CN101709339A - System and method for recovering slag residual heat - Google Patents
System and method for recovering slag residual heat Download PDFInfo
- Publication number
- CN101709339A CN101709339A CN200910254338A CN200910254338A CN101709339A CN 101709339 A CN101709339 A CN 101709339A CN 200910254338 A CN200910254338 A CN 200910254338A CN 200910254338 A CN200910254338 A CN 200910254338A CN 101709339 A CN101709339 A CN 101709339A
- Authority
- CN
- China
- Prior art keywords
- heat
- heat exchanger
- slag
- temperature
- steam
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
Landscapes
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Abstract
The invention discloses a system and a method for recovering slag residual heat. Wherein the residual heat recovering system comprises a steam heat exchange system and a multi-level heat energy storage system; the steam heat exchange system is used for multi-level recovering high-temperature mixed gas generated during slag treatment and comprises more than two levels of steam heat exchange devices; and the multi-level heat energy storage system comprises more than two levels of heat storage devices and is used storing the recovered heat energy by levels according to different temperature. The invention overcomes the defects of low heat energy quality, utilization value and recovery rate in traditional slag residua heat recovering and storing method.
Description
Technical field
The present invention relates to the heat recovery field of ferrous metallurgy process slag treatment; Refer in particular to a kind of afterheat of slags that produces in the slag treatment that relates to and reclaim afterheat of slags recovery system and the recovery method that stores.
Background technology
Ferrous metallurgy process---blast furnace ironmaking, operations such as converter steelmaking, annual 30～40% a large amount of smelted furnace cinders of ratio output with output of steel, the whole world is with the quantity output in more than one hundred million tons of every year, its heat energy of taking away is amounted to more than 2,000 ten thousand tons of standard coals, amount to 15,000,000,000 yuan of Renminbi, this part heat energy can not utilize and directly be discharged, except the waste that causes huge energy, the toxic and harmful that the energy of this waste is discharged and cause the gas of Greenhouse effect to aggravate the burden that human environment is administered undoubtedly, if the heat energy that this part slag produces effectively can be stored, turn waste into wealth, get final product save energy, can also make a contribution for human environmental protection cause.
The tradition heat reclaiming system, adopt single thermal energy storage device usually, with high-quality energy recovery be in or low-quality thermal energy storage.Can cause terminal a large amount of low-quality heat energy not reclaim during quality heat energy in save as and diffuse waste; Solve end when saving as low-quality heat energy and diffused waste, but increased the difficulty and the cost of low-quality heat energy utilization.Therefore, the heat energy poor quality utility value of traditional heat reclaiming system recovery is low, utilising efficiency is low, waste is big.
In view of the deficiency that traditional waste heat recovery storage method exists, make every effort to find a kind of recovery waste heat quality better, novel method that waste heat recovery efficient is high, the inventor has proposed the present invention according to the research experience of being engaged in aspects such as slag treatment, waste heat recovery for many years.
Summary of the invention
The technical problem to be solved in the present invention is: provide a kind of afterheat of slags recovery system and recovery method, to overcome the deficiency that the heat energy quality is low, utility value is not high and the rate of recovery is low that traditional waste heat recovery, storage method exist.
Technical solution of the present invention is:
A kind of afterheat of slags recovery system, described residual neat recovering system comprises: the high-temperature gas mixture body that produces in the slag treatment process is carried out steam heat-exchanging system that classification reclaims and multistage thermal energy storage system, described steam heat-exchanging system comprises the steam heat exchanger that two-stage is above, described multistage thermal energy storage system comprises the heat-storing device that two-stage is above, carries out classification with the heat energy that will reclaim according to differing temps and stores.
A kind of method for recovering waste heat from scoria, wherein, this method comprises:
A. reclaim the heat energy in the slag treatment being carried out the classification heat exchange by the multi-stage heat exchanger device;
B. the heat energy classification of the different qualities that heat exchange is reclaimed is stored in the multistage heat-storing device.
Characteristics of the present invention and advantage are: the present invention carries out high-quality recovery, storage and high-quality utilization according in the afterheat of slags removal process to high-quality heat energy; To the principle that low-quality heat energy carries out low-quality recovery, storage and low-quality utilization, the high temperature heat that slag cooling heat transferring process is reclaimed reclaims, is stored into the high-temperature heat accumulation bag, and the high-quality heat energy that utilizes the high-temperature heat accumulation bag to store is directly used in generating; To further be recovered as low-quality heat energy through the tail gas after the high-quality energy recovery, be used for low-quality utilization, used up water or it is promoted to utilizing after high-quality again by heat pump as a supplement generates electricity, under the prerequisite that does not reduce high-quality heat energy utilization, reclaim and utilize low-quality tail heat, play the purpose that improves comprehensive heat energy recycle.
Description of drawings
Fig. 1 is the structure and the treatment scheme synoptic diagram of a specific embodiment of afterheat of slags recovery system of the present invention and method.
Fig. 2 is the structure and the treatment scheme synoptic diagram of another concrete Application Example of afterheat of slags recovery system of the present invention.
The drawing reference numeral explanation:
100, slag handling system 300, residual neat recovering system 500, afterheat generating system
101, liquid slag 102, fecal iron separator 103, slag guide pipe
104, slag buffer memory storehouse (vapor recovery warehouse) 105, high-pressure aerial fog nozzle
106, shredder assembly 107, plate-type heat exchanger 108, auger heat exchange handling machinery
109, fluid-bed heat exchanger 110, drag-out slag car 111, comb hydrophone
112, tank 113, dirt ash wash-down water pipeline 114, dirt ash flooding nozzle
201, first step interchanger 202, second stage interchanger 203, third stage interchanger
204, level pressure blower fan 205, recirculation blower 206, tail gas heat exchanger
207, strainer 301, high pressure drum 302, middle pressure thermophore
303, low pressure bag 304, relief valve 305, relief valve
306, deoxygenator 307,311,312, liquid pump 308～310, ejector
501, steam turbine 502, generator 503, steam condenser
511, ammonia turbine 512, producer 513, resorber
514, heat exchanger 515,515 ', relief valve 516, ammonia superheater
517, throttling valve 518, pump 520, vapor superheater
521, relief valve
Embodiment
Following conjunction with figs. and specific embodiment are described in further detail the specific embodiment of the present invention.
The present invention proposes a kind of afterheat of slags recovery system, described residual neat recovering system comprises: the high-temperature gas mixture body that produces in the slag treatment process is carried out steam heat-exchanging system that classification reclaims and multistage thermal energy storage system, described steam heat-exchanging system comprises the steam heat exchanger that two-stage is above, described multistage thermal energy storage system comprises the heat-storing device that two-stage is above, carries out classification with the heat energy that will reclaim according to differing temps and stores.
As shown in Figure 1, structural representation for a specific embodiment of afterheat of slags recovery system of the present invention, coupled slag handling system can be the semi-wet slag treatment system, but this semi-wet slag treatment system comprises slag buffer memory storehouse 104, the shredder assembly 106 of high-pressure aerial fog nozzle 105 high speed rotating, solid slag heat-exchanger rig, 104 tops, described slag buffer memory storehouse have high-temperature liquid state slag 101 inlets and high-temperature gas outlet, and described slag inlet is connected to the tap cinder mouth by slag guide pipe 103, fecal iron separator 102; Described high-pressure aerial fog nozzle 105 and shredder assembly 106 are arranged at the below of slag inlet, high-pressure aerial fog nozzle 105 sprays to the shredder assembly direction with high-pressure aerial fog (air-water by a certain percentage mixes the gas-water mixture that forms), and the mouth of slagging tap of described slag guide pipe 103 vertically imports to slag the top of the shredder assembly in the slag buffer memory storehouse 104; The vapour outlet in described steam buffer storehouse 104 is connected to the steam heat-exchanging system; Described solid slag heat-exchange system is the multi-stage heat exchanger take-off equipment, is arranged at the middle and lower part in this slag buffer memory storehouse, the below of shredder assembly.This semi-wet slag treatment system is applicable to the blast furnace ironmaking production process, the liquid slag that high temperature is red-hot becomes to can be used for making the raw material of cement by the cooling cooling process, and residual neat recovering system of the present invention saves as available form with the heat recuperation that slag cooling heat transferring process produces.Those skilled in the art according to description of the invention as can be known; the present invention is not limited in the application that combines with this semi-wet slag treatment system; also can combine with other treatment of slag and reclaim afterheat of slags, similarly variation all belongs to protection scope of the present invention.
