CN212560337U - Converter primary dry dedusting system for recycling ultra-clean coal gas - Google Patents
Converter primary dry dedusting system for recycling ultra-clean coal gas Download PDFInfo
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- CN212560337U CN212560337U CN202021172473.7U CN202021172473U CN212560337U CN 212560337 U CN212560337 U CN 212560337U CN 202021172473 U CN202021172473 U CN 202021172473U CN 212560337 U CN212560337 U CN 212560337U
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Abstract
The utility model relates to a converter primary dry dedusting system for recycling ultra-clean coal gas, which comprises a converter, an evaporative cooler and a deduster; the dust removal system also comprises a high-temperature phase change heat accumulator for stabilizing the temperature of the flue gas; a gas outlet of the converter is communicated with a gas inlet of the high-temperature phase change heat accumulator through a vaporization cooling flue; a gas outlet of the high-temperature phase change heat accumulator is communicated with a gas inlet of the evaporative cooler; the gas outlet of the evaporative cooler is communicated with the gas inlet of the dust remover; and a fan is arranged at a gas outlet of the dust remover. The utility model provides an improvement scheme for realizing the ultra-clean gas recovery, the ultra-low emission of flue gas, effectively eliminating the smoke plume problem and the reliable and stable operation of a converter primary dust removal system.
Description
Technical Field
The utility model belongs to the technical field of energy-saving equipment and environmental protection equipment, concretely relates to dry process dust pelletizing system once of converter of super clean coal gas recovery.
Background
In recent years, haze weather frequently appears in China, and the problem of air quality has attracted high attention of the whole society. The iron and steel industry, as a major consumer of industrial emissions, is increasingly subject to strict limits on emission standards and emissions.
The steel industry in China is in the period of structure adjustment and optimization upgrading, faces increasingly severe resource and environmental pressure, and has to go through resource-saving and environment-friendly sustainable development.
The converter steelmaking, which is the main steelmaking process of steel enterprises, generates gas containing carbon monoxide as a main component, a small amount of carbon dioxide and other trace components in the blowing process, and also carries a large amount of iron oxide, metal iron particles and other fine particle solid dust, thus seriously polluting the atmosphere and the workshop environment. Therefore, the technical level of the converter dust removal system is improved, and the recovery and utilization of converter gas and the recovery of flue gas waste heat have great significance for saving energy and reducing consumption in steelmaking, effectively controlling and reducing the emission of steelmaking atmospheric pollutants and reducing environmental pollution.
The temperature of the flue gas outlet of the converter is about 1400 ℃ to 1600 ℃, and the dust concentration is 70-200g/m3After leaving the furnace mouth, the flue gas is cooled to 800-. At present, the domestic converter primary flue gas dust removal process mainly comprises the traditional OG method, the new OG method, the semi-dry method, the dry method (LT method) and other dust removal processes.
1. Conventional OG systems.
In 1985, Baoshan iron and Steel works (hereinafter referred to as Baoshan first-stage 300t converter, the Japanese OG technology and equipment, so-called 3 rd generation OG technology, was introduced, the core of the process is a two-stage adjustable venturi throat, which mainly controls the micro-differential pressure of the converter mouth and the resistance loss of the throat in Erwen, and further continuously adjusts the resistance distribution of the system under the condition of continuously changing smoke quantity, thereby achieving the best purification effect.
Whole process mining of systemWith wet processing, this technique has the disadvantages of: firstly, the dust content of the treated coal gas is high and can not reach below 10mg/m3, and a wet electrostatic dust collector is required to be arranged at the rear part of the coal gas for fine dust removal so as to reduce the dust content mass concentration to be less than or equal to 10mg/m3(ii) a Secondly, secondary pollution exists in the system, and sewage needs to be treated; and the system has large resistance loss, so the energy consumption is high and the occupied area is large. With the improvement of national energy conservation and emission reduction requirements, the traditional OG dust removal system cannot meet the requirements.
It should be acknowledged that the introduction and localization of the converter OG technology have positive effects on improving the dust removal effect of converter flue gas and the coal gas recovery level in China and realizing negative energy steelmaking. However, with the increase of national energy saving and emission reduction requirements, the 3 rd generation OG system cannot meet the requirements.
