CN100501272C - A system and method for converting medium and low temperature waste heat into steam - Google Patents
A system and method for converting medium and low temperature waste heat into steam Download PDFInfo
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- CN100501272C CN100501272C CNB2007100984994A CN200710098499A CN100501272C CN 100501272 C CN100501272 C CN 100501272C CN B2007100984994 A CNB2007100984994 A CN B2007100984994A CN 200710098499 A CN200710098499 A CN 200710098499A CN 100501272 C CN100501272 C CN 100501272C
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- 238000000034 method Methods 0.000 title claims abstract description 18
- 239000002918 waste heat Substances 0.000 title abstract description 7
- 239000006096 absorbing agent Substances 0.000 claims abstract description 71
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 14
- 230000005611 electricity Effects 0.000 claims abstract description 3
- 230000002745 absorbent Effects 0.000 claims description 50
- 239000002250 absorbent Substances 0.000 claims description 50
- 238000010521 absorption reaction Methods 0.000 claims description 21
- 238000002425 crystallisation Methods 0.000 claims description 20
- 230000008025 crystallization Effects 0.000 claims description 20
- 238000001704 evaporation Methods 0.000 claims description 13
- 230000008020 evaporation Effects 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 230000000694 effects Effects 0.000 claims description 9
- 238000005516 engineering process Methods 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000000463 material Substances 0.000 abstract description 2
- 238000011084 recovery Methods 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 48
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 16
- 229940059936 lithium bromide Drugs 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 239000003546 flue gas Substances 0.000 description 5
- 239000003643 water by type Substances 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- IOLCXVTUBQKXJR-UHFFFAOYSA-M potassium bromide Chemical compound [K+].[Br-] IOLCXVTUBQKXJR-UHFFFAOYSA-M 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- JHJLBTNAGRQEKS-UHFFFAOYSA-M sodium bromide Chemical compound [Na+].[Br-] JHJLBTNAGRQEKS-UHFFFAOYSA-M 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
-
- 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
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/62—Absorption based systems
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- Sorption Type Refrigeration Machines (AREA)
Abstract
一种中低温余热转化为蒸汽的系统及方法，属于能源技术、热能工程以及材料工程等相互交叉的技术领域。由蒸发器、吸收器和发生器组成热泵开路循环系统，并在吸收器和发生器之间设置冷却晶析器和固液分离器。将发生器蒸汽引至外部加于利用并冷凝，实际上将冷凝器置于外部。用300-1300℃的中高温热源作为热泵循环系统发生器的热源，而用90-300℃的低温余热作为蒸发器的热源，同时从吸收器和发生器得到蒸汽。其优点在于，热回收效率高，每一份中温余热或低谷电与一份低温余热可产2份中低压蒸汽；流程简单，设备造价低。
The invention discloses a system and method for converting mid-low temperature waste heat into steam, which belongs to the intersecting technical fields of energy technology, thermal energy engineering, and material engineering. The heat pump open circuit system is composed of evaporator, absorber and generator, and a cooling crystallizer and a solid-liquid separator are arranged between the absorber and the generator. The generator steam is taken externally for utilization and condensed, effectively placing the condenser externally. The medium and high temperature heat source of 300-1300°C is used as the heat source of the heat pump cycle system generator, and the low-temperature waste heat of 90-300°C is used as the heat source of the evaporator, and steam is obtained from the absorber and generator at the same time. The advantage is that the heat recovery efficiency is high, and each part of medium-temperature waste heat or low-peak electricity and one part of low-temperature waste heat can produce 2 parts of medium-low pressure steam; the process is simple and the equipment cost is low.
Description
Technical field
The invention belongs to cross one another technical fields such as new energy technology, Thermal Power Engineering, Chemical Engineering and material engineering, particularly a kind of middle-low temperature heat is converted into the system and method for steam.