Particularly, among this embodiment of the present invention, as shown in Figure 1, in this specific embodiment of the present invention, the steam heat-exchanging system can be high, medium and low temperature classification heat-exchange system, it comprises placed in-line three grades of vapor heat exchangers: first step vapor heat exchanger 201, second stage vapor heat exchanger 202 and third stage vapor heat exchanger 203, and interchanger at different levels are made up of two loops: the outside provides the medium (the high-temperature gas mixture body that slag handling system produces) of heat energy to form first loop; Inside is used for utilizing the medium (present embodiment is adopted and used water as this medium) that reclaims heat energy to form second loop.As shown in the figure, in described three grades of vapor heat exchangers, each vapor heat exchanger includes housing and is arranged at the intravital heat transfer tube of this shell, during being connected to, the heat transfer tube temperature end outlet of first step vapor heat exchanger 201 presses thermophore 302, the temperature end outlet of second stage vapor heat exchanger 202 is connected to low pressure bag 303, third stage vapor heat exchanger 203 comprises two groups of heat transfer tubes, wherein one group of heat transfer tube of diagram top be since the distilled water that gets off of self power generation steam turbine condensation make the water source, its temperature end outlet can directly insert the circulation waterway of interchanger; Another group heat transfer tube of third stage vapor heat exchanger 203 belows is used for replenishing new cold water, and its temperature end outlet is connected to deoxygenator 306 earlier and inserts low pressure bag 303 again, enters the circulation waterway of vapor heat exchangers at different levels.
The high-temperature gas mixture body that produces in the described slag handling system 100 enters vapor heat exchangers 201 at different levels from the vapor recovery warehouse on 104 tops, slag buffer memory storehouse through the steam conveying pipe order, 202,203, and carry out thermal exchange with corresponding heat transfer tubes at different levels, make medium (high-temperature gas mixture body) temperature in first loop of each vapor heat exchanger reduce, medium in second loop (water of heat transfer tube inside) temperature raises, then, the thermal energy storage that will be reclaimed by the temperature end outlet of the heat transfer tube of vapor heat exchangers at different levels is to the heat-storing device (vide infra) of corresponding temperature grade.
Multistage thermal energy storage system comprises high pressure drum 301, middle pressure thermophore 302 and 303 3 grades of heat-storing devices of low pressure bag, and in aforementioned each heat-storing device, and the high pressure drum can press the temperature in the thermophore more stable relatively to middle pressure thermophore supply institute heat requirement in making; Simultaneously, the heat-storing device of low relatively one-level by other heat-exchanger rig of high one-level to other heat-storing device supplementary feed of high one-level.Among Fig. 1, high pressure drum 301 is pressed thermophore 302 in being connected to by relief valve 304; At the intermittence of no slag treatment, along with generating consumes a large amount of steam, the middle thermophore 302 interior temperature of pressing constantly descend, the high-temperature steam that is stored in high pressure drum 301 this moment can be given middle pressure thermophore 302 with the thermal energy transfer in the high pressure drum 301 through relief valve 304, to press the temperature in the thermophore 302 in stable; When the water that consumes when high pressure drum 301 reached certain threshold value, the middle warm water of middle pressure thermophore 301 mixed and supply high pressure drum 301 after plate-type heat exchanger 107 heats through ejector 310 jets with the liquid water of the bottom of high pressure drum 301 through liquid pump 312 pressurization backs; Cryogenic condensation water is given third stage vapor heat exchanger 203 by liquid pump 307 pressurizations, and by mixing via ejector 308 with the liquid water of low pressure bag 303 bottoms after 203 heating of third stage vapor heat exchanger and after 202 heating of second stage vapor heat exchanger, resupplying low pressure bag 303, enter the circulating water line of interchanger, simultaneously, the liquid water that low pressure bag 303 temperature of lower are lower can resupply middle pressure thermophore 302 by the liquid water of liquid pump 311 pressurization backs and middle pressure thermophore 302 bottoms after ejector 309 is mixed into 201 heating of first step vapor heat exchanger, to replenish the steam water that generating consumes; In addition, the middle thermophore 302 of pressing is connected to low pressure bag 303 by relief valve 305, deoxygenator 306, the cold soft water of new benefit injects low pressure bag 303 through third stage vapor heat exchanger 203 heat exchange and after deoxygenator 306 deoxygenations, makes low pressure bag 303 harvest heat, new water supply, deoxygenation function in one.
Wherein, first entrance end of ejector 308, second entrance end are connected to the temperature end outlet and the low pressure bag bottom water outlet of the top water of condensation heat transfer tube of third stage vapor heat exchanger 203 respectively, and its exit end connects the heat transfer tube low-temperature end inlet of second stage vapor heat exchanger 202; And first entrance end of ejector 309, second entrance end are connected to low pressure bag 303 bottom water outlets and middle bottom water outlet of pressing thermophore 302 respectively, and its exit end connects the heat transfer tube low-temperature end inlet of first step vapor heat exchanger 201; Press the bottom water outlet of thermophore 302 bottom water outlets and high pressure drum 301 during first entrance end of ejector 310, second entrance end are connected to respectively, its exit end connects the heat transfer tube low-temperature end inlet of plate-type heat exchanger 107, specifically sees also accompanying drawing.
On the other hand, described solid slag heat-exchange system is in the transmission course of solid slag described solid slag to be carried out the heat exchange cooling.In the present embodiment, this solid slag heat-exchange system comprises plate-type heat exchanger 107 and the air heat-exchange system that forms based on aforementioned solid slag transmission refrigerating unit.The high temperature furnace slag in slag buffer memory storehouse 104 at first carries out the contact heat exchange with plate-type heat exchanger 107, the heat energy of solid slag cooling heat transferring is converted into high temperature heat by plate-type heat exchanger 107 is stored into high pressure drum 301 as the high-temperature heat-storage device.In conjunction with described slag handling system as can be known, in this specific embodiment of the present invention, described solid slag heat-exchange system also is included in the air heat-exchange system that forms in this slag buffer memory storehouse and the described solid slag transmission refrigerating unit, and is specific as follows:
In the embodiments of the invention, be provided with recirculation blower 205 between the tail gas outlet of the last step vapor heat exchanger (present embodiment is a third stage vapor heat exchanger 203) of described steam heat-exchanging system and the blast inlet of described fluid-bed heat exchanger 109, between described steam heat-exchanging system and solid slag heat-exchange system, form the gas circulation path, adopt recirculation blower 205 to provide recirculated air as heat-eliminating medium and slag buffer memory storehouse 104 (containing the slag in plate-type heat exchanger 107 gaps), auger heat exchange handling machinery 108, slag in the fluid-bed heat exchanger 109 carries out heat exchange, and heated air and water vapor enter the steam heat-exchanging system after mixing.Reclaim hypertonia in the path for fear of steam heat-exchanging, can be provided with certain pressure fan 204 at the upstream side of recirculation blower 205, concrete set-up mode can repeat no more with reference to prior art herein.
The high-temperature gas mixture body that produces in the slag treatment process is subjected to recirculation blower 205 draft effects, press thermophore 302 (middle pressure drum) to store in high temperature heat being passed to when the first step vapor heat exchanger 201 by the vapor recovery warehouse at 104 tops, slag buffer memory storehouse with 200～250 ℃ of high temperature heat forms, heat energy is passed to low pressure bag 303 and store through second stage vapor heat exchanger 202 again from first step vapor heat exchanger 201 tail gas discharged with 90～120 ℃ of low temperature heat energy forms, heat energy is passed to 90～120 ℃ water of low pressure bag 303 in from second stage vapor heat exchanger 202 tail gas discharged steam through third stage vapor heat exchanger 203 and mixed, also store with the low temperature heat energy form with it.
