperature level folder point temperature difference, DEG C | >8 | >8 | >8 |
| Turbine efficiency | 0.85 | 0.85 | 0.85 |
| Working medium pump efficiency | 0.85 | 0.85 | 0.85 |
| High-temperature level evaporating temperature, DEG C | 79 | 79 | 79 |
| Low-temperature level evaporating temperature, DEG C | 96 | 96 | 96 |
| Total acting amount, kw | 2758 | 2758 | 2758 |
| Heat exchange area, m2 | 26986 | 26374 | 25046 |
| Blower fan wasted work amount, kw | 462.90 | 453.58 | 433.17 |
| Clean acting amount, kw | 2295.10 | 2304.42 | 2324.83 |
| Clean reuse efficiency | 10.15％ | 10.19％ | 10.28％ |
Result of calculation is known, flue gas inlet/outlet temperature constant, and use the total heat exchange area in recirculation evaporator flue lower than dry evaporator by 2.26% after optimizing, fan energy consumption reduces by 2.0%, and clean acting amount and clean reuse efficiency improve 0.39%.
For using the recirculation evaporator of high flux heat exchanger, boiling heat transfer coefficient is 3 times of calculating by light pipe, the outlet mass dryness fraction of steam flow and vaporizer is constant simultaneously, comparatively light pipe recirculation evaporation ORC system, the heat exchange area of evaporator section can reduce 1328m2, total heat exchange area reduces 5.0%, and fan energy consumption reduces by 4.5%, and net electric generation and clean reuse efficiency improve 0.875%.
According to above-mentioned analysis, although comparatively dry evaporator is complicated for recirculation type evaporator system, because in its pipe, flow is large, outlet mass dryness fraction is low, and inner tube wall liquid wetness is high, and heat-exchange performance is strong, has larger advantage for large scale system.Meanwhile, preheating and evaporation two links of recirculation type evaporator are separated, and the boiling in ducts coefficient of heat transfer of evaporator section is large, and tube wall temperature is low, is beneficial to regulation and control wall temperature to alleviate cold end corrosion.
The above is only preferred implementation of the present utility model; be noted that for those skilled in the art; under the prerequisite not departing from the utility model principle; can also make some improvements and modifications, these improvements and modifications also should be considered as protection domain of the present utility model.
Claims (7)
1. two-stage efficient circulation evaporation organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system, it is characterized in that: in flue, be provided with high-temperature level vaporizer (4) successively, high-temperature level preheater (3), low-temperature level vaporizer (2) and low-temperature level preheater (1), the import of described low-temperature level preheater (1) is connected with the outlet of low-temperature level working medium pump (11), first outlet of described low-temperature level preheater (1) is connected with first import (6-A) of low-temperature level drum 6, second outlet of described low-temperature level preheater (1) is connected with high-temperature level working medium pump (12), second outlet (6-2) of described low-temperature level drum (6) is connected with the import of low-temperature level vaporizer (2), the outlet of described low-temperature level vaporizer (2) is connected with second import (6-B) of low-temperature level drum (6), first outlet (6-1) of described low-temperature level drum (6) is connected with the gas supplementing opening of hot merit power-converting machinery (7),
The outlet of described high-temperature level working medium pump (12) is connected with the import of high-temperature level preheater (3), the outlet of described high-temperature level preheater (3) is connected with first import (5-A) of high-temperature level drum (5), second outlet (5-2) of described high-temperature level drum (5) is connected with the import of high-temperature level vaporizer (4), the outlet of described high-temperature level vaporizer (4) is connected with second import (5-B) of high-temperature level drum (5), first outlet (5-1) of described high-temperature level drum (5) is connected with the suction port of thermal technology's power-converting machinery (7),
The outlet of described thermal technology's power-converting machinery (7) is connected with the import of condenser (9), the outlet of described condenser (9) is connected with the import of working medium liquid container (10), and the outlet of described working medium liquid container (10) is connected with the import of low-temperature level working medium pump (11).
2. two-stage efficient circulation evaporates organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system according to claim 1, it is characterized in that: described hot merit power-converting machinery (7) is steam turbine or decompressor, described hot merit power-converting machinery (7) is connected with generator (8).
3. two-stage efficient circulation evaporates organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system according to claim 1, it is characterized in that: described high-temperature level vaporizer (4) and low-temperature level vaporizer (2) are recirculation type evaporator, in its pipe, iterative cycles heat absorption evaporation is until vaporize completely for evaporation working medium for described recirculation type evaporator, and its preheating and evaporation two links are separated.
4. two-stage efficient circulation evaporates organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system according to claim 1, it is characterized in that: described high-temperature level vaporizer (4) and low-temperature level vaporizer (2) are high flux heat exchanger, described high-flux heat exchange is the inner tubal wall surface sintering one deck porous layer at heat exchanging tube.
5. two-stage efficient circulation evaporates organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system according to claim 1, it is characterized in that: described low-temperature level preheater (1) is the plastic heat exchanger tube reacted with soda acid hardly, realizes low-temperature level preheater (1) outer wall temperature higher than water dew point.
6. two-stage efficient circulation evaporates organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system according to claim 1, it is characterized in that: the outer wall temperature of described low-temperature level vaporizer (2) is higher than water dew point, the outer wall temperature of described high-temperature level vaporizer (4) is higher than acid dew point, then ND steel selected by described low-temperature level vaporizer (2) and high-temperature level preheater (3), and described high-temperature level vaporizer (4) selects common iron.
7. two-stage efficient circulation evaporates organic Rankine bottoming cycle coal-fired flue-gas residual neat recovering system according to claim 1, it is characterized in that: the working medium of described high-temperature level preheater (3) selects first preheating in advance in low-temperature level preheater (1), then flow to high-temperature level working medium pump (12) pressurization.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105089729A (en) * | 2015-09-06 | 2015-11-25 | 东南大学 | System and method for recycling waste heat of two-stage efficient circulation evaporation organic Rankine cycle coal-fired flue gas |
| CN110346665A (en) * | 2019-07-15 | 2019-10-18 | 上海交通大学 | A kind of width temperature range low temperature environment testing apparatus |
-
2015
- 2015-09-06 CN CN201520680042.4U patent/CN204960999U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105089729A (en) * | 2015-09-06 | 2015-11-25 | 东南大学 | System and method for recycling waste heat of two-stage efficient circulation evaporation organic Rankine cycle coal-fired flue gas |
| CN110346665A (en) * | 2019-07-15 | 2019-10-18 | 上海交通大学 | A kind of width temperature range low temperature environment testing apparatus |
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