CN103225961A - Sintering flue gas waste heat power generation system and method - Google Patents
Sintering flue gas waste heat power generation system and method Download PDFInfo
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- CN103225961A CN103225961A CN201310142348XA CN201310142348A CN103225961A CN 103225961 A CN103225961 A CN 103225961A CN 201310142348X A CN201310142348X A CN 201310142348XA CN 201310142348 A CN201310142348 A CN 201310142348A CN 103225961 A CN103225961 A CN 103225961A
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Abstract
The invention relates to a sintering flue gas waste heat power generation system and method. The sintering flue gas waste heat power generation system mainly comprises an ammonia water mixing working medium power circulatory system connected with a fume exhaust pipeline of a sintering system; an ammonia water circulatory system, a fume circulating passage and a cooling water circulating passage are arranged in the ammonia water mixing working medium power circulatory system; the ammonia water circulatory system and the fume circulating passage are arranged in parallel inside a heat exchanger; the ammonia water circulatory system and the cooling water circulating passage are arranged in parallel inside a condenser; the entrance point of the fume circulating passage is respectively communicated with a medium and low temperature fume pipeline and a high temperature fume pipeline, and the outlet end of the fume circulating passage is communicated with a fuel discharge pipeline, and the fuel discharge pipeline is communicated with a diffusion chimney; a cooling water inlet pipeline and a cooling water returning pipeline are both arranged on the cooling water circulating passage and both are communicated with an external cooling tower; and the overheat steam output end of the ammonia water circulatory system is led to a power generator. The sintering flue gas waste heat power generation system has a simple structure, and can efficiently recover sintering flue gas waste heat; and the heat exchanging efficiency is high, and discharged fuel is prevented from dew point corrosion.
Description
Technical field
The present invention relates to sinter fume waste heat recovery field, be specifically related to a kind of system and method that adopts ammoniacal liquor mixed working fluid power cycle to realize the sinter fume exhaust heat recovery power generation.
Background technology
Sintering is an important step in the process for producing steel and iron, and it is with mixing according to a certain ratio such as Iron Ore Powder, coal dust and lime, blast furnace dust, mill scale, slag, and the sintering deposit that sufficient intensity and granularity are arranged that forms through sintering is as the grog of ironmaking.Utilize sintered clinker ironmaking for improve the capacity factor of a blast furnace, reduce coke ratio, to improve blast furnace permeability all significant to guarantee operation of blast furnace.China's sintering deposit output ranks first in the world, and sintering circuit is to be only second to smelt iron the second largest power consumption operation of operation, and wherein the heat taken away of sinter fume accounts for the 16-24% of sintering circuit energy consumption, and it recycles for steel plant energy-saving and cost-reducing significant.The sinter fume flow is big, and wherein the high temperature section temperature is at 300-380 ℃, and middle low-temperature zone temperature is about 180-240 ℃, because sinter fume waste heat grade is lower, employing is that the Rankine cycle system generating efficiency of working medium is lower with water.It is the power circulation system of working medium with ammoniacal liquor that the present invention adopts novel, improves sinter fume waste heat recovery level.
Summary of the invention
The technical problem to be solved in the present invention is the above-mentioned defective that overcomes prior art, and a kind of sinter fume afterheat generating system and method are provided, and can reclaim the sinter fume waste heat expeditiously.
For solving the problems of the technologies described above, the technical solution used in the present invention is:
The sinter fume afterheat generating system is characterized in that: mainly comprise the ammoniacal liquor mixed working fluid power circulation system that links to each other with sintering system smoke discharge tube road; The ammoniacal liquor circulatory system, flue gas recirculation passage and cooling water circulation canal are set in the ammoniacal liquor mixed working fluid power circulation system; The ammoniacal liquor circulatory system and flue gas recirculation passage countercurrent flow in heat exchanger; The ammoniacal liquor circulatory system and cooling water circulation canal countercurrent flow in condenser; Low-temperature flue gas pipeline and high temperature flue gas pipeline during the entrance point of flue gas recirculation passage is communicated with respectively, the port of export are communicated with the fume emission pipeline, the fume emission pipeline with diffuse chimney and be communicated with; Cooling water inlet pipeline and CWR road are set respectively on the cooling water circulation canal, and cooling water inlet pipeline and CWR road are communicated with the external refrigeration tower respectively; The clutch end of the ammoniacal liquor circulatory system is communicated with decompressor, and decompressor links to each other with generator.