2. Novel OG method.
In 1999, the technology is adopted for three-step steelmaking of the horse steel on a 50t converter. The technology carries out technical improvement on the traditional OG method, namely, a throat opening with two characters adjustable is changed into a circular seam washer, RSW for short, a throat opening with one character is also cancelled, and a saturator is replaced, namely, the OG method of the 4 th generation, or the novel OG method is called. The technology has the characteristics of simple flow, less unit equipment, small resistance loss and the like. The RSW technology is adopted, so that the dust removal efficiency is high, the control is easy, and the blockage is not easy.
The resistance of the spray tower is about 1kPa, the saved resistance is increased to the second place, the dust concentration is reduced, but the total circulating water quantity of the system is not reduced much; and the dust cleaning period of the fan impeller is not prolonged. In 2001, the technology is adopted by the division company of Bao Steel works in 150t converters, and a circular seam venturi is changed into an inverted type, so that the problems of uneven water distribution and system resistance distribution are solved, the discharge concentration is reduced, but the circulating water quantity is not reduced greatly.
3. Semi-dry process.
The semidry method (i.e. high-efficiency water-saving type tower-venturi dust-removing system) adopts single or several hollow semidry type high-efficiency spray cooling dust-removing towers to make cooling, i.e. adopts dry evaporation cooling technique, and is different from that the dust-removing still adopts spray dust-removing process, and the produced sewage still utilizes the water-flushing mode to treat. The system mainly comprises 3 parts: high-efficiency water-saving washing tower, upward circular seam long-diameter venturi tube and cyclone rotational flow plate spray composite dehydrator. The system is highly connected with the vaporization cooling flue through a nonmetal compensator or a novel overflow-free water seal, and the outlet of the system is connected with a smoke exhaust pipeline. The blower which is the same as the wet method is adopted, the pressure difference required by effective dust removal of the second file is ensured by rebalancing the system resistance, the resistance of other parts is reduced to the maximum extent, and the problems that the existing first file dust removal efficiency is not up to 95%, the maintenance amount of an overflow water seal is large, potential safety hazards are caused by water discharge with coal gas, the maintenance amount of equipment is large, the water treatment cost is high and the like are solved. Under the same pressure of the converter and the inlet and the outlet of the fan, the purposes of standard discharge and energy saving can be achieved.
The process has the advantages that: the system resistance is reduced, and the dust emission can be ensured to be less than or equal to 50mg/m3Or 1-2 kWh of electricity is saved per ton of steel; ② the circulating water amount is reduced by 50 percent; and the maintenance period of the fan is prolonged. But the technology still has secondary pollution and sewage treatment.
4. Dry process (LT process).
The dry converter gas purifying and recovering system developed by Lurgi Germany and Tisen steelworks in the end of the 20 th century and 60 th era mainly comprises three major parts, namely flue gas cooling, purifying and recovering and dust briquetting. High-temperature flue gas generated by the converter enters the evaporative cooler through the evaporative cooling flue, water and steam are mixed and sprayed out through the top water gun to form a mist shape, and the high-temperature flue gas is subjected to sufficient heat exchange in the advancing process to achieve the purpose of cooling the flue gas. The better the water atomization, the more sufficient the heat exchange. The flue gas is subjected to coarse dust removal in an evaporative cooler, and the temperature of the outlet flue gas can be controlled to be about 220 ℃. The flue gas after coarse dust removal enters a cylindrical electrostatic dust collector for further purification, so that the dust concentration of the flue gas is reduced to below 10mg/m 3. Then, the flue gas enters a gas cooler, the temperature can reach about 100 ℃, and the flue gas enters a gas chamber for recycling.
Compared with the wet method, the dry method has the following advantages: firstly, the dust removal efficiency is high, and the mass concentration of dust is reduced to below 10mg/m 3; the system has no secondary pollution and sewage treatment; the system has small resistance loss, high calorific value of gas and low energy consumption; the system is simplified, the occupied area is small, and the management and the maintenance are convenient; however, the following problems exist: firstly, the danger of gas explosion is high; secondly, the investment is high; consumption of steam and energy conservation. The evaporative cooling tower consumes a large amount of steam (such as 120t converter-5 t/h) during operation; and fourthly, the technical requirements on maintenance and operation are high.
The prior art has the following disadvantages:
under the situation that the global steel industry is vigorously conducting energy conservation and emission reduction, the converter gas dry dedusting technology is more and more concerned as an optimal feasible technology (BAT), and China brings the technology into the national key industry clean production technology guide catalog for key popularization.
