CN102312687A - Solution cooling absorption type ammonia water motive power circulation device - Google Patents
Solution cooling absorption type ammonia water motive power circulation device Download PDFInfo
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- CN102312687A CN102312687A CN201110273602A CN201110273602A CN102312687A CN 102312687 A CN102312687 A CN 102312687A CN 201110273602 A CN201110273602 A CN 201110273602A CN 201110273602 A CN201110273602 A CN 201110273602A CN 102312687 A CN102312687 A CN 102312687A
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Abstract
The invention discloses a solution cooling absorption type ammonia water motive power circulation device, which consists of an evaporator 1, a turbine machine set 3, a regenerator 4, a low-pressure absorbing device 5, a low-pressure ammonia pump 6, a gas-liquid separator 7, a pre-heater 8, a high-pressure absorbing device 9, a high-pressure ammonia pump 10, a throttle valve 11 and a connecting pipeline, wherein the low-pressure absorbing device and the high-pressure absorbing device are respectively divided into a solution cooling absorbing section and a cooling water absorbing section, and the solution cooling absorbing section is arranged above the cooling water absorbing section. The solution cooling absorption type ammonia water motive power circulation device has the advantages that the absorbing device outlet solution is used for cooling the front section of the absorbing process, the cooling water quantity can be reduced, the heat discharge and the heat transfer loss on the environment can be reduced, the heat transfer area is favorably reduced, and the circulation heat efficiency is favorably improved. The solution cooling absorption type ammonia water motive power circulation device is provided with the three-flow pre-heater for preheating work solution before entering the evaporator, the dilute solution and rich ammonia gas entering the absorber can be cooled, the absorption driving force can be enhanced, and in addition, the smoke gas low-temperature corrosion resistance of the device is favorably improved.
Description
Technical field
The present invention relates to a kind of power circulating device, especially a kind of solution cooling and absorbing formula ammoniacal liquor power circulating device that is used for middle and low temperature waste heat power generation.
Background technique
Many industrial processs all can produce a large amount of sensible heat type waste heats, and the thermal source of geothermal power, solar energy is also in the majority with the sensible heat type.Because the characteristics of its exothermic process are that bigger temperature variation is arranged, with it and do not match under the pinch-point temperature difference restriction, there is bigger heat transfer temperature difference irreversible loss in the decalescence process in the water vapor Rankine cycle; Many freon class working medium have the detrimental effect of pair ozonosphere, and price is expensive.The boiling point of tradition working-medium water is higher, and saturation pressure at normal temperatures is a vacuum state, and specific volume is very big, thereby is not adapted at using in the middle and low temperature waste heat power generation circulation.In the cogeneration temperature range, the working pressure of pure ammonia is higher.And adopt both mixture ammonia spirits, can pressure be adjusted to OK range.If but adopt ammonia water mixture simply as cycle fluid; Though the heat absorption evaporation process of working medium can realize the temperature variation with the exothermic process of sensible heat thermal source coupling; But the condensation exothermic process of working medium also can have very big temperature variation; Will improve average exothermic temperature like this, reduce thermal efficiency of cycle.Ka Linna (Kalina) circulation adopts absorption process to substitute condensation process; Can make the also comparison match of temperature variation of the diabatic process of working medium and low-temperature heat source; The present invention further improves its backheat flow process on Ka Linna circuit basis, thereby improves thermal efficiency of cycle.
Summary of the invention
The present invention provides a kind of can make full use of the ammoniacal liquor power cycle flow process that has bigger endothermic temperature excursion and less exothermic temperature excursion when sensible heat type middle-low temperature heat generates electricity and have the higher-energy conversion efficiency.