By technique scheme, the ammoniacal liquor circulatory system mainly comprises evaporimeter, superheater, decompressor, regenerator, flash vessel, low-pressure condenser, low-lift pump, high pressure condenser, high-pressure pump; High temperature flue gas pipeline is through converging with middle low-temperature flue gas pipeline behind the superheater and being communicated with the fume emission pipeline through behind the evaporimeter; Flue gas recirculation passage and high pressure aqua ammonia circulation canal countercurrent flow in evaporimeter and the superheater; The entrance point of high pressure aqua ammonia circulation canal and high-pressure work solution pipeline connection, the port of export is communicated with the superheated steam pipeline; The superheated steam pipeline is communicated with the expander inlet end, and decompressor expands to do work and drives generator for electricity generation; The exhaust steam of decompressor outlet is provided with the exhaust steam pipeline, the exhaust steam pipeline by regenerator and with low pressure base soln pipeline connection; Low pressure base soln pipeline is communicated with the import of low-lift pump by low-pressure condenser; The port of export of low-lift pump is the basic solution pipeline of high pressure; The basic solution pipeline of high pressure is divided into two-way, and the regenerator of leading up to is communicated with the entrance point of flash vessel, and another road is converged with the rich ammonia steam pipeline of the flash vessel port of export and is communicated with the entrance point of high-pressure pump through behind the high pressure condenser; The port of export of high-pressure pump and high-pressure work solution pipeline connection; The port of export of flash vessel also is provided with the liquor ammoniae dilutus pipeline, and liquor ammoniae dilutus pipeline and low pressure base soln pipeline converge before low-pressure condenser, on the liquor ammoniae dilutus pipeline choke valve are set; The cooling water circulation canal is through low-pressure condenser and high pressure condenser.
By technique scheme, the shared cooling water circulation canal of low-pressure condenser and high pressure condenser, cooling water circulation canal in each condenser respectively with low pressure base soln pipeline and operating on low voltage solution pipeline countercurrent flow; And one group of cooling water inlet pipeline and CWR road only are set on the cooling water circulation canal, and cooling water inlet pipeline and CWR road are communicated with the external refrigeration tower respectively.
The method that adopts above-mentioned sinter fume afterheat generating system to generate electricity is characterized in that:
Sintering system produces high-temperature flue gas and middle low-temperature flue gas respectively according to sintering process branch high temperature section and middle low-temperature zone, and the high temperature sintering flue-gas temperature directly enters superheater from high temperature flue gas pipeline at 300-380 ℃; 180-240 ℃ of low temperature sintering flue-gas temperature mixed the back by middle low-temperature flue gas pipeline and fed evaporimeter with high temperature sintering flue gas by superheater;
In evaporimeter, sinter fume makes it to undergo phase transition generation steam with the heat transferred ammonia spirit, and steam is heated to superheat state in superheater, promotes the decompressor acting, and decompressor drives generator and externally generates electricity; With heat transferred high pressure base soln, the high pressure base soln that absorbs heat is separated into dense ammonia steam and liquor ammoniae dilutus in flash vessel at regenerator in the acting exhaust steam; Dense ammonia steam is exported from the rich ammonia steam pipeline; Through the choke valve decompression, the outlet exhaust steam with regenerator afterwards mixes formation low pressure base soln to liquor ammoniae dilutus after the liquor ammoniae dilutus pipeline is discharged; The low pressure base soln is successively through becoming the high pressure base soln behind low-pressure condenser and the low-lift pump, a high pressure base soln part enters regenerator, another part becomes operating on low voltage solution with dense ammonia vapor mixing in the rich ammonia steam pipeline, become high-pressure work solution behind operating on low voltage solution process high pressure condenser and the high-pressure pump, high-pressure work solution is transported to evaporimeter by high-pressure work solution pipeline, finishes a circulation.
By technique scheme, ammonia-water mixture is in different section concentration differences, ammonia concn in high-pressure work solution pipeline, operating on low voltage solution pipeline, superheated steam pipeline and the exhaust steam pipeline is the 70-85% mass concentration, ammonia concn 40-50% mass concentration in the basic solution pipeline of high pressure, the low pressure base soln pipeline, ammonia concentration is the 90-95% mass concentration in the solution concentration 25-35% mass concentration in the liquor ammoniae dilutus pipeline, rich ammonia steam pipeline.
By technique scheme, low-pressure condenser and high pressure condenser are with identical cooling water source, and inlet water temperature is a normal temperature, and the outlet water temperature is controlled at below 50 ℃, recycles after cooling off by cooling tower.
By technique scheme, sinter fume enters by the fume emission pipeline and diffuses chimney after the heat exchange; Sinter fume at evaporator outlet temperature more than 150 ℃.