Although the technology development of the converter primary flue gas dry dedusting process is mature so far, and the dust content of coal gas and the dust content of diffused flue gas can be completely reduced to a very low level, a series of major problems which cannot be solved exist from the viewpoint of modern science and technology:
1. the dry dedusting always has high danger of gas explosion, and the electrostatic deduster cannot avoid the problem of high-voltage flashover of an electric field, so that the explosion venting problem of the electrostatic deduster is caused. In the actual production and operation process of the converter primary flue gas dry electrostatic dust removal system, due to frequent explosion unloading problems and smoke generation problems, the converter primary flue gas dry electrostatic dust removal system can not always ensure stable and standard flue gas emission; meanwhile, the recovered gas requires a large amount of water washing to ensure cleanliness meeting requirements.
2. The dry dedusting system adopts an evaporative cooling mechanism, namely, the flue gas is cooled by water spray and steam, so that the flue gas contains a large amount of moisture, and the flue gas pipeline, the electrostatic precipitator polar plate and shell, the gas pipeline and the gas recovery equipment are corroded.
3. The diffused smoke contains a lot of water vapor, and the problem of smoke plume of the diffused smoke is prominent.
4. Because oxygen blowing smelting is not continuous in the converter steelmaking process, if a purifying and filtering device of a converter primary dust removal system adopts a pulse-blowing high-temperature-resistant ceramic fiber filter tube type dust remover, the purifying and filtering device is always in a working state of heating and cooling alternate circulation and is subjected to great alternating thermal stress. The pulse-injection high-temperature-resistant ceramic fiber filter tube type dust remover has short service life and large daily maintenance and repair workload under the action of alternating thermal stress, and also has great influence on converter steelmaking production to a certain extent.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects of the prior art, the utility model discloses a one-time dry dedusting system of a converter for recycling ultra-clean coal gas. The utility model discloses a based on the problem that exists based on dry process dust removal technology, for realizing that the super clean coal gas of a dust pelletizing system of converter is retrieved, the flue gas is minimum to be discharged, effectively eliminate the plume problem and reliable steady operation, the improvement scheme that specially proposes.
The utility model discloses the technical scheme who adopts as follows:
a converter primary dry dedusting system for recycling ultra-clean coal gas comprises a converter, an evaporative cooler and a deduster; the dust removal system also comprises a high-temperature phase change heat accumulator for stabilizing the temperature of the flue gas; a gas outlet of the converter is communicated with a gas inlet of the high-temperature phase change heat accumulator through a vaporization cooling flue; a gas outlet of the high-temperature phase change heat accumulator is communicated with a gas inlet of the evaporative cooler; the gas outlet of the evaporative cooler is communicated with the gas inlet of the dust remover; and a fan is arranged at a gas outlet of the dust remover.
The dust remover comprises a middle box body, an upper box body and a pattern plate arranged between the middle box body and the upper box body; the pattern plate is provided with a plurality of holes penetrating through the pattern plate; a plurality of filtering components are fixed below the flower plate; the positions of the filter parts correspond to the positions of the holes of the pattern plate one by one; a blowing ash removal pipe is arranged in the upper box body; the blowing ash removal pipe comprises a plurality of nozzles; the positions of the nozzles correspond to the positions of the holes of the pattern plate one by one.
The further technical proposal is that the dust remover comprises an explosion-proof structure; the explosion-proof structure comprises a swash plate type structure and/or an explosion relief valve; the inclined plate type structure is arranged in a corner area where a flower plate of the dust remover is connected with a cylinder of the dust remover; the explosion venting valve is arranged at the top end of the upper box body.
The further technical proposal is that an ash bucket is arranged below the evaporative cooler; an ash hopper is arranged below the middle box body of the dust remover; a compressed inert gas blowing device is arranged at the bottom of the ash bucket of the evaporative cooler and/or the ash bucket of the dust remover; the compressed inert gas blowing device comprises a blowing pipe communicated with an inert gas source and a gas source valve used for controlling gas sprayed out by the blowing pipe; the blowing pipe faces the upper part of the ash hopper.