The present invention adopts following technological scheme:
A kind of solution cooling and absorbing formula ammoniacal liquor power circulating device is made up of vaporizer, turbine modulating valve, turbine unit, regenerator, low-pressure absorber, low pressure ammonia pump, gas-liquid separator, preheater, high pressure absorber, high-pressure ammonia pump, dilute solution throttle valve and connecting line; Vaporizer is provided with thermal source import, thermal source outlet, working solution import and working solution outlet; Regenerator is provided with working solution import and working solution outlet, basic solution inlet port and basic taphole; Gas-liquid separator is provided with basic solution inlet port, the outlet of rich ammonia gas and dilute solution outlet; Low-pressure absorber is divided into solution cooling down absorption segment and cooling water absorber portion; The internal channel of solution cooling down absorption segment is provided with basic solution inlet port and basic taphole; The internal channel of cooling water absorber portion is provided with cooling water intake and coolant outlet, and solution cooling down absorption segment is arranged in the top of cooling water absorber portion; Above solution cooling down absorption segment, also be provided with dilute solution drencher and working solution import, the entry end of dilute solution drencher is the low pressure dilute solution inlet; Bottom liquid capsule at low-pressure absorber is provided with basic taphole; High pressure absorber is divided into high-pressure solution cooling down absorption segment and high-pressure cooling water cooling down absorption segment; The internal channel of high-pressure solution cooling down absorption segment is provided with working solution import and working solution outlet, and the internal channel of high-pressure cooling water absorber portion is provided with cooling water intake and coolant outlet; The high-pressure solution cooling down absorption segment is arranged in the top of high-pressure cooling water cooling down absorption segment; Above the high-pressure solution cooling down absorption segment, also be provided with high pressure dilute solution drencher and rich ammonia import, the entry end of high pressure dilute solution drencher is the dilute solution inlet of high pressure absorber; Bottom liquid capsule at high pressure absorber is provided with the working solution outlet; Preheater is three plume heat exchangers, is provided with the outlet of dilute solution inlet and dilute solution, rich ammonia import and rich ammonia outlet, working solution import and working solution outlet.
The annexation of each parts is: the working solution outlet of vaporizer is connected with the import of turbine modulating valve; The outlet of turbine modulating valve is connected with the import of turbine unit; The outlet of turbine unit is connected with the working solution import of regenerator; The working solution outlet of regenerator is connected with the working solution import of low-pressure absorber; The basic taphole of low-pressure absorber is connected with the import of low pressure ammonia pump; The outlet of low pressure ammonia pump is connected with the basic solution inlet port of low-pressure absorber solution cooling down absorption segment; The basic taphole of low-pressure absorber solution cooling down absorption segment is connected with the basic solution inlet port of regenerator; The basic taphole of regenerator is connected with the import of gas-liquid separator; The rich ammonia outlet of gas-liquid separator is connected with the rich ammonia import of preheater; The dilute solution outlet of gas-liquid separator is connected with the dilute solution inlet of preheater; The rich ammonia outlet of preheater is connected with the rich ammonia import of high pressure absorber; The dilute solution export pipeline of preheater is divided into 2 the tunnel; One the tunnel is connected with the dilute solution inlet of high pressure absorber; Another road is connected with the import of dilute solution throttle valve, and the outlet of dilute solution throttle valve is connected with the dilute solution inlet of low-pressure absorber; The working solution outlet of high pressure absorber is connected with the import of high-pressure ammonia pump, and the high pressure ammonia delivery side of pump is connected with the working solution import of high pressure absorber solution cooling down absorption segment; The working solution outlet of high pressure absorber solution cooling down absorption segment is connected with the working solution import of preheater, and the working solution outlet of preheater is connected with the working solution import of vaporizer.
Compared with prior art, the present invention has following advantage:
1. improved energy conversion efficiency.The present invention compares with Ka Linna (Kalina) circulation, and one of main difference is in 2 adsorbers, the solution cooling down absorption segment heat transfer surface is arranged all.In the ammoniacal liquor power cycle, nearly 20 ~ 40 ℃ of the temperature drop of absorption process is with the leading portion of adsorber outlet solution cooling and absorbing process; Can reduce cooling water inflow; Reduced the temperature difference of absorption process simultaneously, the heat extraction of environment has been decreased with fiery the using of conducting heat, improved thermal efficiency of cycle thereby reduce.Solution cooling and absorbing technology is a kind of energy-conservation means of ten minutes economy; Not only be embodied in cycle efficiency is improved; And be to have obtained two parts of heat-transfer effects with a heat exchange area from the heat transfer angle, make the desorption process of absorption process and solution obtain part simultaneously and realize.In addition, because high temperature heat source and working medium is in the diabatic process of vaporizer, the alternating temperature phase-change characteristic of working medium and the variation of the sensible heat exothermic temperature of thermal source have good coupling; In the diabatic process of working medium and low-temperature heat source, pass through simultaneously to substitute condensation process with absorption process; Make the temperature variation of working medium also be complementary with the temperature variation of low-temperature heat source (cooling water or cold wind), add the solution heat recovery process also be near etc. the heat transfer of the temperature difference, so; The circuit irreversible loss is less, and efficient is higher.