With respect to prior art, the present invention has designed the simple ammoniacal liquor mixed working fluid of structure power circulation system, utilizes ammoniacal liquor mixed working fluid power cycle to realize the sinter fume exhaust heat recovery power generation, can reclaim the sinter fume waste heat expeditiously; Simultaneously, because ammonia-water mixture is recycling, the economy and the feature of environmental protection of ammoniacal liquor mixed working fluid power circulation system all are guaranteed, and be last, because strict control delivery temperature, heat exchange efficiency is high and can not make and discharge flue gas generation dew point corrosion; Because ammonia-water mixture concentration obtains strict control, can guarantee the utilization rate maximization of ammonia-water mixture simultaneously.
Description of drawings
Fig. 1 is sinter fume afterheat generating system structure of the present invention and process schematic representation.
Fig. 2 is an ammoniacal liquor mixed working fluid power circulation system schematic diagram of the present invention.
Reference numeral is as follows among Fig. 1 and 2: the 1-evaporimeter; The 2-superheater; The 3-decompressor; The 4-generator; The 5-regenerator; The 6-flash vessel; The 7-choke valve; The 8-low-pressure condenser; The 9-low-lift pump; The 10-high pressure condenser; The 11-high-pressure pump; The 12-high temperature flue gas pipeline; Low-temperature flue gas pipeline among the 13-; 14-fume emission pipeline; 15-high-pressure work solution pipeline; 16-operating on low voltage solution pipeline; 17-cooling water inlet pipeline; 18-CWR road; The basic solution pipeline of 19-high pressure; 20-low pressure base soln pipeline; 21-exhaust steam pipeline; 22-superheated steam pipeline; 23-rich ammonia steam pipeline; 24-liquor ammoniae dilutus pipeline; The 25-sintering system; 26-ammonia-water mixture power circulation system; The 27-cooling tower; 28-diffuses chimney; 29-sintering feed and fuel mix material; The 30-sintering deposit; Low-temperature zone combustion air among the 31-; 32-high temperature section combustion air.
The specific embodiment
The invention will be further described below in conjunction with drawings and Examples, but do not limit the present invention.
As illustrated in fig. 1 and 2, the sinter fume afterheat generating system is the electricity generation system by being the power cycle recovery waste heat of working medium with ammoniacal liquor.
The sintering feed of input and fuel mix material 29 are through being heated as sintering deposit 30 outputs in the sintering system 25; High temperature section combustion air 32 enters sintering system 25 combustion-supporting burning backs and discharges, and enters ammoniacal liquor mixed working fluid power circulation system 26 through high temperature flue gas pipeline 12; Discharge middle low-temperature zone combustion air 31 combustion-supporting burnings backs, and low-temperature flue gas pipeline 13 enters ammoniacal liquor mixed working fluid power circulation system 26 in the warp; The ammoniacal liquor circulatory system, flue gas recirculation passage and cooling water circulation canal are set in the ammoniacal liquor mixed working fluid power circulation system 26; Low-temperature flue gas pipeline 13 and high temperature flue gas pipeline 12 during the entrance point of flue gas recirculation passage is communicated with respectively, the port of export are communicated with fume emission pipeline 14, fume emission pipeline 14 with diffuse chimney 28 and be communicated with; Cooling water inlet pipeline 17 and CWR road 18 are set respectively on the cooling water circulation canal, and cooling water inlet pipeline 17 and CWR road 18 are communicated with external refrigeration tower 27 respectively; Ammoniacal liquor circulatory system output work drives generator 4 and externally generates electricity.
The distribution of the ammoniacal liquor circulatory system in ammoniacal liquor mixed working fluid power circulation system 26 be as shown in Figure 2: mainly comprise evaporimeter 1, superheater 2, decompressor 3, regenerator 5, flash vessel 6, low-pressure condenser 8, low-lift pump 9, high pressure condenser 10, high-pressure pump 11; High temperature flue gas pipeline 12 converges with middle low-temperature flue gas pipeline 13 through superheater 2 backs and is communicated with fume emission pipeline 14 through evaporimeter 1 back; Flue gas recirculation passage and high pressure aqua ammonia circulation canal countercurrent flow in evaporimeter 1 and the superheater 2;
The entrance point of high pressure aqua ammonia circulation canal is communicated with high-pressure work solution pipeline 15, and the port of export is communicated with superheated steam pipeline 22; Superheated steam pipeline 22 is communicated with decompressor 3 entrance points, and decompressor 3 links to each other with generator 4, and the exhaust steam outlet of decompressor 4 is communicated with exhaust steam pipeline 21, and exhaust steam pipeline 21 is communicated with by regenerator 5 and with low pressure base soln pipeline 20; Low pressure base soln pipeline 20 is communicated with the import of low-lift pump 9 by low-pressure condenser 8; The port of export of low-lift pump 9 is the basic solution pipeline 19 of high pressure; The basic solution pipeline 19 of high pressure is divided into two-way, and the regenerator 5 of leading up to is communicated with the entrance point of flash vessel 6, and another road is converged with the rich ammonia steam pipeline 23 of flash vessel 6 ports of export and is communicated with the entrance point of high-pressure pump 11 through high pressure condenser 10 backs; The port of export of high-pressure pump 11 is communicated with high-pressure work solution pipeline 15; The port of export of flash vessel 6 also is provided with liquor ammoniae dilutus pipeline 24, and liquor ammoniae dilutus pipeline 24 converged with low pressure base soln pipeline 20 before low pressure base soln pipeline 20 enters low-pressure condenser 8, and choke valve 7 is set on the liquor ammoniae dilutus pipeline 24.