In order to make the temperature that enters the recirculated air in the fluid-bed heat exchanger 109 lower, thereby make the slag temperature of output lower, in the present embodiment, 109 of described recirculation blower 205 and fluid-bed heat exchangers also are provided with tail gas heat exchanger 206, the low temperature water-in of the heat transfer tube of this tail gas heat exchanger 206 is connected to precipitation tank 112 through a strainer 207, will provide through the water after the heating to dirt ash flushing pipe.The high-temperature gas mixture body after aforementioned three grades of heat exchange, can make exhaust temperature reach≤50 ℃, again by recirculation blower pressurization,, heat energy is passed to flushing cinder water and dirt ash wash water further with tail gas heat exchanger 206 heat exchange; Low temperature exhaust gas is re-used as heat-eliminating medium in fluid-bed heat exchanger and slag heat exchange, can make the slag tapping temperature drop to minimum (50～80 ℃), and be fluidized an interchanger 109 warmed-up tail gas again when auger heat exchange handling machinery 108, plate-type heat exchanger 107 and solid-state slag heat exchange, and the high-temperature gas mixture (being called for short the high-temperature gas mixture body) that heats up and be converted into steam and air, enter next circulation through slag buffer memory storehouse 104.
In conjunction with aforementioned slag handling system as can be known, the principle of work of this residual neat recovering system of the present invention is as follows:
1400～1500 ℃ of red-hot liquid slags of high temperature import to vapor recovery warehouse according to definite shape, direction behind guide pipe; Make its cooling, preliminary heat exchange be cooled to 900～1100 ℃ with high-pressure aerial fog (present embodiment the is vaporific gas-water mixture) spray of pointing to shredder assembly towards liquid slag; The heat exchange of further spraying water is cooled to 600～700 ℃ to the slag shattering process by the commutation shredder assembly of a pair of high speed rotating again; Lower the temperature at high temperature furnace slag, solidify, in the cooling heat transferring process, the water in the high-pressure aerial fog is evaporated vaporization and forms 300～400 ℃ of high-temperature gas mixture bodies with air in the pipeline; The high-temperature gas mixture body is subjected to recirculation blower draft effect, presses thermophore in high temperature heat being passed to when the first step vapor heat exchanger by vapor recovery warehouse, and stores with 200～250 ℃ of high temperature heat forms; The tail gas that goes out first step vapor heat exchanger is passed to the low pressure bag through second stage vapor heat exchanger with heat energy, and stores with 90～120 ℃ of low temperature heat energy forms; The tail gas steam that goes out second stage vapor heat exchanger is passed to the low pressure bag through third stage vapor heat exchanger with heat energy, and mixes with 90～120 ℃ of water, also stores with the low temperature heat energy form; Tail gas pressurizes through recirculation blower, further makes exhaust temperature reach minimum with the tail gas heat exchanger heat exchange, simultaneously with waste heat heating flushing cinder water that absorbs and interchanger dirt ash wash water; Tail gas be re-used as heat-eliminating medium further in fluid-bed heat exchanger with solid-state slag heat exchange, tail gas is heated once more, it is minimum that the slag tapping temperature is dropped to; Be fluidized the warmed-up gas of an interchanger, when conveying auger interchanger, plate-type heat exchanger and solid slag heat exchange and heat up and to be converted into 300～400 ℃ of high temperature airs, enter vapor recovery warehouse and water vapour and be mixed into next the circulation again; 600～700 ℃ high-temp solid slag between plate-type heat exchanger with the heat transfer tube contact heat-exchanging, slag heat energy is converted into high temperature heat by plate-type heat exchanger is stored into the high pressure drum with 300～400 ℃ of high temperature saturation water forms, in addition, also can carry out heat exchange during recirculated air process plate-type heat exchanger, further the heating cycle air with high-temp solid slag therebetween; The water of condensation that water vapor in the high-temperature gas mixture body forms through three grades of interchanger condensations of steam and wash the sewage that gets off by dirt ash wash-down water enters the tank precipitation through the dedusting reflux line, enters the next round circulation after filtering through filter.
Corresponding with above-mentioned afterheat of slags recovery system, the present invention also proposes a kind of method for recovering waste heat from scoria, and this method comprises:
A. reclaim the heat energy in the slag treatment being carried out the classification heat exchange by the multi-stage heat exchanger device;
B. the heat energy classification of the different qualities (temperature) that heat exchange is reclaimed is stored in the multistage heat-storing device.
Particularly, in the described steps A, the high-temperature gas in described slag buffer memory storehouse 104 enters placed in-line steam heat exchanger at different levels through the transport pipe order, utilizes the multistage steam heat-exchanger rig that the heat energy of the steam that produces in the slag treatment is carried out multi-stage heat exchanger and reclaims; And, the thermal energy storage that first step vapor heat exchanger 201 reclaims is to middle pressure thermophore 302, the thermal energy storage that second stage vapor heat exchanger 202 reclaims is to low pressure bag 303, cryogenic condensation water or newly mend cold soft water can enter vapor heat exchangers at different levels after 203 heating of third stage vapor heat exchanger circulation waterway.
Wherein, as shown in Figure 1, third stage vapor heat exchanger 203 is provided with upper and lower two groups of heat transfer tubes, wherein one group of heat transfer tube of diagram top be since the distilled water that gets off of self power generation steam turbine condensation make the water source, its temperature end outlet can directly insert the circulation waterway of interchanger; Another group heat transfer tube of third stage vapor heat exchanger 203 belows is used for replenishing new cold water, and its temperature end outlet is connected to deoxygenator 306 earlier and inserts low pressure bag 303 again, enters the circulation waterway of vapor heat exchangers at different levels.
On the other hand, also can utilize multistage solid slag heat-exchanger rig liquid towards slag to carry out the multi-stage heat exchanger recovery in the described steps A through the heat energy of the broken solid granulates that forms of shredder assembly, as at first passing through plate-type heat exchanger 107 contact heat-exchangings of bottom, slag buffer memory storehouse, auger heat exchange handling machinery 108 by plate-type heat exchanger 107 bottoms is delivered to fluid-bed heat exchanger 109 and to the process of the equipment of mucking haulage, carries out the heat exchange processing by this auger heat exchange handling machinery 108 and fluid-bed heat exchanger 109 then.
Further, in order fully to reclaim afterheat of slags, between described steam heat-exchanging system and solid slag heat-exchange system, form the gas circulation path, be provided with recirculation blower 205 between the tail gas outlet of the last step vapor heat exchanger (third stage vapor heat exchanger 203) of described steam heat-exchanging system and the blast inlet of last step solid slag interchanger (fluid-bed heat exchanger 109), adopt recirculated air that recirculation blower 205 provides to carry out heat exchange as heat-eliminating medium and plate-type heat exchanger 107, auger heat exchange handling machinery 108, fluid-bed heat exchanger 109 interior slags.
Among this embodiment of the present invention, described multistage thermal energy storage system can comprise high pressure drum 301, middle pressure thermophore 302 and 303 3 grades of heat-storing devices of low pressure bag, and in described each heat-storing device, high pressure drum 301 can cooperate with the middle pressure thermophore 302 of low one-level with to its supply institute heat requirement, presses in the thermophore 302 temperature more stable relatively in making; Simultaneously, the heat-storing device of low relatively one-level by other heat-exchanger rig of high one-level to other heat-storing device supplementary feed of high one-level.Specifically see also Fig. 1, described high pressure drum 301 is pressed thermophore 302 in being connected to by relief valve 304, press thermophore 302 to be connected to the low pressure bag in described by relief valve 305,305 ', deoxygenator 306, and newly mend cold soft water and inject the low pressure bag, make the low pressure bag harvest heat, new water supply, deoxygenation function in one through third stage vapor heat exchanger 203 heat exchange and after deoxygenator 306 deoxygenations.