2. two of the main difference compared of the present invention and Ka Linna (Kalina) circulation be to be provided with three plume preheaters and come the working solution before preheating gets into vaporizer; Can obtain cooling with dilute solution that gets into high pressure absorber and rich ammonia so that get into the dilute solution of low-pressure absorber simultaneously; Increase the driving force that absorbs, helped improving the ability of the anti-flue gas low-temperature corrosion of vaporizer (boiler) simultaneously.
3. water vapour tension is on the low side and higher ammonia mix the ammoniacal liquor mixed working fluid that forms and can maximize favourable factors and minimize unfavourable ones; Formulated component through control ammoniacal liquor can make the system pressure level proper; Not only turbine ingress pressure is very not high, and the turbine outlet port can remain and be higher than atmospheric malleation, and the range of working pressure of ammoniacal liquor mixed working fluid is suitable; Enthalpy drop and water vapour medium quite, can directly adopt existing back pressure type industrial steam turbine; Owing to compare with organic working medium, the heat-transfer character of ammoniacal liquor mixed working fluid is good, helps reducing heat transfer area simultaneously, reduces initial cost.
4. because the compatibility of ammonia and aluminium; Adopting aluminum plate-fin heat exchanger will be to raise the efficiency; Reduce cost and the wisdom of compactness is selected, except the vaporizer of HTHP, all the other heat exchangers all can consider to adopt aluminum plate-fin heat exchanger; Especially adsorber can also adopt air-cooled aluminum plate-fin heat exchanger scheme, and this will make the waste heat electric power station system greatly simplify.
5. ammonia and water all are natural refrigerants, and the source is abundant, and price is more cheap.
Description of drawings
Fig. 1 is the schematic flow sheet of the embodiment of the invention 1.
Embodiment
Embodiment 1Referring to Fig. 1; A kind of ammonia water absorbing power circulating device that is used for the utilization of low-temperature heat source power recovery is made up of vaporizer 1, turbine modulating valve 2, turbine unit 3, regenerator 4, low-pressure absorber 5, low pressure ammonia pump 6, gas-liquid separator 7, preheater 8, high pressure absorber 9, high-pressure ammonia pump 10, dilute solution throttle valve 11 and connecting line; Vaporizer 1 is provided with heat source fluid import 1-1, heat source fluid outlet 1-2, working solution import 1-3 and working solution outlet 1-4; Regenerator 4 is provided with working solution import 4-1 and working solution outlet 4-2, basic solution inlet port 4-3 and basic taphole 4-4, and gas-liquid separator 7 is provided with basic solution inlet port 7-1, rich ammonia gas outlet 7-2 and dilute solution outlet 7-3; It is characterized in that low-pressure absorber 5 is divided into solution cooling down absorption segment 51 and cooling water absorber portion 52; The internal channel of solution cooling down absorption segment 51 is provided with basic solution inlet port 51-1 and basic taphole 51-2; The internal channel of cooling water absorber portion 52 is provided with cooling water intake 52-1 and coolant outlet 52-2; Solution cooling down absorption segment 51 is arranged in the top of cooling water absorber portion 52; Above solution cooling down absorption segment 51, also be provided with dilute solution drencher 5-3 and gaseous state working solution import 5-4; The entry end of dilute solution drencher 5-3 is low-pressure absorber dilute solution inlet 5-5, is provided with basic taphole 5-6 at the bottom liquid capsule of low-pressure absorber 5, and high pressure absorber 9 is divided into high-pressure solution cooling down absorption segment 91 and high-pressure cooling water cooling down absorption segment 92; The internal channel of high-pressure solution cooling down absorption segment 91 is provided with working solution import 91-1 and working solution outlet 91-2; The internal channel of high-pressure cooling water absorber portion 92 is provided with cooling water intake 92-1 and coolant outlet 92-2, and high-pressure solution cooling down absorption segment 91 is arranged in the top of high-pressure cooling water cooling down absorption segment 92, above high-pressure solution cooling down absorption segment 91, also is provided with high pressure dilute solution drencher 9-3 and rich ammonia import 9-4; The entry end of high pressure dilute solution drencher 9-3 is the dilute solution inlet 9-5 of high pressure absorber 9, is provided with working solution outlet 9-6 at the bottom liquid capsule of high pressure absorber 9; Preheater 8 is three plume heat exchangers, is provided with dilute solution inlet 8-1, dilute solution outlet 8-2, rich ammonia import 8-3, rich ammonia outlet 8-4, working solution import 8-5 and working solution outlet 8-6;