Background technology
Along with the new stage of pursuing recycling economy has been come in China's economic development, further saving energy and reduce the cost has become the important topic that high energy consumption industries such as iron and steel, chemical industry, building materials must be faced.
Passed through enterprise's effort for many years, higher waste heat, the waste gas of grade has obtained effective utilization mostly in the factory, thereby the remaining space of taping the latent power mainly is the low-grade energy that grade is low, quantity big, the reuse difficulty is big, and promptly temperature range is at 90-500 ℃ middle-low temperature heat.Typical middle-low temperature heat has the entrained sensible heat of the steam boiler outlet flue gas of about 300 ℃ of temperature and steel billet, slag etc.
Usually, middle-low temperature heat, especially the method for utilizing of low temperature exhaust heat is this waste heat to be converted into 60-90 ℃ hot water, with this thermal source as worker domestic hot-water or heating cooling.For large and medium-sized enterprise, because worker living area and producing region are far apart usually, this utilizes method obviously is inapplicable.In addition, also there are some low temperature exhaust heat to be converted into the research report (Zhao Xiaowei of steam by adopting the second class absorption heat pump technology, Wang Shukun. second class absorption heat pump and the application prospect in smelter thereof. Shandong metallurgy, 2004,26 (6): 37-39.)., the second traditional class absorption heat pump circulatory system exists three shortcomings, and promptly institute's producing steam pressure is low, the thermal efficiency is low (steam of 1 part of calorific value need consume the low temperature exhaust heat of calorific value more than two parts) and the low-temperature heat source that need be used to cool off.
Summary of the invention
The object of the present invention is to provide a kind of middle-low temperature heat to be converted into the system and method for steam, solved three shortcomings that the above-mentioned second class absorption heat pump system exists.
System of the present invention adopts evaporimeter 1, absorber 2, generator 3 and liquid-feeding pump 9 to form the absorption heat pump open-circuit system.Connect with steam passage 7 between evaporimeter 1 and the absorber 2, connect with first, second absorbent solution pipeline 18,19 between absorber 2, generator 3 and the liquid-feeding pump 9; First heat exchanger 4 places evaporimeter 1, the second heat exchanger 5 to place absorber 2, the three heat exchangers 6 to place generator 3.With the thermal source of 250-1300 ℃ of thermal source as generator 3, add the absorbent solution of heater 3 by the 3rd heat exchanger 6 that places generator 3, make it evaporation and produce steam 21; Absorb the steam of flash-pot 1 and produce absorption heat in absorber 2 absorbent solutions,, make it evaporation and produce first steam 20 by placing second heat exchanger, 5 heating condensate waters of absorber 2; With the thermal source of 90-500 ℃ of middle-low temperature heat as evaporimeter 1, the condensed water of first heat exchanger, 4 heating fumigators 1 by placing evaporimeter 1 makes it evaporation and produces steam, by steam passage 7 this steam is introduced absorber 2.
The outside that the present invention causes this circulation with generator second steam 21 is used and makes it to obtain condensation, and the form with condensed water turns back to evaporimeter 1 and absorber 2 afterwards.This is actually the outside that condenser is placed this circulatory system.Therefore, this circulation with respect to the second traditional class heat pump cycle adopted closed (closed circuit) circulation, be the circulation of a kind of heat pump open circuit.As shown in Figure 1, the absorbent solution of absorber 2 is sent into generator 3, utilize the generator 3 and the pressure differential of absorber 2 that the absorbent solution of generator 3 is introduced absorber 2 then, thereby constitute the circulation of absorbent solution by liquid-feeding pump 9.
The present invention also can be provided with steam jet pump 8 in said system, with steam pipework 16 high-pressure side of steam jet pump 8 inlet 14 is connected with the steam (vapor) outlet 12 of absorber 2, with steam pipework 17 low-pressure side of steam jet pump 8 inlet 15 is connected with the steam (vapor) outlet 13 of generator 3, first steam 20 and second steam, 21 interflow of the different parameters that the effect by steam jet pump 8 will be respectively obtains from absorber 2 and generator 3 are the 3rd steam 22 of same parameter, thereby the pressure of generator second steam 21 is got a promotion.