The further technical proposal is that the dust removing system is also provided with a plurality of pneumatic ash conveying and sending devices; the evaporative cooler, the high-temperature phase change heat accumulator and the dust remover are all provided with ash hoppers; the bin pump of the pneumatic ash conveying and sending device is arranged at the discharge opening of the ash hopper; a compressed gas source inlet of the pneumatic ash conveying and sending device is communicated with an inert gas source; the ash spraying outlet of the pneumatic ash conveying and sending device is communicated with an ash warehouse; a bin pump heat tracing and heat insulating device is arranged in the bin pump of the pneumatic ash conveying and sending device.
The further technical proposal is that the dust removing system also comprises an inert gas heating device; and the inert gas source is output after being preheated by the inert gas heating device.
The further technical proposal is that the dust removal system also comprises a flue gas purification device; the gas outlet of the dust remover is communicated with the gas inlet of the flue gas purification device; and a fan is arranged at a gas outlet of the flue gas purification device.
The further technical scheme is that an emergency inert gas blowing and compressing device is arranged below an ash bucket of the high-temperature phase change heat accumulator; the emergency inert gas blowing and compressing device comprises a blowing pipe communicated with an inert gas source and a gas source valve used for controlling gas sprayed out by the blowing pipe.
The utility model has the advantages as follows:
1. original method in primary dry dedusting system adopting pulse-blowing high-temperature-resistant ceramic fiber filter tube type deduster to replace converterThe electrostatic precipitator thoroughly eliminates the situation that the prior electrostatic precipitator can not avoid the occurrence of the explosion venting of the complex electricity, thereby realizing the stable and reliable recovery of ultra-clean coal gas and the discharge of flue gas with ultra-low dust content in a primary dust removal system of the converter, and the dust content of the recovered coal gas and the discharged flue gas is less than or equal to 5mg/Nm3。
2. Compared with the prior art, the high-temperature phase-change type heat accumulator is additionally arranged, the thermal shock influence of a pulse-injection high-temperature-resistant ceramic fiber filter tube type dust remover adopted by a converter primary dust removal system produced by a converter is effectively avoided, the stable and reliable operation of the system is ensured, the service life of the pulse-injection high-temperature-resistant ceramic fiber filter tube type dust remover is prolonged to the greatest extent, and the maintenance and repair workload is reduced.
3. A flue gas purification device for eliminating smoke plume is arranged between a smoke outlet of the pulse-jet high-temperature-resistant ceramic fiber filter tube type dust remover and a fan, and is used for eliminating water vapor contained in flue gas and further reducing the temperature of the flue gas, reducing the corrosivity of recovered coal gas on pipelines and equipment, and effectively eliminating the smoke plume problem of diffused flue gas.
Drawings
Fig. 1 is a schematic diagram of a system structure according to an embodiment of the present invention.
Fig. 2 is an enlarged schematic view of the precipitator of fig. 1.
In the figure: 1. a converter; 2. movable smoke hood and hood skirt structure; 3. a vaporizing cooling flue; 4. a high-temperature phase change heat accumulator; 5. a temperature transmitter; 6. flue gas containing O2A quantity measuring device; 7. flue gas containing H2A quantity measuring device; 8. A device for measuring the CO content in the flue gas; 9. a pressure transmitter; 10. an evaporative cooler; 11. a flue gas duct; 12. A dust remover; 13. an explosion venting valve; 14. a differential pressure transmitter; 15. a flue gas purification device; 16. a fan; 17. switching stations; 18. an automated control device; 19. a flue gas diffusing chimney; 20. ultra-clean gas pipelines; 21. a condensed water discharge port; 22. a heat tracing and heat preserving device of the bin pump; 23. a dust spraying outlet; 24. a pneumatic ash conveying and sending device; 25. A compressed inert gas purging device; 26. an inert gas conduit; 27. an emergency inert gas blowing and compressing device; 28. an inert gas heating device; 29. inert gas source。
Detailed Description
The following describes embodiments of the present invention with reference to the drawings.
Fig. 1 is a schematic diagram of a system structure according to an embodiment of the present invention. As shown in fig. 1, the dust removal system includes a converter 1, an evaporative cooler 10, and a dust remover 12.
A high-temperature phase change heat accumulator 4 for stabilizing the temperature of flue gas is additionally arranged in front of an evaporative cooler 10 of the dust removal system. Under the oxygen blowing smelting working state and the non-oxygen blowing smelting working state of the converter 1, the high-temperature phase change heat accumulator 4 can stabilize the temperature of the gas discharged by the converter 1 within a small variation range.