The annexation of each parts is: the working solution outlet 1-4 of vaporizer 1 is connected with the import 2-1 of turbine modulating valve 2; The outlet 2-2 of turbine modulating valve is connected with the import 3-1 of turbine unit 3; The outlet 3-2 of turbine unit is connected with the working solution import 4-1 of regenerator 4; The working solution outlet 4-2 of regenerator is connected with the working solution import 5-4 of low-pressure absorber 5; The basic taphole 5-6 of low-pressure absorber is connected with the import 6-1 of low pressure ammonia pump 6, and the outlet 6-2 of low pressure ammonia pump 6 is connected with the basic solution inlet port 51-1 of low-pressure absorber 5 solution cooling down absorption segments 51, and the basic taphole 51-2 of hypotonic solution cooling down absorption segment 51 is connected with the basic solution inlet port 4-3 of regenerator; The basic taphole 4-4 of regenerator is connected with the import 7-1 of gas-liquid separator 7; The rich ammonia outlet 7-2 of gas-liquid separator 7 is connected with the rich ammonia import 8-3 of preheater 8, and the dilute solution outlet 7-3 of gas-liquid separator 7 is connected with the dilute solution inlet 8-1 of preheater 8, and the rich ammonia outlet 8-4 of preheater is connected with the rich ammonia import 9-4 of high pressure absorber 9; The dilute solution outlet 8-2 pipeline of preheater 8 is divided into 2 the tunnel; One the tunnel is connected with the dilute solution inlet 9-5 of high pressure absorber 9, and another road is connected with the import 11-1 of dilute solution throttle valve 11, and the outlet 11-2 of dilute solution throttle valve 11 is connected with the dilute solution inlet 5-5 of low-pressure absorber; The working solution outlet 9-6 of high pressure absorber 9 is connected with the import 10-1 of high-pressure ammonia pump 10, and the outlet 10-2 of high-pressure ammonia pump 10 is connected with the working solution import 91-1 of high pressure absorber 9 solution cooling down absorption segments 91; The working solution outlet 91-2 of high pressure absorber 9 solution cooling down absorption segments 91 is connected with the working solution import 8-5 of preheater 8, and the working solution outlet 8-6 of preheater is connected with the working solution import 1-3 of vaporizer 1.
The workflow of this ammoniacal liquor power cycle is following:
The liquid of ammonia water absorbing power cycle working solution gets in the vaporizer and accomplishes endothermic process, is evaporated to the gaseous state working solution, in turbine, realizes the expansion working process, accomplishes the hot merit conversion; The turbine exhaust is lowered the temperature in regenerator earlier, gets in the low-pressure absorber to be absorbed by the dilute solution of spray in the low-pressure absorber tube bank again, and the latent heat of vaporization of release is taken away by the basic solution and the cooling water of low-pressure absorber opposite side; Dilute solution becomes basic solution after having absorbed the gaseous state working solution, and flow out the bottom that collects in low-pressure absorber, and basic solution is after the low pressure ammonia pump boosts; Successively realization solution backheat intensification desorption process in the solution cooling down absorption segment of low-pressure absorber and regenerator becomes gas-liquid two-phase fluid, in separator, carries out gas-liquid separation; Gas phase is rich ammonia gas, and liquid phase is a dilute solution, and rich ammonia gas and dilute solution get into preheater simultaneously and cool; Rich ammonia gas cooling back gets into high pressure absorber; Dilute solution then is divided into two-way, and most of dilute solution is in throttle valve flows back to low-pressure absorber, and spray is in the adsorber tube bank; The fraction dilute solution becomes working solution after absorbing rich ammonia gas in spraying tube flows into high pressure absorber.The latent heat of vaporization is taken away by working solution and cooling water.Collect in the working solution that the bottom of high pressure absorber flows out and boost, after successively heat absorption heats up in the solution cooling down absorption segment of high pressure absorber and preheater again, flow back to completion evaporation process in the vaporizer through high-pressure ammonia pump; The outlet gaseous state working solution of vaporizer gets into expansion working in the turbine again, so circulation.