In order further to improve the pressure of absorber first steam 20 and generator second steam 21, second system of the present invention as shown in Figure 2, cooling partial crystallization device 10 and solid-liquid separator 11 are set between absorber 2 and generator 3, make the concentration reduction of the absorbent solution of introducing generator by the effect of cooling partial crystallization device 10 and solid-liquid separator 11.More particularly,, make solute supersaturation partial crystallization, after Separation of Solid and Liquid, parting liquid is sent into generator by absorber outlet absorbent solution is cooled off.According to the characteristic of absorbent solution VLE, the pressure of the low more saturated vapor of concentration of absorbent solution is just high more under the certain condition of temperature.Because the part solute in the absorbent solution is at cooling partial crystallization device 10 partial crystallizations, the solute crystallization obtains separating at solid-liquid separator 10, thereby the concentration of absorbent solution has obtained reduction in the generator 3, and the pressure of generator second steam 21 also just increases.Simultaneously, will send into absorber 2, and make the solute crystallization in absorber 2, obtain dissolving in solute crystallization and generator exports absorbent solution that solid-liquid separator obtains.Characteristic according to the absorbent solution VLE, at the absorption steam pressure is that the high more absorption temperature of concentration of absorbent solution under the certain condition of evaporator pressure is just high more, because the concentration of absorbent solution is improved in the dissolving absorber 2 of solute crystallization, absorber 2 operating temperatures just increase, and the absorption heat of emitting with absorption process is that the pressure of absorber first steam 20 of thermal source also just increases.Second system of the present invention is characterised in that, by cooling partial crystallization device 10 and solid-liquid separator 11 are set, have reached the purpose that can set and optimize absorber 2 and generator 3 absorbent solution working concentrations respectively between absorber 2 and generator 3.That is to say, second system of the present invention can realize a kind of for the very useful process conditions of absorption heat pump circulation, be when absorber is worked under high absorbent solution concentration conditions, generator is worked under than the low absorbent solution concentration conditions of absorber absorbent solution concentration, and this to be the circulation of traditional absorption heat pump be difficult to accomplish.
The present invention is also without particular limitation to the kind of employing absorbent solution, can adopt LiBr solution, also can adopt LiBr, NaBr, KBr, MgBr
2Deng mixed solution.
The present invention can utilize the thermal source of low ebb electricity as generator 3.
Method of the present invention is to adopt evaporimeter, absorber and generator to form the absorption heat pump open-circuit system to transform; With the thermal source of 250-1300 ℃ of thermal source as generator 3, add the absorbent solution of heater 3 by the 3rd heat exchanger 6 that places generator 3, make it evaporation and produce second steam 21; Absorb the steam of flash-pot 1 and produce absorption heat in absorber 2 absorbent solutions,, make it evaporation and produce first steam 20 by placing second heat exchanger, 5 heating condensate waters of absorber 2; With the thermal source of 90-500 ℃ of middle-low temperature heat as evaporimeter 1, the condensed water of first heat exchanger, 4 heating fumigators 1 by placing evaporimeter 1 makes it evaporation and produces steam, by steam passage 7 this steam is introduced absorber 2.
The present invention also can be provided with steam jet pump 8 in system shown in Figure 1, with steam pipework 16 high-pressure side of steam jet pump 8 inlet 14 is connected with the steam (vapor) outlet 12 of absorber 2, with steam pipework 17 low-pressure side of steam jet pump 8 inlet 15 is connected with the steam (vapor) outlet 13 of generator 3, it is the 3rd steam 22 that first steam 20 and generator second steam 21 are collaborated in the effect by steam jet pump 8.
The present invention can also transform with system shown in Figure 2, cooling partial crystallization device 10 and solid-liquid separator 11 promptly are set between absorber 2 and generator 3, make the concentration reduction of the absorbent solution of introducing generator by the effect of cooling partial crystallization device 10 and solid-liquid separator 11.