And a gas outlet of the converter 1 is communicated with a gas inlet of the high-temperature phase change heat accumulator 4. Specifically, a circle of movable smoke hood and cover skirt structure 2 is arranged around the gas outlet of the converter 1. One end of the vaporization cooling flue 3 is communicated with a gas outlet of the converter 1, and the other end of the vaporization cooling flue 3 is communicated with a gas inlet of the high-temperature phase change heat accumulator 4.
An emergency blowing compressed inert gas device 27 is arranged below an ash bucket of the high-temperature phase change heat accumulator 4. The emergency blowing compressed inert gas device 27 includes a blowing tube that can be blown with inert gas and a blowing valve for controlling the blowing tube. And the outlet of the injection pipe is positioned inside the high-temperature phase change heat accumulator 4. The blowing pipe of the emergency blowing compressed inert gas device 27 is communicated with an inert gas source 29 through an inert gas pipeline 26.
And a gas outlet of the high-temperature phase change heat accumulator 4 is communicated with a gas inlet of the evaporative cooler 10.
A temperature transmitter 5 and a flue gas containing O are arranged on a pipeline between the high-temperature phase change heat accumulator 4 and the evaporative cooler 102Quantity measuring device 6, flue gas contain H2A quantity measuring device 7, a flue gas CO content measuring device 8 and a pressure transmitter 9. The automation control device 18 reads the temperature transmitter 5 and the flue gas contains O2Quantity measuring device 6, flue gas contain H2The measurement data of the quantity measuring device 7, the flue gas CO content measuring device 8 and the pressure transmitter 9 are started when the working condition is abnormal according to the measured process parameters and the system automatic control programAnd the injection valve of the emergency injection and compression inert gas device 27 injects inert gas into the high-temperature phase change heat accumulator 4 and the pipeline between the high-temperature phase change heat accumulator 4 and the evaporative cooler 10, so as to avoid the explosion of the flue gas.
A compressed inert gas blowing device 25 is installed below the ash hopper of the evaporative cooler 10. The compressed inert gas purging device 25 includes an injection tube that can be injected with inert gas and a gas source valve for controlling the injection tube. The blowing pipe is located at the bottom of the ash hopper of the evaporative cooler 10, and the blowing pipe is arranged upwards. The blowing pipe of the compressed inert gas purging device 25 is communicated with an inert gas source 29 through an inert gas pipeline 26.
The gas outlet of the evaporative cooler 10 communicates with the gas inlet of the precipitator 12 via a flue gas duct 11. Because the high-temperature phase change heat accumulator 4 is additionally arranged in front of the evaporative cooler 10, the temperature of the flue gas fed into the dust remover 12 can be stabilized within a small variation range, so that the problem of thermal expansion and cold contraction of the dust remover 12 caused by rapid cooling and rapid heating in the intermittent production of the steelmaking converter 1 is solved, the service life of the dust remover 12 is prolonged, the system is ensured to stably and reliably filter the primary flue gas of the converter 1 in a fine mode, and ultra-clean coal gas and ultra-low emission flue gas are reliably and stably recovered.
Preferably, the dust collector 12 is a pulse-jet high-temperature-resistant ceramic fiber filter tube type dust collector. The primary flue gas of the converter 1 is filtered by selecting the pulse-jet high-temperature-resistant ceramic fiber filter tube type dust remover, so that the explosion venting problem caused by the unavoidable electricity leakage in the prior art can be thoroughly solved, the primary flue gas of the converter 1 can be reliably and stably purified effectively and finely, and the recovery of ultra-clean coal gas and the discharge of ultra-low dust-containing flue gas (namely the dust contents of the recovered coal gas and the discharged flue gas are less than or equal to 5 mg/Nm)3)。
To ensure safe operation, the precipitator 12 includes an explosion-proof construction. The explosion-proof structure comprises a swash plate type structure and/or an explosion relief valve 13, and the swash plate type structure and the explosion relief valve 13 are preferably installed together. The ramp type structure is installed at a corner region where the flower plate of the dust catcher 12 and the cylinder of the dust catcher 12 are connected, for eliminating a dead angle.
Fig. 2 is an enlarged schematic view of the precipitator of fig. 1. As shown in fig. 2, the dust collector 12 in the present embodiment includes a middle case, an upper case, and a pattern plate provided between the middle case and the upper case. The top end of the upper box body is provided with an explosion venting valve 13.