Claims (1)
1. a solution cooling and absorbing formula ammoniacal liquor power circulating device is made up of vaporizer (1), turbine modulating valve (2), turbine unit (3), regenerator (4), low-pressure absorber (5), low pressure ammonia pump (6), gas-liquid separator (7), preheater (8), high pressure absorber (9), high-pressure ammonia pump (10), dilute solution throttle valve (11) and connecting line; Vaporizer (1) is provided with heat source fluid import (1-1), heat source fluid outlet (1-2), working solution import (1-3) and working solution outlet (1-4); Regenerator (4) is provided with working solution import (4-1) and working solution outlet (4-2), basic solution inlet port (4-3) and basic taphole (4-4), and gas-liquid separator (7) is provided with basic solution inlet port (7-1), rich ammonia gas outlet (7-2) and dilute solution outlet (7-3); It is characterized in that low-pressure absorber (5) is divided into solution cooling down absorption segment (51) and cooling water absorber portion (52); The internal channel of solution cooling down absorption segment (51) is provided with basic solution inlet port (51-1) and basic taphole (51-2); The internal channel of cooling water absorber portion (52) is provided with cooling water intake (52-1) and coolant outlet (52-2); Solution cooling down absorption segment (51) is arranged in the top of cooling water absorber portion (52); Also be provided with dilute solution drencher (5-3) and gaseous state working solution import (5-4) in the top of solution cooling down absorption segment (51); The entry end of dilute solution drencher (5-3) is low-pressure absorber dilute solution inlet (5-5); Bottom liquid capsule at low-pressure absorber (5) is provided with basic taphole (5-6); High pressure absorber (9) is divided into high-pressure solution cooling down absorption segment (91) and high-pressure cooling water cooling down absorption segment (92), and the internal channel of high-pressure solution cooling down absorption segment (91) is provided with working solution import (91-1) and working solution outlet (91-2), and the internal channel of high-pressure cooling water absorber portion (92) is provided with cooling water intake (92-1) and coolant outlet (92-2); High-pressure solution cooling down absorption segment (91) is arranged in the top of high-pressure cooling water cooling down absorption segment (92); Also be provided with high pressure dilute solution drencher (9-3) and rich ammonia import (9-4) in the top of high-pressure solution cooling down absorption segment (91), the entry end of high pressure dilute solution drencher (9-3) is the dilute solution inlet (9-5) of high pressure absorber (9), is provided with working solution outlet (9-6) at the bottom liquid capsule of high pressure absorber (9); Preheater (8) is three plume heat exchangers, is provided with dilute solution inlet (8-1), dilute solution outlet (8-2), rich ammonia import (8-3), rich ammonia outlet (8-4), working solution import (8-5) and working solution outlet (8-6);
The annexation of each parts is: the working solution outlet (1-4) of vaporizer (1) is connected with the import (2-1) of turbine modulating valve (2); The outlet of turbine modulating valve (2-2) is connected with the import (3-1) of turbine unit (3); The outlet of turbine unit (3-2) is connected with the working solution import (4-1) of regenerator (4); The working solution outlet (4-2) of regenerator is connected with the working solution import (5-4) of low-pressure absorber (5); The basic taphole (5-6) of low-pressure absorber is connected with the import (6-1) of low pressure ammonia pump (6); The outlet (6-2) of low pressure ammonia pump (6) is connected with the basic solution inlet port (51-1) of low-pressure absorber (5) solution cooling down absorption segment (51); The basic taphole (51-2) of hypotonic solution cooling down absorption segment (51) is connected with the basic solution inlet port (4-3) of regenerator, and the basic taphole (4-4) of regenerator is connected with the import (7-1) of gas-liquid separator (7), and the rich ammonia outlet (7-2) of gas-liquid separator (7) is connected with the