According to principle of the present invention, the generator thermal source of each part heat also can be converted into steam with the middle-low temperature heat of a heat simultaneously except self can produce the steam of a heat.And then, the two parts of steam that produce can be the steam of same parameter in the effect interflow by steam jet pump, this steam can be directly used in steam turbine generating, also can be used as the heating thermal source of existing steam turbine condensed water, by reducing or saving the purpose that the turbine rate of air sucked in required reaches increases generated energy.And then institute of the present invention producing steam also can be incorporated the steam pipe system of factory into by the effect of second steam jet pump.In addition, institute of the present invention producing steam also can be used as the required water vapour of vapor reforming hydrogen production process of natural gas, coke-stove gas etc.
Another feature of the present invention is, by adjusting the capacity of absorption liquid, absorber and generator both can move synchronously continuously, can distinguish independent periodic running again, and these characteristics are very useful for the utilization of the middle-low temperature heat of steelmaking process intermittent discharge.
Effect of the present invention
The first, heat recovery efficiency height, the generator thermal source of each part calorific value and the middle-low temperature heat of a calorific value can produce the steam of 2 parts of calorific values;
The second, flow process is simple, and equipment manufacturing cost is low.This is owing to need not sub-cooled thermal source and system thereof, and device all moves under the pressure conditions of higher, need not to be provided with the noncondensable gas treatment system;
Three, absorber and generator both can move synchronously continuously, also can distinguish independent periodic running, very were suitable for the characteristics of steel manufacture process.
Four, can organicly incorporate the existing energy of enterprise and use system such as steam turbine generating set or steam pipe system etc., thereby reach the purpose of maximum energy-saving consumption reduction and economic benefit.
Description of drawings
Fig. 1 is the flow chart of first absorption heat pump open-circuit system of the present invention; Fig. 2 is the flow chart of second absorption heat pump open-circuit system of the present invention.Wherein, evaporimeter 1, absorber 2, generator 3, evaporimeter first heat exchanger 4, absorber second heat exchanger 5, generator the 3rd heat exchanger 6, steam passage 7, steam jet pump 8, liquid-feeding pump 9, cooling partial crystallization device 10, solid-liquid separator 11, absorber steam (vapor) outlet 12, steam of generator outlet 13, steam jet pump high-pressure side inlet 14, steam jet pump low-pressure side inlet 15, steam pipework 16, steam pipework 17, the first absorbent solution pipeline 18, the second absorbent solution pipeline 19, absorber exports first steam 20, generator exports second steam 21, steam jet pump exports the 3rd steam 22.
The specific embodiment
Embodiment 1
As shown in Figure 1, be the thermal source of generator 3 with about 500 ℃ flue gas, add the absorbent solution of heater 3 by the heat exchanger 6 that places generator 3, make it evaporation and produce about 200 ℃, the steam 21 of 0.2MPa, the concentration of absorbent solution raises in the synchronizer 3; The absorbent solution of generator 3 is introduced into absorber 2.Absorb the steam of flash-pot 1 and produce absorption heat in absorber 2 absorbent solutions,, make it evaporation and produce about 150 ℃ by heat exchanger 5 heating condensate waters that place absorber 2, the steam 20 of 0.5MPa, the concentration of absorbent solution reduces in the absorber 2 simultaneously.With about 250 ℃ low-temperature flue gas is the thermal source of evaporimeter 1, and the condensed water of first heat exchanger, 4 heating fumigators 1 by placing evaporimeter 1 makes it to evaporate and produce the about 90 ℃ steam of temperature, and by steam passage 7 this steam is introduced absorber 2.First steam 20 and second steam 21 that absorber 2 and generator 3 are produced are introduced steam jet pumps 8, obtain about 160 ℃, the 3rd steam 22 of 0.3MPa in the outlet of steam jet pump 8.The 3rd steam 22 can be incorporated steam pipe system into by another steam jet pump, also can introduce steam turbine system and do directly or indirectly generating.The absorbent solution that present embodiment adopted is lithium-bromide solution, and the lithium bromide mass percent of absorber 2 absorbent solutions is about 65%; The lithium bromide mass percent of generator 3 absorbent solutions is about 67%;