This embodiment principle of work of the present invention is as follows:
1400～1500 ℃ of red-hot liquid slags of high temperature import to vapor recovery warehouse according to definite shape, direction behind guide pipe; Make its cooling, preliminary heat exchange be cooled to 900～1100 ℃ with the high-pressure aerial fog that points to broken wheel mechanism (air-water by a certain percentage mixes the gas-water mixture that forms) spray towards liquid slag; The heat exchange of further spraying water is cooled to 600～700 ℃ to the slag shattering process by the broken wheel mechanism of the commutation of a pair of high speed rotating again; Lower the temperature at high temperature furnace slag, solidify, in the cooling heat transferring process, the water in the high-pressure aerial fog is evaporated vaporization and forms 300～400 ℃ of high-temperature gases with air in the pipeline; High-temperature gas is subjected to recirculation blower draft effect, press thermophore to store in high temperature heat being passed to when the steam first-class heat exchanger by vapor recovery warehouse with 200～250 ℃ of high temperature heat forms, the tail gas that goes out first step vapor heat exchanger is passed to the low pressure bag stored, goes out second stage vapor heat exchanger with 90～120 ℃ of low temperature heat energy forms tail gas steam through second stage vapor heat exchanger with heat energy and through the third stage vapor heat exchanger heat energy is passed to 90～120 ℃ of water of low pressure Bao Bingyu and mix, and also stores with the low temperature heat energy form; Tail gas pressurizes through recirculation blower, further makes exhaust temperature reach minimum with the tail gas heat exchanger heat exchange, simultaneously with the waste heat heating flushing cinder water and the interchanger dust wash water that absorb; Tail gas is re-used as heat-eliminating medium further by fluid-bed heat exchanger and solid-state slag heat exchange, and tail gas is heated once more, and it is minimum that the slag tapping temperature is dropped to; Be fluidized the warmed-up gas of an interchanger, heating up through conveying auger interchanger, plate-type heat exchanger heat exchange is converted into 300～400 ℃ of high temperature airs again, enters vapor recovery warehouse and water vapour and is mixed into next circulation; The high-temp solid slag in plate-type heat exchanger except that the heat exchange of carrying out with recirculated air, 600～700 ℃ high temperature furnace slag and plate-type heat exchanger carry out the contact heat exchange simultaneously, slag heat energy is converted into high temperature heat by plate-type heat exchanger is stored into the high pressure drum with 300～400 ℃ of high temperature saturation water forms; The water of condensation that high-temperature water vapor forms through three grades of interchanger condensations of steam and wash the sewage that gets off by the dust wash-down water enters the water reservoir precipitation through the dedusting reflux line, enters the next round circulation after filtering through filter.
Because afterheat of slags recovery system of the present invention and recovery method, adopted high, medium and low temperature classification heat exchanger system that the classification in high, medium and low temperature heat accumulation bag of corresponding different quality heat energy is stored, the high-quality heat energy of warm drum can be directly used in generating in making; High thermometer bulb cooperates with middle thermometer bulb, heat when making no slag treatment can be by high thermometer bulb to middle thermometer bulb supply, thermometer bulb has realized that middle Hair Fixer electricity and accumulation of heat in one, have guaranteed the more stable relatively of middle pressure thermophore temperature in making, and cooperates the use of steam turbine relief valve to make steam turbine work more stable; Being used of low pressure bag, deoxygenator makes the accumulation of heat of low pressure bag, new water supply deoxygenation in one; Make that system component is with better function, system is simpler.
As shown in Figure 2, it is the structural representation of a concrete Application Example of afterheat of slags recovery system of the present invention and method.In this Application Example, the agent structure of afterheat of slags recovery system, the step of exhaust heat recovering method can repeat no more with reference to aforementioned content herein.Further, should be that this afterheat of slags recovery system is combined with semi-wet slag treatment system and afterheat generating system with embodiment.
The semi-wet slag treatment system comprises slag buffer memory storehouse, high-pressure aerial fog nozzle (or high-pressure water mist nozzle, below be that example describes with the high-pressure aerial fog nozzle) but the shredder assembly and the solid slag transmission refrigerating unit of high speed rotating, top, described slag buffer memory storehouse has high-temperature liquid state slag inlet and high-temperature gas outlet, and described slag inlet is connected to the tap cinder mouth by fecal iron separator, slag guide pipe; Described high-pressure aerial fog nozzle and shredder assembly are arranged at the below of slag inlet, the high-pressure aerial fog nozzle sprays to the shredder assembly direction with high-pressure aerial fog, the mouth of slagging tap of described slag guide pipe vertically imports to slag the top of the shredder assembly in slag buffer memory storehouse, described solid slag transmission refrigerating unit is positioned at the below of this shredder assembly, be used to transmit this solid slag, and in the transmission course of this solid slag, further described solid slag cooled.
Preferable, this semi-wet slag treatment system is to utilize air-water by a certain percentage to mix the high-pressure aerial fog cooling blast furnace liquid slag that forms, and utilizes shredder assembly that slag is carried out Mechanical Crushing, is processed into the raw material that is used to make cement.
Semi-wet slag treatment system of the present invention is applicable to the blast furnace ironmaking production process, and the liquid slag that high temperature is red-hot becomes to can be used for making the raw material of cement by the cooling cooling process, and the heat recuperation that the slag process of cooling is produced saves as available form.
Particularly, in conjunction with shown in Figure 2, semi-wet slag treatment system 100 mainly comprises: liquid slag 101, fecal iron separator 102, slag guide pipe 103, slag buffer memory storehouse 104, high-pressure aerial fog nozzle 105, shredder assembly 106 etc.
Effusive 1400～1500 ℃ of red-hot liquid slags 101 of tap cinder mouth realize that through fecal iron separator 102 slag iron separates, and makes liquid slag import to slag buffer memory storehouse 104 by definite shape, distribution, direction through slag guide pipe 103 then earlier.In the present embodiment, the mouth of slagging tap of described slag guide pipe 103 is flat pattern and along the shredder assembly axial distribution, slag is vertically imported slag buffer memory storehouse 104, because the shredder assembly 106 of present embodiment comprises two broken wheels, therefore, this mouth of slagging tap can be along axially being distributed to slag on the shredder assembly 106 of broken wheels, and high-pressure aerial fog nozzle 105 sprays to the shredder assembly direction with high-pressure aerial fog.
As shown in Figure 2, the solid slag transmission refrigerating unit of present embodiment comprises plate-type heat exchanger 107, auger heat exchange handling machinery 108, fluid-bed heat exchanger 109, wherein, described plate-type heat exchanger 107 is installed in the middle and lower part in described slag buffer memory storehouse 104, be positioned at the below of described shredder assembly 106, the feed end of described auger heat exchange handling machinery 108 is located at the bottom of this plate-type heat exchanger 107, and its discharging termination is established this fluid-bed heat exchanger 109, the outer equipment of mucking haulage that is provided with of the outlet of fluid-bed heat exchanger 109.Solid slag after the fragmentation falls into 107 of plate-type heat exchangers, and under the combined action of gravity and the 108 rotation transmission drives of bottom auger conveying interchanger, constantly move down, and in folding process by lowering the temperature with the contact heat-exchanging of plate-type heat exchanger 107 and heat being passed to recirculated water in the plate-type heat exchanger 107, the gas converting heat between the slag charge slit also and around the plate-type heat exchanger simultaneously; Described auger heat exchange handling machinery 108, fluid-bed heat exchanger 109 then utilize the Cryogenic air that feeds to carry out the heat exchange cooling in the other direction.Because the concrete structure and the set-up mode of this plate-type heat exchanger 107, auger heat exchange handling machinery 108 and fluid-bed heat exchanger 109 can be implemented with reference to prior art, therefore, repeat no more herein.
The high-temperature gas outlet top at these 104 tops, slag buffer memory storehouse is provided with dirt ash flooding nozzle 114, is used to clear up the floating ash on the superheater; The bottom in this slag buffer memory storehouse 104 is a comb hydrophone 111, and the water outlet of this comb hydrophone 111 can lead to the precipitation tank by pipeline, and the water of tank 112 can be recycled through behind the sedimentation and filtration, supplies water for high-pressure aerial fog nozzle 105 and dirt ash wash-down water pipeline 113.