rich ammonia import (8-3) of preheater (8); The dilute solution outlet (7-3) of gas-liquid separator (7) is connected with the dilute solution inlet (8-1) of preheater (8); The rich ammonia outlet (8-4) of preheater is connected with the rich ammonia import (9-4) of high pressure absorber (9), and the dilute solution of preheater (8) outlet (8-2) pipeline is divided into 2 the tunnel, the one tunnel and is connected with the dilute solution inlet (9-5) of high pressure absorber (9); Another road is connected with the import (11-1) of dilute solution throttle valve (11), and the outlet (11-2) of dilute solution throttle valve (11) is connected with the dilute solution inlet (5-5) of low-pressure absorber; The working solution outlet (9-6) of high pressure absorber (9) is connected with the import (10-1) of high-pressure ammonia pump (10), and the outlet (10-2) of high-pressure ammonia pump (10) is connected with the working solution import (91-1) of high pressure absorber (9) solution cooling down absorption segment (91); The working solution outlet (91-2) of high pressure absorber (9) solution cooling down absorption segment (91) is connected with the working solution import (8-5) of preheater (8), and the working solution outlet (8-6) of preheater is connected with the working solution import (1-3) of vaporizer (1).
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Cited By (9)
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| CN102661181A (en) * | 2012-04-25 | 2012-09-12 | 北京亿玮坤节能科技有限公司 | Novel power generating working medium |
| CN103161535A (en) * | 2013-03-06 | 2013-06-19 | 中冶南方工程技术有限公司 | Smoke waste heat power generation system of heating furnace |
| CN103776192A (en) * | 2014-02-24 | 2014-05-07 | 梁兆福 | Low-temperature waste heat power generation device |
| CN104929708A (en) * | 2015-06-24 | 2015-09-23 | 张高佐 | Low-temperature heat source thermoelectricity conversion system and method by means of mixed component working media |
| CN105134321A (en) * | 2015-07-10 | 2015-12-09 | 东南大学 | Dual-pressure evaporation ammonium hydroxide power circulation power generation device |
| CN107830657A (en) * | 2017-09-14 | 2018-03-23 | 中国科学院理化技术研究所 | Temperature-changing cooling absorber and absorption type circulating system |
| CN108426388A (en) * | 2017-02-13 | 2018-08-21 | 山东大学 | Absorption power and spray type refrigerating combined cycle system and its working method |
| CN110374704A (en) * | 2019-06-06 | 2019-10-25 | 东南大学 | Low grade heat energy driving electricity generation system and working method based on reversible chemical reaction |
| CN112413922A (en) * | 2020-11-18 | 2021-02-26 | 山东大学 | Power-cooling combined supply system and method for fully utilizing middle-low grade industrial waste heat |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102661181A (en) * | 2012-04-25 | 2012-09-12 | 北京亿玮坤节能科技有限公司 | Novel power generating working medium |
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| CN108426388A (en) * | 2017-02-13 | 2018-08-21 | 山东大学 | Absorption power and spray type refrigerating combined cycle system and its working method |
| CN108426388B (en) * | 2017-02-13 | 2019-12-24 | 山东大学 | Absorption type power and jet type refrigeration composite circulation system and working method thereof |
| CN107830657A (en) * | 2017-09-14 | 2018-03-23 | 中国科学院理化技术研究所 | Temperature-changing cooling absorber and absorption type circulating system |
| CN110374704A (en) * | 2019-06-06 | 2019-10-25 | 东南大学 | Low grade heat energy driving electricity generation system and working method based on reversible chemical reaction |
| CN110374704B (en) * | 2019-06-06 | 2022-04-12 | 东南大学 | Low-grade heat energy driving power generation system based on reversible chemical reaction and working method |
| CN112413922A (en) * | 2020-11-18 | 2021-02-26 | 山东大学 | Power-cooling combined supply system and method for fully utilizing middle-low grade industrial waste heat |
| CN112413922B (en) * | 2020-11-18 | 2022-06-21 | 山东大学 | Power-cooling combined supply system and method for fully utilizing middle-low grade industrial waste heat |
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Application publication date: 20120111 |