The cooling water circulation canal is in low-pressure condenser 8 and high pressure condenser 10, and respectively with low pressure base soln pipeline 20 and operating on low voltage solution pipeline 16 countercurrent flows, and cooling water inlet pipeline 17 and CWR road 18 are set respectively on the cooling water circulation canal, and cooling water inlet pipeline 17 and CWR road 18 are communicated with external refrigeration tower 27 respectively.
Whole power circulation system is connected by pipeline, ammonia-water mixture is in different section concentration differences, ammonia concn in working solution pipeline (high-pressure work solution pipeline 15, operating on low voltage solution pipeline 16, superheated steam pipeline 22) and the exhaust steam pipeline 21 is the 70-85%(mass concentration, as follows), the interior ammonia concn 40-50% of base soln pipeline (the basic solution pipeline 19 of high pressure, low pressure base soln pipeline 20), solution concentration 25-35% in the liquor ammoniae dilutus pipeline 24, ammonia concentration is 90-95% in the rich ammonia steam pipeline 23.
Low-pressure condenser 8 and the identical cooling water source of high pressure condenser 10 usefulness, inlet water temperature is a normal temperature, the outlet water temperature is controlled at below 50 ℃, by recycling after cooling tower 27 coolings;
Sinter fume sulfur content height after the heat exchange, must the control sinter fume at the exit gas temperature of evaporimeter 1 more than 150 ℃, to avoid dew point corrosion, the heat exchange sinter fume enters by fume emission pipeline 14 and diffuses chimney 28.
Claims (8)
1. the sinter fume afterheat generating system is characterized in that: mainly comprise the ammoniacal liquor mixed working fluid power circulation system that links to each other with sintering system smoke discharge tube road; The ammoniacal liquor circulatory system, flue gas recirculation passage and cooling water circulation canal are set in the ammoniacal liquor mixed working fluid power circulation system; The ammoniacal liquor circulatory system and flue gas recirculation passage countercurrent flow in heat exchanger; The ammoniacal liquor circulatory system and cooling water circulation canal countercurrent flow in condenser; Low-temperature flue gas pipeline and high temperature flue gas pipeline during the entrance point of flue gas recirculation passage is communicated with respectively, the port of export are communicated with the fume emission pipeline, the fume emission pipeline with diffuse chimney and be communicated with; Cooling water inlet pipeline and CWR road are set respectively on the cooling water circulation canal, and cooling water inlet pipeline and CWR road are communicated with the external refrigeration tower respectively; The clutch end of the ammoniacal liquor circulatory system is communicated with decompressor, and decompressor links to each other with generator.
2. system according to claim 1 is characterized in that: the ammoniacal liquor circulatory system mainly comprises evaporimeter, superheater, decompressor, regenerator, flash vessel, low-pressure condenser, low-lift pump, high pressure condenser, high-pressure pump; High temperature flue gas pipeline is through converging with middle low-temperature flue gas pipeline behind the superheater and being communicated with the fume emission pipeline through behind the evaporimeter; In evaporimeter and the superheater, flue gas recirculation passage and high pressure aqua ammonia circulation canal countercurrent flow; The entrance point of high pressure aqua ammonia circulation canal and high-pressure work solution pipeline connection, the port of export is communicated with the superheated steam pipeline; The superheated steam pipeline is communicated with the expander inlet end; The exhaust steam of decompressor outlet is provided with the exhaust steam pipeline, the exhaust steam pipeline by regenerator and with low pressure base soln pipeline connection; Low pressure base soln pipeline is communicated with the import of low-lift pump by low-pressure condenser; The port of export of low-lift pump is the basic solution pipeline of high pressure; The basic solution pipeline of high pressure is divided into two-way, and the regenerator of leading up to is communicated with the entrance point of flash vessel, and another road is converged with the rich ammonia steam pipeline of the flash vessel port of export and is communicated with the entrance point of high-pressure pump through behind the high pressure condenser; The port of export of high-pressure pump and high-pressure work solution pipeline connection; The port of export of flash vessel also is provided with the liquor ammoniae dilutus pipeline, and liquor ammoniae dilutus pipeline and low pressure base soln pipeline converge before low-pressure condenser, on the liquor ammoniae dilutus pipeline choke valve are set; The cooling water circulation canal is through low-pressure condenser and high pressure condenser.