The flower plate is provided with a plurality of holes penetrating through the flower plate. A plurality of filter elements are fixed below the pattern plate. The positions of the filter components correspond to the positions of the holes of the pattern plate one by one. The filter member may be a filter bag or a filter cartridge. Specifically, the upper end part of each filter component is opened, the lower end part of each filter component is sealed, the upper end part of each filter component is fixed at the position of a hole above the flower plate, and the contact and fixation part of each filter component and the flower plate is a sealing structure.
A blowing ash removal pipe is arranged in the upper box body. The blow ash removal tube includes a plurality of nozzles. The positions of the nozzles correspond to the positions of the holes of the pattern plate one by one. The gas inlet of the blowing ash pipe is communicated with an inert gas pipeline 26. An inert gas source 29 is delivered to the lance tube through inert gas line 26.
The lower part of the middle box body is provided with an ash hopper with a funnel-shaped structure. A compressed inert gas purging device 25 is mounted at the bottom end of the funnel-shaped structure. The compressed inert gas purging device 25 includes an injection tube that can be injected with inert gas and a gas source valve for controlling the injection tube. The blowing pipe is located above the discharge opening of the ash hopper of the dust separator 12. Preferably, the blowing pipes are provided in plural, and the nozzles of the plural blowing pipes are inclined upward and are all arranged toward the center of the dust hopper of the dust collector 12. The injection tube is in communication with an inert gas source 29 through an inert gas conduit 26.
A differential pressure transmitter 14 is installed between the gas outlet of the dust separator 12 and the gas outlet.
The dust removal system also comprises a flue gas cleaning device 15. The gas outlet of the dust collector 12 is communicated with the gas inlet of the flue gas purification device 15 through the flue gas pipeline 11. The gas outlet of the flue gas cleaning device 15 is provided with a fan 16. The flue gas purification device 15 is used for eliminating water vapor contained in flue gas, further reducing the temperature of the flue gas, reducing the corrosivity of recovered coal gas on pipelines and equipment, and effectively eliminating the smoke plume problem of the diffused flue gas. The bottom of the flue gas cleaning device 15 is provided with a condensed water outlet 21.
The fan 16 delivers the fumes to a switching station 17. The switching station 17 discharges the flue gas which does not reach the purification degree of the ultra-clean gas through the flue gas emission chimney 19, and sends the ultra-clean gas to the gas chamber through the ultra-clean gas pipeline 20.
Further, the dust removing system is also provided with a plurality of pneumatic ash conveying and sending devices 24. The structures of the evaporative cooler 10, the high-temperature phase change heat accumulator 4, the dust remover 12 and the like are all provided with ash hoppers. The pneumatic ash conveying and sending device 24 is arranged below each ash bucket. The bin pump of the pneumatic ash conveying and sending device 24 is arranged at the discharge opening of the ash bucket. The inlet of the compressed air source of the pneumatic ash conveying and sending device 24 is communicated with an inert gas pipeline 26.
Preferably, a bin pump heat tracing and heat preserving device 22 is arranged in the bin pump of the pneumatic ash conveying and sending device 24. Specifically, the heat tracing and preserving device 22 of the bin pump can be a heating wire for heating the inert gas.
Preferably, the system is also provided with an inert gas heating device 28. The inert gas source 29 enters the inert gas pipeline 26 after being preheated by the inert gas heating device 28, and is conveyed to each pneumatic ash conveying and sending device 24 or the emergency compressed inert gas blowing device 27 and the compressed inert gas blowing device 25. The inert gas heating device 28 and the cabin pump heat tracing and heat preserving device 22 are used for preventing the unstable operation of the system caused by the condensation of the inert gas in the operation process of the system.
The utility model discloses a working method of a converter one-time dry dedusting system for ultra-clean recovery of coal gas, which comprises the following steps:
step 1, the converter 1 is in an intermittent working state, and the discharged flue gas is conveyed to a high-temperature phase change heat accumulator 4 through a vaporization cooling flue 3. In the oxygen blowing smelting working state of the converter 1, the temperature T1 of the flue gas discharged by the converter 1 is 1450-1650 ℃.