First system of the present invention has the simple advantage of flow process, but has the lower deficiency of institute's producing steam pressure.This is because absorber absorbent solution working concentration and generator absorbent solution working concentration are subjected to the result of mutual restriction.In order further to improve institute's producing steam pressure, second system of the present invention as shown in Figure 2, its flow process characteristics are to be provided with cooling partial crystallization device 10 and solid-liquid separator 11 between absorber 2 and generator 3.Present embodiment is the same with the foregoing description one, is the thermal source of evaporimeter 1 with about 250 ℃ low-temperature flue gas, and is the thermal source of generator 3 with about 500 ℃ flue gas.Produce about 90 ℃ steam at evaporimeter 1, this steam enters absorber 2 by steam passage 7; Absorb the steam of flash-pot 1 and produce absorption heat in absorber 2 absorbent solutions, by placing second heat exchanger, 5 heating condensate waters of absorber 2, make it evaporation and produce about 170 ℃, first steam 20 of 0.8MPa, the concentration of absorbent solution reduces in the absorber 2 simultaneously.The absorbent solution of drawing from absorber 2 is admitted to cooling partial crystallization device 10, cools off partial crystallization with about 8 ℃ cooling water as refrigerant, and after solid-liquid separator 11 carried out Separation of Solid and Liquid, the parting liquid that obtains was sent into generator 3 by liquid-feeding pump 11.Absorbent solution evaporation in the generator 3 produces about 200 ℃, second steam 21 of 0.3MPa, and the absorbent solution concentration in the synchronizer 3 raises; The solute crystallization that absorbent solution of being drawn by generator 3 and solid-liquid separator 11 obtain is admitted to absorber 2.And then, first steam 20 and second steam 21 are introduced steam jet pump 8, obtain about 180 ℃, the 3rd steam 22 of 0.5MPa in steam jet pump 8 outlets.The absorbent solution that present embodiment adopted is lithium-bromide solution, and the lithium bromide mass percent of absorber 2 absorbent solutions is about 70%; The lithium bromide mass percent of generator 3 absorbent solutions is about 60%.
Claims (7)
1. a middle-low temperature heat is converted into the system of steam, it is characterized in that: adopt evaporimeter (1), absorber (2), generator (3) and liquid-feeding pump (9) composition absorption heat pump open-circuit system; Connect with steam passage (7) between evaporimeter (1) and the absorber (2), connect with the first absorbent solution pipeline (18) between the inlet of the outlet of absorber (2), liquid-feeding pump (9) and generator (3), connect with the second absorbent solution pipeline (19) between the inlet of the outlet of generator (3) and absorber (2); First heat exchanger (4) places evaporimeter (1), and second heat exchanger (5) places absorber (2), and the 3rd heat exchanger (6) places generator (3); With the thermal source of 250-1300 ℃ of thermal source as generator (3), with the thermal source of 90-500 ℃ of middle-low temperature heat of temperature, obtain first steam (20) at absorber (2) respectively simultaneously as evaporimeter (1), obtain second steam (21) at generator (3).
2, according to the described system of claim 1, it is characterized in that: steam jet pump (8) is set, be connected with the steam (vapor) outlet (12) of absorber (2) with the high-pressure side inlet (14) of steam pipework (16), be connected with the steam (vapor) outlet (13) of generator (3) with the low-pressure side inlet (15) of steam pipework (17) with steam jet pump (8) with steam jet pump (8).
3, according to the described system of claim 1, it is characterized in that: cooling partial crystallization device (10) and solid-liquid separator (11) are set between the inlet of the outlet of absorber (2) and generator (3).