In this semi-wet slag treatment system, high-temperature liquid state slag 101 realizes that by fecal iron separator 102 the slag iron of slag separates; Slag guide pipe 103 imports to slag buffer memory storehouse 104 (can simultaneously as vapor recovery warehouse) with liquid slag 1 according to definite shape, distribution, direction; High-pressure aerial fog nozzle 105 points to the shredder assembly direction with high pressure water, impacts liquid slag 101 and makes its preliminary fragmentation, cooling be cooled to half curdled appearance; The commutation shredder assembly of high speed rotating is further broken to the semi-solid state slag that falls, spout hole 1182 on the broken simultaneously wheel 116 further is cooled to its cooling and satisfies follow-up air-cooled required condition, comprise uniform grain sizes, NA temperature, ventilation property and bulk cargo flowability preferably, in the specific embodiment of the present invention, described slag is cooled to 600～700 ℃ of granularity 1～8mm, temperature by the water spraying structure fragmentation on the described shredder assembly, cooling; This solid granulates is further lowered the temperature through plate-type heat exchanger 107, conveying auger interchanger 108, fluid-bed heat exchanger 109 and is cooled to 50～80 ℃ or following, transfers to cement source mill by drag-out slag car 110 again.
Afterheat of slags recovery system and recovery method see also the content of last embodiment, and can repeat no more in conjunction with the content of aforementioned slag treatment part and the hereinafter description of cogeneration part herein.
Afterheat of slags power generation system 500 is to utilize the heat energy that classification stores in the multistage thermal energy storage system to generate electricity, this power generation system comprises generator, steam turbine, ammonia turbine and absorption heat pump, the heat energy that reclaims in the slag treatment process is stored in the described multistage thermal energy storage system by different temperature grade classifications, described multistage thermal energy storage system is to the steam turbine delivering vapor, steam turbine is converted into the power machine energy with heat energy, and the drive generator is converted into electric energy with mechanical energy; This absorption heat pump adopts ammonia-water to make working medium, the low-quality heat energy that described steam turbine is exported terminal steam is converted into higher quality heat energy, and provide high-quality driving heat source for described heat pump by described thermal energy storage system, the strong aqua mixing solutions is under high pressure evaporated in a large number form the saturated ammonia of high pressure, drive the ammonia turbine and can be converted to mechanical energy, export to generator with the mechanical energy merging that steam turbine produces with the pressure that ammonia is produced.
The present invention utilizes the classification of heat energy to reclaim, the high-quality heat energy that makes energy recovery return is realized high-quality direct utilization, low-quality heat energy and the tail gas that in the past diffused can promote by means of heat pump and utilize, thereby played the purpose that improves comprehensive utilization ratio, and, because the use of ammonia turbine, except that more howing than the generated energy of simple steam turbine, the use of ammonia turbine also has the generating of reduction fluctuation, improves the effect of power generating quality; And heat pump makes the turbine exhaust gas temperature, pressure reduce, and help improving turbine efficiency, and the reduction of exhaust temperature helps reducing the slag charge temperature out, and has the energy emission of minimizing effect.
In the present embodiment, steam turbine and ammonia turbine can adopt existing multiple mode to realize driving the purpose that generator rotates generating with the power that merges, and repeat no more herein.
As shown in Figure 2 and in conjunction with aforementioned content, this multistage thermal energy storage system can comprise high pressure drum 301, middle pressure thermophore 302 and low pressure bag 303.
The heat energy that is reclaimed by the high-temperature gas mixture body in the slag treatment process is stored in high pressure drum 301, middle pressure thermophore 302 and the low pressure bag 303 by different temperature grade classifications, and the high-quality energy recovery that the solid slag heat-exchange system reclaims in the slag treatment process is to high pressure drum 301; The heat energy of the high-temperature gas mixture body that produces in the slag treatment process passes through the steam heat-exchanging system recoveries, and the thermal energy storage of high temperature grade is used for generating in middle pressure thermophore 302.
Press thermophore 302 to steam turbine 501 delivering vapors in described, steam turbine 501 is converted into the power machine energy with heat energy, and drives generator 502 mechanical energy is converted into electric energy; This absorption heat pump adopts ammonia-water to make working medium, strong aqua mixing solutions in the described heat pump under high pressure is heated to 100～120 ℃ through the driving heat source from high pressure drum 301, ammonia is evaporated in a large number form the saturated ammonia of high pressure, cross heat abstraction free liquid attitude molecule and enter ammonia turbine 511 through 120～150 ℃, the pressure that ammonia is produced can be converted to mechanical energy, exports to generator 502 with the mechanical energy merging that steam turbine 501 produces.
As shown in Figure 2, preferably, middle thermophore 302 and 501 in the steam turbine of pressing is provided with vapor superheater 520 and relief valve 521, this vapor superheater 520 is arranged at the top of the vapor recovery warehouse 104 of slag treatment, the saturation steam of pressing thermophore 302 to come out in described is crossed liquid saturation water in the heat abstraction steam through vapor superheater 520, and through relief valve 521 to the metastable generating superheated vapour of steam turbine 501 transfer pressures.
In addition, described high pressure drum 301 is connected by a relief valve 304 with middle pressure thermophore 302, off period in no slag treatment, along with warm steam in the continuous consumption of generating, the middle thermophore 302 interior temperature of pressing constantly descend, the high-temperature steam that is stored in high pressure drum 301 this moment is given middle pressure thermophore 302 through this relief valve 304 with the thermal energy transfer in the high pressure drum 301, press thermophore 302 temperature relatively stable in keeping, and the water that high pressure drum 301 is consumed also can be supplied with high pressure drum 301 through water pump 310 pressurizations again by the middle warm water of middle pressure thermophore 302 after plate-type heat exchanger 107 heating.
As shown in the figure, absorption heat pump comprises producer 512, resorber 513, steam condenser 503 and heat exchanger 514, this producer 512 with the high-temperature steam of high pressure drum 301 as driving heat source, and the import of an ammonia superheater 516 is connected with this high pressure drum 301, its exit end is connected to the steam-gas inlet of heat pump producer 512 by a relief valve 515 ', and the vapor outlet port of this producer 512 is pressed thermophore 302 in being connected to; Present embodiment is pressed thermophore 302 in the exit end of described ammonia superheater 516 also is connected to by another relief valve 515 so that in ammonia superheater 516 overheated ammonias, be convenient to flexible overheated with the ratio that drives with heat.
On the one hand, the circulating path of the steam-water in this power generation system is: press the high-temperature gas outlet of thermophore 302 to be connected to steam turbine 501 by vapor superheater 520, relief valve 521 in described, the tail gas of this steam turbine 501 (low-temperature saturated steam) outlet is sent into by pipeline and is formed cryogenic condensation water in the steam condenser 503, the condensation-water drain of this steam condenser 503 is connected to the cryogenic condensation water inlet end of steam heat-exchanging system, so that recirculated water to be provided.
On the other hand, the ammonia of this power generation system-ammoniacal liquor circulating path is: the high-temperature gas outlet of high pressure drum 301 is connected to heat pump producer 512 as driving heat source by relief valve 515 '; The ammonia outlet of described producer 512 is delivered to ammonia turbine 511 via a throttling valve 517, and this ammonia pipeline is arranged at the ammonia superheater 516 of this producer outside through one simultaneously, so that ammonia is carried out Overheating Treatment; The low temperature ammonia outlet of ammonia turbine 511 is connected to resorber 513, the low concentration ammonia water inlet of this resorber 513 is connected to the low concentration ammonia water out of producer 512 by heat exchanger 514, the high strength ammonia water inlet that is connected to producer 512 after steam condenser 503 heats again through this heat exchanger 514 is delivered in the low temperature and high concentration ammoniacal liquor outlet of this resorber 513 by a force (forcing) pump 518, realize the circulation of ammonia, the lifting utilization that has realized low-quality heat energy simultaneously, diffused tail gas.