Step 2, cooling the flue gas discharged by the converter 1 by the high-temperature phase change heat accumulator 4, so that the temperature of the converter 1 is stable in the change process of the oxygen blowing smelting working state and the non-oxygen blowing smelting working state; the high-temperature phase change heat accumulator 4 conveys the treated flue gas to an evaporative cooler 10. The temperature T2 of the gas after being processed by the high-temperature phase-change heat accumulator 4 is 800-1000 ℃.
In the process of transmitting the flue gas from the high-temperature phase change heat accumulator 4 to the evaporative cooler 10, the temperature transmitter 5 and the flue gas containing O are arranged on the pipeline between the high-temperature phase change heat accumulator 4 and the evaporative cooler 102Quantity measuring device 6, flue gas contain H2The quantity measuring device 7, the flue gas CO content measuring device 8 and the pressure transmitter 9 measure and monitor the flue gas in the pipeline between the high-temperature phase change heat accumulator 4 and the evaporative cooler 10. When the working state is abnormal, a blowing valve of the device 27 for blowing and compressing the inert gas in an emergency mode is opened, and the inert gas is blown into the high-temperature phase change heat accumulator 4 and the pipeline between the high-temperature phase change heat accumulator 4 and the evaporative cooler 10, so that the smoke is prevented from exploding.
And 3, further cooling the flue gas by the evaporative cooler 10, wherein the temperature T4 of the flue gas treated by the evaporative cooler 10 is 320-350 ℃. The evaporative cooler 10 then delivers the treated flue gas to a pulse-jet refractory ceramic fiber filter tube precipitator 12. The material which is cooled down to solid particles by the flue gas after being treated by the evaporative cooler 10 falls into the ash hopper of the evaporative cooler 10.
The inside coil pipe that is provided with of evaporative cooler 10, the coil pipe outside has spray set, and the flue gas gets into evaporative cooler 10, carries out the heat transfer with the refrigerant in the coil pipe and cools down.
And 4, filtering the flue gas by using a pulse-jet high-temperature-resistant ceramic fiber filter tube type dust remover 12, wherein gas substances pass through the pattern plate after being filtered by a filter part, and enter a gas outlet of the upper box body to enter a flue gas purification device 15. The solid particles fall into the ash hopper of the precipitator 12.
The temperature T6 of the flue gas treated by the pulse-jet high-temperature-resistant ceramic fiber filter tube type dust collector 12 is 300-.
Step 5, the flue gas purification device 15 further eliminates water vapor contained in the flue gas, reduces the gas temperature and effectively eliminates the problem of smoke plume of the diffused flue gas; the flue gas purification device 15 generally comprises a cooling phase-change coalescer, a flue demister, a warmer and the like, and can eliminate white smoke plume in flue gas. The temperature T7 of the flue gas treated by the flue gas purification device 15 is not more than 45-55 ℃.
Step 6, blowing the gas and the smoke conveyed by the smoke purification device 15 to a switching station 17 by a fan 16; the switching station 17 discharges the flue gas through a flue gas emission chimney 19, and sends the ultra-clean coal gas to a coal gas cabinet through an ultra-clean coal gas pipeline 20.
In the above steps 1 to 6, the inert gas source 29 is heated by the compressed inert gas heating device 28, enters the inert gas pipeline 26, and is conveyed to each pneumatic ash conveying and sending device 24 or the emergency compressed inert gas blowing device 27 and the compressed inert gas blowing device 25.
In this context, compressed nitrogen is generally used as inert gas. Other inert gases of similar nature may be used.
In the text, the high-temperature phase-change heat accumulator, the evaporative cooler, the flue gas purification device, the fan, the switching station, the temperature transmitter and the flue gas contain O2Quantity measuring device and flue gas containing H2The quantity measuring device, the flue gas CO content measuring device, the pressure transmitter and the like are common prior art, the structure of the prior art is not improved, and the commercially available products and the like can be directly used.
The above description is for the purpose of explanation and not limitation of the invention, which is defined in the claims, and any modifications may be made without departing from the basic structure of the invention.
Claims (8)
1. A converter primary dry dedusting system for recycling ultra-clean coal gas comprises a converter (1), an evaporative cooler (10) and a deduster (12); the method is characterized in that: the dust removal system also comprises a high-temperature phase change heat accumulator (4) for stabilizing the temperature of the flue gas; a gas outlet of the converter (1) is communicated with a gas inlet of the high-temperature phase change heat accumulator (4) through a vaporization cooling flue (3); a gas outlet of the high-temperature phase change heat accumulator (4) is communicated with a gas inlet of the evaporative cooler (10); the gas outlet of the evaporative cooler (10) is communicated with the gas inlet of the dust remover (12); and a fan (16) is arranged at the gas outlet of the dust remover (12).