4, according to claim 1,2 or 3 described systems, it is characterized in that: utilize the thermal source of low ebb electricity as generator (3).
5. one kind is adopted the described system of claim 1 that middle-low temperature heat is converted into the method for steam, it is characterized in that: form the absorption heat pump open-circuit system with evaporimeter, absorber and generator and transform; With the thermal source of 250-1300 ℃ of thermal source as generator (3), add the absorbent solution of heater (3) by the 3rd heat exchanger (6) that places generator (3), make it evaporation and produce second steam (21); Absorbent solution in absorber (2) absorbs the 3rd steam of flash-pot (1) and produces and absorbs heat, by placing second heat exchanger (5) heating condensate water of absorber (2), makes it evaporation and produces first steam (20); With the thermal source of 90-500 ℃ of middle-low temperature heat as evaporimeter (1), the condensed water of first heat exchanger (4) heating fumigators (1) by placing evaporimeter (1), make it evaporation and produce steam, the steam that evaporimeter produces is introduced absorber (2) by steam passage (7).
6. in accordance with the method for claim 5, it is characterized in that: steam jet pump (8) is set, be connected with the steam (vapor) outlet (12) of absorber (2) with the high-pressure side inlet (14) of steam pipework (16) steam jet pump (8), be connected with the steam (vapor) outlet (13) of generator (3) with the low-pressure side inlet (15) of steam pipework (17) steam jet pump (8), first steam (20) and second steam (21) interflow of the different parameters that the effect by steam jet pump (8) will be respectively obtains from absorber (2) and generator (3) are the 3rd steam (22) of same parameter, thereby the pressure of generator second steam (21) is got a promotion.
7. in accordance with the method for claim 5, it is characterized in that: cooling partial crystallization device (10) and solid-liquid separator (11) are set between absorber (2) and generator (3), make the concentration reduction of the absorbent solution of introducing generator by the effect of cooling partial crystallization device (10) and solid-liquid separator (11).
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| CNB2007100984994A CN100501272C (en) | 2007-04-19 | 2007-04-19 | A system and method for converting medium and low temperature waste heat into steam |
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| CNB2007100984994A CN100501272C (en) | 2007-04-19 | 2007-04-19 | A system and method for converting medium and low temperature waste heat into steam |
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| CNA2009101308023A Division CN101566404A (en) | 2007-04-19 | 2007-04-19 | System and method for transforming low temperature residual heat into steam |
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| CN100501272C true CN100501272C (en) | 2009-06-17 |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1056089A (en) * | 1991-05-25 | 1991-11-13 | 北京化工学院 | A Method of Using Heat Pump to Recover Waste Heat in Transformation Process |
| CN1128856A (en) * | 1994-09-27 | 1996-08-14 | 巴布考克及威尔考克斯公司 | Ammonia absorption circulation used for combined circulation power apparatus |
| CN2310291Y (en) * | 1997-09-10 | 1999-03-10 | 西安交通大学 | High-efficiency composite circulation refrigerating device |
-
2007
- 2007-04-19 CN CNB2007100984994A patent/CN100501272C/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1056089A (en) * | 1991-05-25 | 1991-11-13 | 北京化工学院 | A Method of Using Heat Pump to Recover Waste Heat in Transformation Process |
| CN1128856A (en) * | 1994-09-27 | 1996-08-14 | 巴布考克及威尔考克斯公司 | Ammonia absorption circulation used for combined circulation power apparatus |
| US5555738A (en) * | 1994-09-27 | 1996-09-17 | The Babcock & Wilcox Company | Ammonia absorption refrigeration cycle for combined cycle power plant |
| CN2310291Y (en) * | 1997-09-10 | 1999-03-10 | 西安交通大学 | High-efficiency composite circulation refrigerating device |
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| Publication number | Publication date |
|---|---|
| CN101033897A (en) | 2007-09-12 |
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