3. system according to claim 2 is characterized in that: the shared cooling water circulation canal of low-pressure condenser and high pressure condenser, cooling water circulation canal in each condenser respectively with low pressure base soln pipeline and operating on low voltage solution pipeline countercurrent flow; And one group of cooling water inlet pipeline and CWR road only are set on the cooling water circulation canal, and cooling water inlet pipeline and CWR road are communicated with the external refrigeration tower respectively.
4. the method that adopts above-mentioned sinter fume afterheat generating system to generate electricity is characterized in that:
Sintering system produces high-temperature flue gas and middle low-temperature flue gas respectively according to sintering process branch high temperature section and middle low-temperature zone, and the high temperature sintering flue-gas temperature directly enters superheater from high temperature flue gas pipeline at 300-380 ℃; 180-240 ℃ of low temperature sintering flue-gas temperature mixed the back by middle low-temperature flue gas pipeline and fed evaporimeter with high temperature sintering flue gas by superheater;
In evaporimeter, sinter fume makes it to undergo phase transition generation steam with the heat transferred ammonia spirit, and steam is heated to superheat state in superheater, promotes the decompressor acting, and decompressor drives generator and externally generates electricity; With heat transferred high pressure base soln, the high pressure base soln that absorbs heat is separated into dense ammonia steam and liquor ammoniae dilutus in flash vessel at regenerator in the acting exhaust steam; Dense ammonia steam is exported from the rich ammonia steam pipeline; Through the choke valve decompression, the outlet exhaust steam with regenerator afterwards mixes formation low pressure base soln to liquor ammoniae dilutus after the liquor ammoniae dilutus pipeline is discharged; The low pressure base soln is successively through becoming the high pressure base soln behind low-pressure condenser and the low-lift pump, a high pressure base soln part enters regenerator, another part becomes operating on low voltage solution with dense ammonia vapor mixing in the rich ammonia steam pipeline, become high-pressure work solution behind operating on low voltage solution process high pressure condenser and the high-pressure pump, high-pressure work solution is transported to evaporimeter by high-pressure work solution pipeline, finishes a circulation.
5. method according to claim 4, it is characterized in that: ammonia-water mixture is in different section concentration differences, ammonia concn in high-pressure work solution pipeline, operating on low voltage solution pipeline, superheated steam pipeline and the exhaust steam pipeline is the 70-85% mass concentration, ammonia concn 40-50% mass concentration in the basic solution pipeline of high pressure, the low pressure base soln pipeline, ammonia concentration is the 90-95% mass concentration in the solution concentration 25-35% mass concentration in the liquor ammoniae dilutus pipeline, rich ammonia steam pipeline.
6. according to claim 4 or 5 described methods, it is characterized in that: low-pressure condenser and high pressure condenser are with identical cooling water source, and inlet water temperature is a normal temperature, and the outlet water temperature is controlled at below 50 ℃, by recycling after the cooling tower cooling.
7. according to claim 4 or 5 described methods, it is characterized in that: sinter fume enters by the fume emission pipeline and diffuses chimney after the heat exchange; Sinter fume at evaporator outlet temperature more than 150 ℃.
8. method according to claim 6 is characterized in that: sinter fume enters by the fume emission pipeline and diffuses chimney after the heat exchange; Sinter fume at evaporator outlet temperature more than 150 ℃.
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| CN104074565A (en) * | 2014-01-16 | 2014-10-01 | 中冶南方工程技术有限公司 | Working medium concentration adjustable ammonia power cycle system |
| CN105587427A (en) * | 2016-03-18 | 2016-05-18 | 中国科学院工程热物理研究所 | Engine waste heat recovery power generation system based on organic Rankine cycle |
| CN108443941A (en) * | 2018-03-26 | 2018-08-24 | 东南大学 | A kind of distributed energy island system |
| CN111852599A (en) * | 2019-04-30 | 2020-10-30 | 中国船舶重工集团公司第七一一研究所 | Ship waste heat recovery power generation system |
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