2. The converter primary dry dedusting system for ultra-clean gas recovery according to claim 1, wherein the deduster (12) comprises a middle box body, an upper box body and a flower plate arranged between the middle box body and the upper box body; the pattern plate is provided with a plurality of holes penetrating through the pattern plate; a plurality of filtering components are fixed below the flower plate; the positions of the filter parts correspond to the positions of the holes of the pattern plate one by one; a blowing ash removal pipe is arranged in the upper box body; the blowing ash removal pipe comprises a plurality of nozzles; the positions of the nozzles correspond to the positions of the holes of the pattern plate one by one.
3. The converter primary dry dedusting system for ultra-clean gas recovery as recited in claim 2, wherein the deduster (12) includes an explosion-proof structure; the explosion-proof structure comprises a swash plate type structure and/or an explosion relief valve (13); the inclined plate type structure is arranged in the corner area where the pattern plate of the dust remover (12) is connected with the cylinder of the dust remover (12); and the explosion venting valve (13) is arranged at the top end of the upper box body.
4. The converter primary dry dedusting system for ultra-clean gas recovery according to claim 1, wherein an ash hopper is installed below the evaporative cooler (10); an ash hopper is arranged below the middle box body of the dust remover (12); a compressed inert gas blowing device (25) is arranged at the bottom of the ash bucket of the evaporative cooler (10) and/or the ash bucket of the dust remover (12); the compressed inert gas blowing device (25) comprises a blowing pipe communicated with an inert gas source (29) and a gas source valve used for controlling gas sprayed out of the blowing pipe; the blowing pipe faces the upper part of the ash hopper.
5. The converter primary dry dedusting system for ultra-clean gas recovery according to claim 1, wherein the dedusting system is further provided with a plurality of pneumatic ash conveying and sending devices (24); the evaporative cooler (10), the high-temperature phase change heat accumulator (4) and the dust remover (12) are all provided with ash hoppers; a bin pump of the pneumatic ash conveying and sending device (24) is arranged at a discharge opening of the ash hopper; the inlet of a compressed gas source of the pneumatic ash conveying and sending device (24) is communicated with an inert gas source (29); an ash spraying outlet (23) of the pneumatic ash conveying and sending device (24) is communicated with an ash warehouse; a bin pump heat tracing and heat insulating device (22) is arranged in the bin pump of the pneumatic ash conveying and sending device (24).
6. The converter primary dry dedusting system for ultra-clean gas recovery according to claim 4 or 5, further comprising an inert gas heating device (28); the inert gas source (29) is output after being preheated by the inert gas heating device (28).
7. The converter primary dry dedusting system for ultra-clean gas recovery according to claim 1, further comprising a flue gas cleaning device (15); the gas outlet of the dust remover (12) is communicated with the gas inlet of the flue gas purification device (15); and a fan (16) is arranged at a gas outlet of the flue gas purification device (15).
8. The converter primary dry dedusting system for ultra-clean gas recovery according to claim 1, characterized in that an emergency compressed inert gas injection device (27) is installed below an ash hopper of the high-temperature phase change heat accumulator (4); the emergency blowing compressed inert gas device (27) comprises a blowing pipe communicated with an inert gas source (29) and a gas source valve used for controlling gas sprayed out of the blowing pipe.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021172473.7U CN212560337U (en) | 2020-06-22 | 2020-06-22 | Converter primary dry dedusting system for recycling ultra-clean coal gas |
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| CN202021172473.7U CN212560337U (en) | 2020-06-22 | 2020-06-22 | Converter primary dry dedusting system for recycling ultra-clean coal gas |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111575435A (en) * | 2020-06-22 | 2020-08-25 | 无锡红旗除尘设备有限公司 | Converter primary dry dedusting system and method for recycling ultra-clean coal gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111575435A (en) * | 2020-06-22 | 2020-08-25 | 无锡红旗除尘设备有限公司 | Converter primary dry dedusting system and method for recycling ultra-clean coal gas |
| CN111575435B (en) * | 2020-06-22 | 2023-11-03 | 无锡红旗除尘设备有限公司 | Primary dry dedusting system and method for ultra-clean gas recovery converter |
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