Wherein the strong aqua mixing solutions in this producer 512 under high pressure is heated to 100～120 ℃ through the driving heat source from high pressure drum 301, ammonia is evaporated in a large number form the saturated ammonia of high pressure, carry out 120～150 ℃ through ammonia superheater 516 and cross heat abstraction free liquid attitude molecule, and enter ammonia turbine 501 through throttling valve 517; The low concentration ammonia aqueous solution in the producer 512 after the ammonia evaporation is got back to resorber 513 after heat exchanger 514 heat exchange; And the ammonia that leaves ammonia turbine 511 outlet forms high density ammoniacal liquor once more resorber 513 in and from low concentration aqueous solution's blended absorbent of producer 512, high density ammoniacal liquor is by pump 518 pressurizations, make water vapor condensation through 60～80 ℃ of terminal steam heat-exchangings of steam condenser 503 and steam turbine 501 outlets, and the latent heat of condensation of absorption water vapour, after heat exchanger 514 and lower concentration ammoniacal liquor heat exchange, enter producer 512 again, enter next the circulation thereby the low-quality heat energy that makes present embodiment can utilize this heat pump to absorb is converted into 100～120 ℃ higher quality heat energy from producer 512.
As can be seen from Figure, 60～80 ℃ of terminal low-temperature saturated steams of being discharged by steam turbine 501 outlets cool off through steam condenser 503, terminal steam cooling is condensed into 30～40 ℃ distilled water, and low-temperature distillation water is made heat-eliminating medium and is injected third stage vapor heat exchanger 203 by liquid pump 307 pressurizations, enters the circulation waterway of steam heat-exchanging system through third stage interchanger 203 heated hot water; Finally can after pressurized, heated, supply be used for replenishing the steam water that generating consumes to middle pressure thermophore.
Because steam turbine 501 terminal steam condensers 503 use, not only improved terminal negative pressure value, thereby improved steam turbine 501 heat energy-mechanical energy transformation efficiency, made the open end of original water cooling tower change internal heat energy recovery loop into simultaneously, greatly reduced terminal heat-energy losses.And, at the intermittence of no slag treatment, the middle interior pressure of thermophore of pressing can reduce with temperature, thereby have influence on the works better of generator, if the intermittently long works better that just possibly can't guarantee generator, and the use of ammonia turbine, can guarantee under middle pressure thermophore 302 vapor pressures situation on the low side, to keep the generator works better, and the heat dynamic resource of its use is the cheap generator tail gas that in the past was dropped, therefore, present embodiment is except that more howing than the generated energy of simple steam turbine, the use of ammonia turbine can also reduce the generating fluctuation, improve power generating quality, the influence that fluctuate to power generation system the intermittence in the time of further can also weakening no slag treatment.
By said structure as can be known, in the present embodiment, the working process of this afterheat of slags power generation system is as follows:
The saturation steam that comes out by middle pressure thermophore 302, cross liquid saturation water in the heat abstraction steam through vapor superheater 520,, through steam turbine 501 heat energy is converted into power drive generator 502 and is converted into electric energy to the metastable generating steam of steam turbine 501 transfer pressures through relief valve 521; 60～80 ℃ of terminal low-temperature saturated steams that steam turbine 501 outlets are discharged are through steam condenser 503 coolings, with terminal steam cooling is 30～40 ℃ of water of condensation, cryogenic condensation water is made heat-eliminating medium and is given third stage vapor heat exchanger 203 by water pump 307 pressurizations, and heated hot water enters circulation waterway behind third stage vapor heat exchanger 203; Off period in no slag treatment, along with generating constantly consumes a large amount of steam, the middle thermophore 302 interior temperature of pressing constantly descend, the high-temperature steam that is stored in this moment in the high pressure drum 301 is given middle pressure thermophore 302 through relief valve 304 with the thermal energy transfer in the high pressure drum 301, press the relatively stable of thermophore 302 temperature in keeping, and the water that is consumed is pressurizeed through water pump 309 after press thermophore 302 in supplying with after 202 heating of second stage vapor heat exchanger by the water at low temperature of low pressure bag 303; Supply with high pressure drum 301 by the middle warm water of middle pressure thermophore 302 through water pump 310 pressurizations and after plate-type heat exchanger 107 heating at the water that high pressure drum 301 is consumed; Absorption heat pump adopts ammonia-water to make working medium, ammoniacal liquor mixing solutions in its producer 512 under high pressure is heated to 100～120 ℃ through the driving heat source from high pressure drum 301, make the ammonia that ammonia evaporates generation in a large number cross heat abstraction free liquid attitude molecule through 120～150 ℃, enter ammonia turbine 511 through throttling valve 517, the pressure that ammonia is produced can be converted to mechanical energy, and can export to generator 502 with the mechanical energy merging that steam turbine 501 produces; The low concentration ammonia aqueous solution after the evaporation is got back to resorber 513 after heat exchanger 514 heat exchange; Heat absorption causes self temperature to drop to 0～10 ℃ because air pressure sharply descends to leave the ammonia of ammonia turbine 511 outlet, forms high density ammoniacal liquor once more resorber 513 in and from low concentration aqueous solution's blended absorbent of producer 512; High density ammoniacal liquor is by pump 518 pressurizations, make water vapor condensation through steam condenser 503 and 60～80 ℃ of terminal steam heat-exchangings that steam turbine 501 exports, absorb the latent heat of condensation of water vapour, enter producer 512 again after heat exchanger 514 and the lower concentration ammoniacal liquor heat exchange from producer 512, the higher quality heat energy that the low-quality heat energy that absorbs is converted into 100～120 ℃ enters next circulation.
This afterheat generating system has adopted heat pump techniques and steam turbine, ammonia turbine to unite to drive generation technology and has utilized the afterheat of slags of multistage recovery, storage, has realized high-quality heat energy (steam turbine) direct generation of electricity; The low-quality thermal power transfer of utilizing heat pump to absorb turbine exhaust gas is the high-quality energy that can be used for the ammonia generating, has solved traditional steam turbine cooling tower heat radiation problem that heat-energy losses is big, conversion efficiency of thermoelectric is low; Heat pump also makes the steam turbine terminal temperature lower, and negative pressure value is bigger, makes the steam turbine energy conversion efficiency higher; Low condensing water temperature and replenish new water and be used for flushing cinder water, dirt ash wash-down water makes residual neat recovering system recycle gas temperature lower to the heat exchange of tail gas, the slag tapping temperature is lower, the system synthesis thermosteresis has still less improved the heat-photoelectric transformation efficiency of whole afterheat generating system greatly.
Though the present invention discloses with specific embodiment; but it is not in order to limit the present invention; any those skilled in the art; the displacement of the equivalent assemblies of under the prerequisite that does not break away from design of the present invention and scope, having done; or, all should still belong to the category that this patent is contained according to equivalent variations and modification that scope of patent protection of the present invention is done.
Claims (19)
1. afterheat of slags recovery system, it is characterized in that, described residual neat recovering system comprises: multistage steam heat-exchange system and multistage thermal energy storage system, described steam heat-exchanging system comprises the steam heat exchanger that two-stage is above, reclaim the high-temperature gas mixture body that produces in the slag treatment process is carried out classification, described multistage thermal energy storage system comprises the heat-storing device that two-stage is above, carries out classification with the heat energy that will reclaim in the slag treatment process according to differing temps and stores.
2. afterheat of slags recovery system as claimed in claim 1, it is characterized in that, described steam heat-exchanging system comprises the first step, the second stage, third stage vapor heat exchanger, the high-temperature gas mixture body that produces in the described slag treatment process enters vapor heat exchangers at different levels from the vapor recovery warehouse on top, slag buffer memory storehouse through the steam conveying pipe order, and vapor heat exchanger at different levels is with the thermal energy storage that the reclaims heat-storing device to the corresponding temperature grade.
3. afterheat of slags recovery system as claimed in claim 2, it is characterized in that, described multistage thermal energy storage system comprises high pressure drum, middle pressure thermophore and three grades of heat-storing devices of low pressure bag, and in described each heat-storing device, the high pressure drum can make its temperature more stable relatively to middle pressure thermophore supply heat; Simultaneously, the heat-storing device of low relatively one-level by other heat-exchanger rig of high one-level to other heat-storing device supplementary feed of high one-level.
4. afterheat of slags recovery system as claimed in claim 1 is characterized in that, described afterheat of slags recovery system also comprises the solid slag heat-exchange system, and this solid slag heat-exchange system carries out the multi-stage heat exchanger recovery to the heat energy of the solid slag that slag treatment forms.
5. afterheat of slags recovery system as claimed in claim 4, it is characterized in that, described solid slag heat-exchange system comprises plate-type heat exchanger, described plate-type heat exchanger is installed in the below of the shredder assembly of slag handling system, the solid slag that fragmentation forms in the slag treatment process falls into utmost point formula interchanger and carries out contact heat-exchanging, utilizes this plate-type heat exchanger that solid slag heat energy is converted into the heat-storing device that high temperature heat is stored into the corresponding temperature grade.
6. afterheat of slags recovery system as claimed in claim 5, it is characterized in that, described plate-type heat exchanger bottom is provided with auger heat exchange handling machinery, the discharge end of described auger heat exchange handling machinery is connected with fluid-bed heat exchanger, cryogenic gas enters from the blast inlet of fluid-bed heat exchanger, carries out heat exchange with the solid slag with this fluid-bed heat exchanger, auger heat exchange handling machinery and plate-type heat exchanger correspondence position.
7. afterheat of slags recovery system as claimed in claim 5, it is characterized in that, described afterheat of slags recovery system comprises the gas converting heat circulation path, and this gas converting heat circulation path is provided with recirculation blower, the high-temperature gas mixture body that produces in the slag treatment process is sent in the solid slag heat-exchange system at this recirculation blower of waste gas utilization that the steam heat-exchanging system carries out after multi-stage heat exchanger is handled, as the heat-eliminating medium that carries out heat exchange with solid slag, thereby be communicated with the solid slag heat-exchange system and the steam heat-exchanging system forms the gas converting heat circulation path.
8. afterheat of slags recovery system as claimed in claim 6, it is characterized in that, also be provided with tail gas heat exchanger between the tail gas outlet of described steam heat-exchanging system and fluid-bed heat exchanger blast inlet, after further heat exchange is lowered the temperature to the low temperature exhaust gas of steam heat-exchanging system, send into the solid slag heat-exchange system, and the water-in of this tail gas heat exchanger is connected to tank through a strainer, will provide through the water after the heating to dirt ash flushing pipe.
9. afterheat of slags recovery system as claimed in claim 2, it is characterized in that, vapor heat exchangers at different levels include housing and are arranged at the intravital heat transfer tube of this shell, during being connected to, the heat transfer tube high temperature outlet of first step vapor heat exchanger presses thermophore, the outlet of the heat transfer tube of second stage vapor heat exchanger is connected to the low pressure bag, third stage vapor heat exchanger comprises that is used to heat the cold soft heat transfer tube of new benefit, and its temperature end outlet is connected to the circulation waterway that deoxygenator enters each vapor heat exchanger more earlier.
10. afterheat of slags recovery system as claimed in claim 8 is characterized in that, described high pressure drum is pressed thermophore in being connected to by relief valve; Press thermophore to be connected to the low pressure bag in described, and newly mend cold soft water pipeline is connected to the low pressure bag through third stage vapor heat exchanger water supplement port by relief valve, deoxygenator.
11. a method for recovering waste heat from scoria is characterized in that, this method comprises:
A. reclaim the heat energy in the slag treatment being carried out the classification heat exchange by the multi-stage heat exchanger device;
B. the heat energy that heat exchange is reclaimed is stored in the multistage heat-storing device by the differing temps classification.
12. method for recovering waste heat from scoria as claimed in claim 10 is characterized in that, comprises in the described steps A:
A1. the high-temperature gas mixture body that produces of slag treatment process enters the first step, the second stage and third stage vapor heat exchanger through the transport pipe order, utilizes the multistage steam interchanger that the heat energy of the high-temperature gas mixture body that produces in the slag treatment is carried out multi-stage heat exchanger and reclaims.
13. method for recovering waste heat from scoria as claimed in claim 11, it is characterized in that, the thermal energy storage that first step vapor heat exchanger is reclaimed is to middle pressure thermophore, the thermal energy storage that second stage vapor heat exchanger is reclaimed is to the low pressure bag, and the water after by third stage vapor heat exchanger the cold soft water of new benefit or low-temperature distillation water being heated is sent into steam heat-exchanging systemic circulation water route.
14. method for recovering waste heat from scoria as claimed in claim 10 is characterized in that, also comprises in the described steps A:
A2. utilizing multistage solid slag heat-exchange system that the high-temperature solid particulate heat energy that forms in the slag treatment process is carried out multi-stage heat exchanger reclaims.
15. method for recovering waste heat from scoria as claimed in claim 14, it is characterized in that, comprise in the described steps A 2: at first pass through plate-type heat exchanger and solid slag contact heat-exchanging in the slag buffer memory storehouse, utilize this plate-type heat exchanger that solid slag heat energy is converted into the heat-storing device that high temperature heat is stored into the corresponding temperature grade; Auger heat exchange handling machinery by the plate-type heat exchanger bottom is delivered to fluid-bed heat exchanger and to the process of the equipment of mucking haulage, utilizes reverse cryogenic gas and the solid slag of sending into wherein to carry out the heat exchange processing in this auger heat exchange handling machinery and fluid-bed heat exchanger then.
16. method for recovering waste heat from scoria as claimed in claim 14, it is characterized in that, be communicated with described steam heat-exchanging system and solid slag heat-exchange system, to form the gas converting heat circulation path, and on the gas converting heat circulation path between the blast inlet of the tail gas outlet of described steam heat-exchanging system and described solid slag heat-exchange system, recirculation blower is set, utilize recirculated air that recirculation blower provides as heat-eliminating medium, carry out heat exchange with solid slag in the solid slag heat-exchange system.
17. method for recovering waste heat from scoria as claimed in claim 15, it is characterized in that, also be provided with tail gas heat exchanger between the tail gas outlet of described steam heat-exchanging system and fluid-bed heat exchanger blast inlet, after further heat exchange is lowered the temperature to the low temperature exhaust gas of steam heat-exchanging system, send into the solid slag heat-exchange system, and the water-in of this tail gas heat exchanger is connected to tank through a strainer, will provide through the water after the heating to dirt ash flushing pipe.
18. method for recovering waste heat from scoria as claimed in claim 10, it is characterized in that, described multistage thermal energy storage system comprises high pressure drum, middle pressure thermophore and three grades of heat-storing devices of low pressure bag, and in described each heat-storing device, the high pressure drum can make its temperature more stable relatively to middle pressure thermophore supply heat; On the other hand, the heat-storing device of low relatively one-level by other heat-exchanger rig of high one-level to other heat-storing device supplementary feed of high one-level.
19. method for recovering waste heat from scoria as claimed in claim 18 is characterized in that, described high pressure drum is pressed thermophore in being connected to by relief valve; Press thermophore to be connected to the low pressure bag in described, and newly mend cold soft water process vapor heat exchanger heat exchange, make the low pressure bag harvest heat, new water supply, deoxygenation function in one after this deoxygenator injects the low pressure bag by relief valve, deoxygenator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009102543389A CN101709339B (en) | 2009-12-11 | 2009-12-11 | System and method for recovering slag residual heat |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009102543389A CN101709339B (en) | 2009-12-11 | 2009-12-11 | System and method for recovering slag residual heat |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101709339A true CN101709339A (en) | 2010-05-19 |
| CN101709339B CN101709339B (en) | 2012-08-22 |
Family
ID=42402145
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009102543389A Active CN101709339B (en) | 2009-12-11 | 2009-12-11 | System and method for recovering slag residual heat |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101709339B (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101907405A (en) * | 2010-07-28 | 2010-12-08 | 鹤壁地恩地新材料科技有限公司 | Heat recovery device of magnesium smelting reducing slag |
| CN102221198A (en) * | 2010-08-19 | 2011-10-19 | 西安交通大学 | Low NOx combustion method for cyclone furnace and liquid state slagging and afterheat recycling system for cyclone furnace |
| CN103721494A (en) * | 2014-01-04 | 2014-04-16 | 扬州市刘氏化工有限公司 | Pneumatic slagging device |
| CN104087691A (en) * | 2014-07-23 | 2014-10-08 | 福建立信换热设备制造股份公司 | Process for recycling waste heat of slag flushing water vapor and dispersing fog and equipment adopted in same |
| CN105650884A (en) * | 2016-01-31 | 2016-06-08 | 江苏韩通船舶重工有限公司 | Water heating system for compressed natural gas vessel and working method thereof |
| CN105910448A (en) * | 2016-06-03 | 2016-08-31 | 中国重型机械研究院股份公司 | Combined type small particle semi-coke cooling and waste heat recycling device |
| CN107478067A (en) * | 2017-09-14 | 2017-12-15 | 思安新能源股份有限公司 | Heat recovery system |
| CN108302950A (en) * | 2018-03-16 | 2018-07-20 | 南京有荣节能科技有限公司 | A kind of afterheat of slags utilizes device |
| CN109124390A (en) * | 2018-07-17 | 2019-01-04 | 常州大学 | A kind of pump type heat thermal insulation carrier for food |
| CN112710157A (en) * | 2020-12-09 | 2021-04-27 | 清华大学山西清洁能源研究院 | Organic working medium Rankine cycle power generation system for waste heat of blast furnace slag flushing water |
| CN112781376A (en) * | 2021-01-08 | 2021-05-11 | 刘小丽 | Petrochemical heating furnace |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5594405A (en) * | 1979-01-11 | 1980-07-17 | Nippon Kagaku Gijutsu Kenkyusho:Kk | Waste heat recovery apparatus of slag |
| KR20030018157A (en) * | 2001-08-27 | 2003-03-06 | 재단법인 포항산업과학연구원 | System for High Temperature Waste Heat Recovery from Molten Slag in Cooling Process |
| CN1920380A (en) * | 2005-08-23 | 2007-02-28 | 东北大学 | Blast-furnace cement sensible heat recovery system and its production process |
| CN200955757Y (en) * | 2006-09-10 | 2007-10-03 | 马应成 | Furnace slag residual heat recovery device |
| CN201567338U (en) * | 2009-12-11 | 2010-09-01 | 中冶京诚工程技术有限公司 | Furnace slag waste heat recovery system |
-
2009
- 2009-12-11 CN CN2009102543389A patent/CN101709339B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5594405A (en) * | 1979-01-11 | 1980-07-17 | Nippon Kagaku Gijutsu Kenkyusho:Kk | Waste heat recovery apparatus of slag |
| KR20030018157A (en) * | 2001-08-27 | 2003-03-06 | 재단법인 포항산업과학연구원 | System for High Temperature Waste Heat Recovery from Molten Slag in Cooling Process |
| CN1920380A (en) * | 2005-08-23 | 2007-02-28 | 东北大学 | Blast-furnace cement sensible heat recovery system and its production process |
| CN200955757Y (en) * | 2006-09-10 | 2007-10-03 | 马应成 | Furnace slag residual heat recovery device |
| CN201567338U (en) * | 2009-12-11 | 2010-09-01 | 中冶京诚工程技术有限公司 | Furnace slag waste heat recovery system |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101907405A (en) * | 2010-07-28 | 2010-12-08 | 鹤壁地恩地新材料科技有限公司 | Heat recovery device of magnesium smelting reducing slag |
| CN102221198A (en) * | 2010-08-19 | 2011-10-19 | 西安交通大学 | Low NOx combustion method for cyclone furnace and liquid state slagging and afterheat recycling system for cyclone furnace |
| CN102221198B (en) * | 2010-08-19 | 2013-11-13 | 西安交通大学 | Low NOx combustion method for cyclone furnace and liquid state slagging and afterheat recycling system for cyclone furnace |
| CN103721494A (en) * | 2014-01-04 | 2014-04-16 | 扬州市刘氏化工有限公司 | Pneumatic slagging device |
| CN104087691A (en) * | 2014-07-23 | 2014-10-08 | 福建立信换热设备制造股份公司 | Process for recycling waste heat of slag flushing water vapor and dispersing fog and equipment adopted in same |
| CN104087691B (en) * | 2014-07-23 | 2016-01-13 | 福建立信换热设备制造股份公司 | The technique of washing slag water steam heat recovery and fog dispersal and the equipment adopted |
| CN105650884A (en) * | 2016-01-31 | 2016-06-08 | 江苏韩通船舶重工有限公司 | Water heating system for compressed natural gas vessel and working method thereof |
| CN105910448A (en) * | 2016-06-03 | 2016-08-31 | 中国重型机械研究院股份公司 | Combined type small particle semi-coke cooling and waste heat recycling device |
| CN107478067A (en) * | 2017-09-14 | 2017-12-15 | 思安新能源股份有限公司 | Heat recovery system |
| CN108302950A (en) * | 2018-03-16 | 2018-07-20 | 南京有荣节能科技有限公司 | A kind of afterheat of slags utilizes device |
| CN108302950B (en) * | 2018-03-16 | 2024-04-12 | 南京有荣节能科技有限公司 | Slag waste heat utilization device |
| CN109124390A (en) * | 2018-07-17 | 2019-01-04 | 常州大学 | A kind of pump type heat thermal insulation carrier for food |
| CN112710157A (en) * | 2020-12-09 | 2021-04-27 | 清华大学山西清洁能源研究院 | Organic working medium Rankine cycle power generation system for waste heat of blast furnace slag flushing water |
| CN112710157B (en) * | 2020-12-09 | 2022-11-25 | 清华大学山西清洁能源研究院 | Organic working medium Rankine cycle power generation system for waste heat of blast furnace slag flushing water |
| CN112781376A (en) * | 2021-01-08 | 2021-05-11 | 刘小丽 | Petrochemical heating furnace |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101709339B (en) | 2012-08-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101709339B (en) | System and method for recovering slag residual heat | |
| CN101709661B (en) | Waste heat generating system and generating method | |
| CN101736101B (en) | Semi-wet slag treatment waste heat recovery generating system and method | |
| CN201567338U (en) | Furnace slag waste heat recovery system | |
| CN201574792U (en) | Waste heat generation system | |
| CN101709338A (en) | Half-wet method slag processing system and method | |
| CN101344359B (en) | Sintered ring cold exhaust heat stepped recovery power generation system and technique | |
| CN105909330B (en) | A kind of flue gas waste heat recovery and smoke processing system based on Organic Rankine Cycle | |
| CN201561662U (en) | Semi-wet-method slag processing and waste heat recovery power-generating system | |
| CN208982172U (en) | A kind of three circulation integral coal gasification fuel cell generations of zero carbon emission | |
| CN103642956A (en) | Liquid state blast furnace slag granulation and multi-roller residual heat recovery system | |
| CN201670845U (en) | High temperature solid slag sensible heat recovery device | |
| CN201581088U (en) | Slag processing system with semi-wet method | |
| CN102776302A (en) | Liquid slag waste heat recovery device and method for recovering slag waste heat by utilizing same | |
| CN202647718U (en) | Supercritical clamminess heating machine set heat supply net drainage treating system | |
| CN113998751A (en) | System for desulfurization slurry flash distillation is carried hot water intaking | |
| CN205980316U (en) | Organic rankine cycle of absorption formula distributing type supply of cooling, heating and electrical powers system | |
| CN211650417U (en) | Desulfurization slurry cooling flue gas waste heat supply integrated system | |
| CN102003887B (en) | Sintering waste heat utilization system | |
| CN203116539U (en) | Constant-temperature compound cycle sintering flue gas waste heat recovery system | |
| CN101641145B (en) | System, apparatus and method for carbon dioxide sequestration | |
| CN115585440A (en) | Device and method for recycling waste heat of pyrite cinder | |
| CN106498102A (en) | Boiler steam/water circulating method residues processing technique | |
| CN115899716A (en) | Thermal power plant flue gas-sludge-solar energy comprehensive gradient utilization system and method | |
| CN108151358A (en) | Cool and thermal power carbon sequestration alliance multipotency stream Regional Energy station based on regenerative resource driving |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |