CN212504610U - Device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas - Google Patents
Device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas Download PDFInfo
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- CN212504610U CN212504610U CN202021746223.XU CN202021746223U CN212504610U CN 212504610 U CN212504610 U CN 212504610U CN 202021746223 U CN202021746223 U CN 202021746223U CN 212504610 U CN212504610 U CN 212504610U
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Abstract
The utility model relates to a light-burned magnesia production technology field, in particular to a device for preparing light-burned magnesia and enriching carbon dioxide by flue gas self-circulation pyrolysis. The gas path of the feeding drying device is sequentially connected with a primary preheating cyclone device, a multi-stage recovery device and a multi-stage preheating device and then returns to the flash dryer, and the material path of the feeding drying device is connected to a bin through the multi-stage preheating device, the jet pulse type entrained flow bed calcining furnace, the multi-stage recovery device, a transition bin and a heat exchanger; one end of the gas circuit of the heat exchanger is connected with the fan, and the other end of the gas circuit of the heat exchanger is heatedIs connected with a jet pulse type entrained flow bed calcining furnace. The utility model reasonably utilizes the generated CO2Residual heat of gas and product, drying and preheating material, and CO2The preheating of the gas provides heat, so that the fuel consumption of the heat accumulating type hot blast stove is greatly reduced; by CO2The self-circulation pyrolysis method for preparing the light-burned magnesium oxide not only ensures the reasonable operation of the production flow, but also reduces CO2Can enrich CO generated by magnesite pyrolysis2A gas.
Description
Technical Field
The utility model relates to the field of light-burned magnesia production process, in particular to a method for producing CO by using light-burned magnesia2Performing self-circulation pyrolysis of magnesite and CO2A device for recycling.
Background
The magnesite resources in China are rich, the total storage capacity is about 50 hundred million tons, and the magnesite occupies the second place in the world. The Liaoning magnesite is the most abundant, and accounts for 86.5% of the whole country. The magnesite in China has the main characteristics that: the method has the advantages of dense reserves, more large mineral deposits, shallow burial, easy open-pit mining, high grade and high industrial utilization value. In general, magnesite is an important strategic resource in China.
At present, the main production method of light-burned magnesia in China is to calcine magnesite at 700-1000 ℃, and the used calcining equipment mainly comprises a shaft kiln, a rotary kiln, a rotational flow dynamic calcining calciner and the like. However, regardless of the type of furnace, most of the prior furnaces calcine magnesite by using flue gas generated by burning fuel, a large amount of burning flue gas is generated in the production process, and a certain amount of CO is generated by calcining and decomposing the magnesite2A gas. Theoretically 1.1 tonnes of CO will be produced per 1 tonne of magnesium oxide produced2A gas. For CO generated in the process of calcination2The treatment of (2) is always a key problem in the production process of producing the magnesium oxide by calcining. If the direct discharge is carried out, the greenhouse effect is caused, and the environment is damaged. And in the traditional calcination method, CO in the discharged flue gas2Gas only accounts for 15%, CO is difficult to be removed2Collecting the gas for resource utilization.
The utility model discloses a CO that produces among the calcination process2Self-circulation is carried out to pyrolyze magnesite, no burner is arranged in the calcining kiln, and CO except for pyrolysis can be used2Other than the remaining part of CO2The gas is collected for other industrial purposes, and is used for reducing CO in the process of producing light-burned magnesium oxide2And (4) a method for discharging.
Patent CN106007415A published in 26.04.2017 describes a complete set of device for preparing high-activity light-burned magnesia in a suspension flash manner, which adopts the technical scheme that magnesite powdery materials are fed into a Venturi mixer by a feeding machine, then the magnesite powdery materials enter a material multistage cyclone preheating device for multistage preheating, the last stage of preheated materials enter a suspension roasting furnace for flash decomposition, then the last stage of preheated materials enter a gas-material separation device for gas-material separation, the separated materials enter a material multistage cyclone cooling device for multistage cooling, and the last stage of cooled materials are discharged; the air flow direction is opposite to that of the air flow direction, and finally the waste gas cooled by the material multi-stage cyclone preheating device enters the waste gas treatment device for treatment and discharge. The method can realize CO2The waste heat is utilized and the suspension dynamic calcining technology is adopted, but the invention adopts the flue gas generated by fuel combustion to calcine the magnesite, the fuel consumption is large, and CO generated in the production process2The gas and the combustion flue gas are discharged after being treated, and no CO is generated2The gas resource utilization also causes certain damage to the environment.
Patent CN101372333A published on 25.02.2009 describes a method and a device for producing carbon dioxide by thermal decomposition of carbonate, and the technical proposal is to utilize CO generated by decomposition of carbonate2As a carrier, and the lime mud is heated outside the kiln body and then returns to the closed lime kiln to be heated and decomposed. The method can realize CO2Pyrolysis of carbonates, but without CO produced by calcination2The raw material is preheated and calcined, so that the decomposition time of the raw material is long, the fuel consumption in a heat accumulator is high, the emission of combustion products is high, the environment is damaged, and the production of products is not economical.
Patent CN106892578A published on 27.06.2017 describes a total recovery of CO2The technical scheme of the lime kiln device is that CO is utilized2Calcining mineral aggregate by hot air and heating CO by using regenerative heating furnace2Industrial lime production plant, CO produced in lime production2Is totally recovered. The process is carried out by CO2Calcination of mineral aggregates with hot air and recovery of CO2However, the invention only uses the dust removal device in the lime kiln to separate the gas and the products in the kiln, the separation rate is low, and the gas is difficult to separateThe solids were completely separated.
In the prior art, carbon dioxide generated in the calcining process is utilized, but the utilization efficiency is low, so that the energy consumption is relatively high, the separation efficiency is low, and the purposes of improving the efficiency and saving resources are not achieved.
SUMMERY OF THE UTILITY MODEL
Utility model purpose:
the utility model aims to solve the problem that CO can not be reasonably, efficiently and energy-efficiently utilized in the production process2And the resource provides a device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas.
The technical scheme is as follows:
the device comprises a device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas, wherein a gas path of a loading drying device is sequentially connected with a primary preheating cyclone device, a multi-stage recovery device and a multi-stage preheating device and then returns to a flash evaporation dryer, and a material path of the loading drying device passes through the multi-stage preheating device, a jet pulse type entrained flow bed calcining furnace, the multi-stage recovery device, a transition bin and a heat exchanger to the bin; one end of the gas circuit of the heat exchanger is connected with the fan, and the other end of the gas circuit of the heat exchanger is connected with the jet pulse type entrained flow bed calcining furnace through the heating device.
Further, a feeding machine of the feeding drying device is communicated with the flash dryer, and the flash dryer is communicated with a first-stage preheating cyclone device of the multi-stage preheating device.
Further, a gas path pipeline of the multi-stage preheating device sequentially passes through a three-stage preheating cyclone device, a two-stage preheating cyclone device, a flash evaporation dryer and a one-stage preheating cyclone device; a material path pipeline in the multi-stage preheating device sequentially passes through the primary preheating cyclone device, the secondary preheating cyclone device and the tertiary preheating cyclone device.
Further, a gas material pipeline of the flash dryer is sequentially connected with a first material pipeline of a first-stage preheating cyclone device, a second material pipeline of a second-stage preheating cyclone device and a third material pipeline of a third-stage preheating cyclone device of the multi-stage preheating device; a third material pipeline of the third-stage preheating cyclone device is connected with a feeding port of the jet pulse type entrained flow bed calcining furnace; the gas path in the multi-stage preheating device returns to the primary preheating cyclone device through a third gas outlet pipeline of the three-stage preheating cyclone device, a second gas outlet pipeline of the secondary preheating cyclone device and a gas material pipeline of the flash dryer in sequence; a first air outlet pipeline of the primary preheating cyclone device is sequentially connected with the bag-type dust collector and the dehumidifying device; the powder outlet of the bag-type dust collector is communicated with the feeding port of the primary preheating cyclone device.
Further, gas pipelines in the multistage recovery device sequentially pass through the primary recovery cyclone device, the secondary recovery cyclone device and the tertiary recovery cyclone device, and material path pipelines in the multistage recovery device are respectively connected with the transition bin.
Further, a gas-solid mixing feed inlet of the primary recovery cyclone device is communicated with a mixing outlet of the jet flow pulse type entrained flow calciner, a gas pipeline in the multi-stage recovery device sequentially passes through a fourth gas outlet pipeline of the primary recovery cyclone device, a fifth gas outlet pipeline of the secondary recovery cyclone device and a sixth gas outlet pipeline of the tertiary recovery cyclone device, and the sixth gas outlet pipeline of the recovery cyclone device is connected with the tertiary preheating cyclone device; a first magnesium oxide discharge port of the first-stage recovery cyclone device, a second magnesium oxide discharge port of the second-stage recovery cyclone device and a third magnesium oxide discharge port of the third-stage recovery cyclone device are connected with the transition bin.
Furthermore, a heat accumulating type hot blast stove of the heating device is connected with a flue gas treatment device, the flue gas treatment device is respectively connected with a chimney and an air and flue gas mixing chamber, a temperature regulating chamber is arranged behind the heat accumulating type hot blast stove, one end of a heating air outlet pipe is communicated with the temperature regulating chamber, and an air outlet of the temperature regulating chamber is connected with an air inlet of the jet pulse type entrained flow bed calcining furnace.
Furthermore, the heat accumulating type hot blast stove consists of three top combustion type heat accumulating type hot blast stoves, and the top combustion type heat accumulating type hot blast stoves are respectively connected with natural gas and air; a heating air inlet pipeline of the heating device is respectively connected with the heat accumulating type hot blast stove and the temperature regulating chamber provided with a fourth flow regulating valve, and a third flow regulating valve is arranged on a carbon dioxide gas pipeline communicated between the heat accumulating type hot blast stove and the temperature regulating chamber; and a fifth flow regulating valve is arranged on a flue gas pipeline between the flue gas treatment device and the air flue gas mixing part.
Furthermore, the furnace type adopted by the jet pulse type entrained flow bed calcining furnace is an inverted U shape, the furnace body is provided with a feeding port, an air inlet and a mixing outlet, one side of the feeding port and the air inlet is a main furnace of the jet pulse type entrained flow bed calcining furnace, one side of the mixing outlet is an auxiliary furnace of the jet pulse type entrained flow bed calcining furnace, the main furnace and the auxiliary furnace are communicated above, and the jet pulse part of the main furnace adopts a dumbbell-like structure; the main furnace below is the main furnace efflux section, and the top of main furnace efflux section is the main furnace pulse section, and main furnace efflux section and main furnace pulse section communicate, and the choke department of the main furnace efflux section on the main furnace sets up two relative pan feeding mouths in position, and the income gas mouth sets up in the bottom of main furnace, and the mixed export setting is in the below of auxiliary furnace.
Furthermore, the proportion range of the throat of the furnace jet section to the normal furnace diameter of the main furnace is 0.4-0.5, and the inclination angle of the feeding port relative to the vertical direction of the main furnace is 30-35 degrees.
The advantages and effects are as follows:
the utility model has the advantages of it is following and beneficial effect:
rational utilization of generated CO2The waste heat of gas and products, namely preheating and drying devices and CO before entering a heat accumulating type hot blast furnace2The preheating of the gas provides heat, so that the fuel consumption of the heat accumulating type hot blast stove is greatly reduced; the flue gas generated by burning the fuel in the heat accumulating type hot blast furnace is mixed with the combustion air to realize the recycling of the flue gas, the concentration of oxygen is diluted, the burning speed is reduced, the over-high temperature in the furnace is prevented, and NO is inhibitedxGenerating; utilizes CO generated in the process of calcining magnesite2By CO2The self-circulation pyrolysis method for preparing the light-burned magnesium oxide not only ensures the reasonable operation of the production flow, but also reduces CO2And may be used in addition to CO for pyrolysis2Other than the remaining part of CO2Gas enrichment for other industrial uses, CO achieved2The whole production system is environment-friendly and green, the technology is advanced, and the production efficiency is high.
Magnesite powder is calcined by jet pulse airflow bed calciner to increaseThe calcination quality and the energy consumption are reduced. In the feeding part, CO is fed in a jet pulse mode2The gas velocity sharply rises at the throat of the jet part of the main furnace to form high-speed fluid, at the moment, the kinetic energy is increased, the pressure intensity in the furnace is reduced, and powder at the feeding port can be sucked into the furnace, and compared with the feeding mode of the traditional calcining furnace, the energy consumption is reduced by 40%; the main furnace adopts a dumbbell-like structure, so that the disturbance of air flow is enhanced, the effect of three transmissions and one reaction between gas and solid in the furnace is promoted, the reaction rate is increased, and the calcining quality is improved.
Drawings
FIG. 1 is a system diagram of an apparatus for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas.
FIG. 2 is a schematic view showing the flow direction of the gas path of the device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas.
FIG. 3 is a schematic view of the flow direction of the material path of the device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas.
FIG. 4 is a schematic diagram of a jet pulse type entrained flow calciner of a device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas.
FIG. 5 is a left side view of the jet pulse entrained flow calciner main furnace of FIG. 4.
Reference numerals:
1-feeding machine, 2-flash evaporation dryer, 3-primary preheating cyclone device, 4-bag dust collector, 5-secondary preheating cyclone device, 6-tertiary preheating cyclone device, 7-tertiary recovery cyclone device, 8-jet pulse type entrained flow bed calcining furnace, 801-feeding port, 802-air inlet, 803-mixing outlet, 804-primary furnace, 805-secondary furnace, 806-primary furnace jet section, 807, primary furnace pulse section, 9-secondary recovery cyclone device, 10-primary recovery cyclone device, 11-transition bin, 12-heat exchanger, 13-bin, 14-fan, 15-dehumidifying device, 16-heat accumulating type hot blast stove, 17-temperature regulating chamber, 18-first flow regulating valve, 19-second flow regulating valve, 20-a third flow regulating valve, 21-a fourth flow regulating valve, 22-a flue gas treatment device, 23-a chimney, 24-an air and flue gas mixing chamber and 25-a fifth flow regulating valve.
Detailed Description
The invention will be further explained with reference to the drawings:
as shown in fig. 1, fig. 2 and fig. 3, the device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas comprises a feeding machine 1, a flash dryer 2, a bag-type dust collector 4, a multi-stage preheating device, a jet pulse type entrained flow calciner 8, a multi-stage recovery device, a heat exchanger 12, a heat accumulating type hot blast stove 16 and the like.
The gas circuit of the feeding drying device is sequentially connected with the primary preheating cyclone device 3, the multistage recovery device and the multistage preheating device and then returns to the flash dryer 2.
The material path of the feeding drying device is connected with a bin 13 through a multi-stage preheating device, a jet pulse type entrained flow calcining furnace 8, a multi-stage recovery device, a transition bin 11 and a heat exchanger 12.
One end of a gas path of the heat exchanger 12 is connected with a gas path outlet, and the other end of the gas path of the heat exchanger 12 is connected with the jet pulse type entrained flow bed calcining furnace 8 through a heating device. The gas path outlet is disposed between the fan 14 and the first flow regulating valve 18, and the first flow regulating valve 18 is disposed between the fan 14 and the heat exchanger 12.
As shown in fig. 1, 2 and 3, magnesite powdery material is fed into a flash dryer 2 from a feeding machine 1, and moisture brought in during the flotation process is dried; the dried materials are sequentially fed into a multi-stage cyclone preheating device to be subjected to graded preheating, wherein the heat required in the preheating and drying processes is CO generated by calcining magnesite2Supplying gas, namely feeding the preheated magnesite powdery material into a jet pulse type entrained flow bed calcining furnace 8 for calcining, wherein the calcined product is light-burned magnesia and CO2Introducing the obtained calcined product into a multistage cyclone recovery device to separate gas and solid, recovering light calcined magnesia product, and separating CO2The gas is separated by the cyclone recovery device and then sequentially led back to the multistage cyclone preheating device and the flash evaporation dryer 2 to provide heat for the preheating and drying processes, and then led into the bag-type dust collector 4 to remove CO brought in the preheating process2The powder in the gas is removed by a dehumidifier 15To remove water vapor, in this case CO, entrained during the drying process2The gas temperature is reduced; the CO at this time is2Sent into a heat exchanger 12 to exchange heat with the light-burned magnesia product from the primary recovery cyclone device 10, so that CO is generated2The gas is heated to a certain temperature and then is introduced into a heat accumulating type hot blast stove 16 to lead CO to2Heating the gas to the temperature meeting the requirement of producing light-burned magnesium oxide from magnesite, and adding CO2The gas is introduced into the jet pulse type entrained flow calcining furnace, which not only provides heat for the calcining process, but also can meet the requirement of magnesite fluidization calcining.
The material loading machine 1 of the material loading drying device is communicated with the flash dryer 2, and the flash dryer 2 is communicated with the one-level preheating cyclone device 3 of the multi-level preheating device.
The gas path pipeline of the multi-stage preheating device sequentially passes through a three-stage preheating cyclone device 6, a primary preheating cyclone device 3, a flash dryer 2 and a secondary preheating cyclone device 5; the material path pipeline in the multi-stage preheating device sequentially passes through the first-stage preheating cyclone device 3, the second-stage preheating cyclone device 5 and the third-stage preheating cyclone device 6.
The multi-stage preheating device is formed by mutually connecting three cyclone preheating devices, and materials are sequentially subjected to stage preheating through the primary preheating cyclone device 3, the secondary preheating cyclone device 5 and the tertiary preheating cyclone device 6;
a gas material pipeline of the flash dryer 2 is sequentially connected with a first material pipeline of a first-stage preheating cyclone device 3 of the multi-stage preheating device, a second material pipeline of a second-stage preheating cyclone device 5 and a third material pipeline of a third-stage preheating cyclone device 6; a third material pipeline of the third-stage preheating cyclone device 6 is connected with a feeding port of the jet pulse type entrained flow bed calcining furnace 8; the gas path in the multi-stage preheating device returns to the primary preheating cyclone device 3 through a third gas outlet pipeline of the three-stage preheating cyclone device 6, a second gas outlet pipeline of the secondary preheating cyclone device 5 and a gas material pipeline of the flash dryer 2 in sequence; a first air outlet pipeline of the primary preheating cyclone device 3 is sequentially connected with the bag-type dust collector 4 and the dehumidifying device 15; the powder outlet of the bag-type dust collector 4 is communicated with the feeding port of the primary preheating cyclone device 3.
The gas pipeline in the multistage recovery device sequentially passes through the first-stage recovery cyclone device 10, the second-stage recovery cyclone device 9 and the third-stage recovery cyclone device 7, and the material path pipeline in the multistage recovery device is respectively connected with the transition bin 11.
The multi-stage cyclone recovery device is formed by connecting three cyclone preheating devices, and a gas-solid mixture is separated and recovered in three stages; is more beneficial to the separation of solid in the gas-solid mixture and the recovery of gas.
A gas-solid mixing feed inlet of the primary recovery cyclone device 10 is communicated with a mixing outlet of the jet flow pulse type entrained flow calciner 8; the gas pipeline in the multi-stage recovery device sequentially passes through a fourth gas outlet pipeline of the first-stage recovery cyclone device 10, a fifth gas outlet pipeline of the second-stage recovery cyclone device 9, a sixth gas outlet pipeline of the third-stage recovery cyclone device 7, and the sixth gas outlet pipeline of the recovery cyclone device 7 is connected with the third-stage preheating cyclone device 6.
A first magnesium oxide discharge port of the first-stage recovery cyclone device 10, a second magnesium oxide discharge port of the second-stage recovery cyclone device 9 and a third magnesium oxide discharge port of the third-stage recovery cyclone device 7 are connected with a transition bin 11.
As shown in fig. 4 and 5, the furnace type adopted by the jet pulse type entrained flow bed calcining furnace is an inverted U shape, the furnace body is provided with a feeding port 801, an air inlet 802 and a mixing outlet 803, one side of the feeding port 801 and the air inlet 802 is a main furnace of the jet pulse type entrained flow bed calcining furnace 8, one side of the mixing outlet 803 is an auxiliary furnace 805 of the jet pulse type entrained flow bed calcining furnace 8, the main furnace 804 and the auxiliary furnace 805 are communicated above, and the jet pulse part of the main furnace 804 adopts a dumbbell-like structure, namely, a shape with a thin middle part and two thick ends; the jet flow pulse part comprises a main furnace jet flow section 806 and a main furnace pulse section 807, the main furnace jet flow section 807 is communicated with the upper part of the main furnace jet flow section 806, the main furnace jet flow section 806 is arranged below the main furnace 804, the main furnace pulse section 807 is arranged above the main furnace jet flow section 806, the main furnace jet flow section 806 is communicated with the main furnace pulse section 807, two feeding ports 801 which are opposite in position are arranged at the throat of the main furnace jet flow section 806 on the main furnace 804, the feeding ports 802 are arranged at the bottom of the main furnace 804, and the mixing outlet 803 is arranged below the auxiliary furnace 805.
The ratio range of the throat of the jet section 806 of the main furnace to the normal furnace diameter of the main furnace 804 is 0.4-0.5, the throat is the part with the smallest diameter of the jet section 806 of the main furnace, the ratio range of the upper contraction part of the pulse section 807 of the main furnace to the normal furnace diameter of the main furnace 804 is 0.8-0.85, and the contraction part is the part with the smallest diameter of the pulse section 807 of the main furnace; the inclination angle of the feeding port 801 relative to the vertical direction of the main furnace 804 is 30-35 degrees. Two feeding ports 801 are symmetrically arranged on two opposite sides at 180 degrees relative to the circumferential direction of the main furnace 804. The furnace diameter of the main furnace 804 refers to the diameter of the position where the main furnace is the largest and is communicated with the auxiliary furnace.
The arrangement of the inlet 801 and the inlet 802 is shown in the left side view of the main furnace of the jet pulse type entrained flow calciner in fig. 5, and in order to prevent the concentration distribution of magnesite powder particles in the furnace from being uneven, two opposite inlets are arranged at the throat of the jet part on the main furnace. In order to ensure the gas-solid mixing and pneumatic transmission in the furnace, the inclination angle of the feeding port 801 relative to the vertical direction of the main furnace 804 is 30-35 degrees. The gas inlet 802 is provided at the bottommost portion of the main furnace 804, and the CO is introduced into the main furnace side2The gas flows upwards, and when passing through the throat of the jet part of the main furnace, the gas velocity is increased sharply to form high-velocity fluid. According to Bernoulli's theorem, when kinetic energy is increased, the pressure in the furnace is reduced, powder at the feeding port can be sucked into the furnace, and compared with the feeding mode of the traditional calcining furnace, the energy consumption is reduced by 40%. The main furnace is composed of a main furnace jet flow section 806 and a main furnace pulse section 807, and adopts a dumbbell-like structure. When the airflow drives the powder to enter the main furnace pulse section 807, the gas and the powder are fully mixed and contacted due to the aggravated airflow disturbance caused by the dumbbell-like shape of the furnace body, so that the effect of three-transmission-one-reaction (momentum transfer, heat transfer, mass transfer and chemical reaction process) between gas and solid in the furnace is promoted, the reaction rate is increased, and the calcining quality is improved. Due to the increase of the reaction rate, the overall height of the calcining furnace is reduced by about 20-30% compared with that of a dynamic cyclone calcining furnace adopted in patent CN110590191A published in 12, 20 and 2019. If the dynamic cyclone calcining furnace adopted in patent CN110590191A published in 12, 20 and 12 in 2019 is used for calcining magnesite to produce light-burned magnesia, the calculated maximum kiln thermal decomposition strength is 440 kg/(m)3H) calcining magnesite by the jet pulse type entrained flow bed calcining furnace shown in FIG. 4 to produce light-calcined magnesiaThe thermal decomposition strength of the furnace is improved by about 20 percent.
A heat accumulating type hot blast stove of the heating device is connected with a flue gas treatment device 22, the flue gas treatment device 22 is respectively connected with a chimney 23 and an air and flue gas mixing chamber 24, a temperature adjusting chamber 17 is arranged behind the heat accumulating type hot blast stove, one end of a heating air outlet pipe is communicated with the temperature adjusting chamber 17, and an air outlet of the temperature adjusting chamber 17 is connected with an air inlet of a jet pulse type entrained flow bed calcining furnace 8.
The heat accumulating type hot blast stove consists of three top combustion heat accumulating type hot blast stoves, and the top combustion heat accumulating type hot blast stoves are respectively connected with natural gas and air; a heating air inlet pipeline of the heating device is respectively connected with a heat accumulating type hot blast stove and a temperature regulating room 17 provided with a fourth flow regulating valve 21, and a third flow regulating valve 20 is arranged on a carbon dioxide gas pipeline communicated between the heat accumulating type hot blast stove and the temperature regulating room 17; the flue gas duct between the flue gas treatment device 20 and the air-flue gas mixing 24 is provided with a fifth flow regulating valve 25.
As shown in fig. 1, the regenerative hot blast stove is composed of three existing top-combustion regenerative hot blast stoves, which use natural gas as fuel, and work by switching in a two-intermittent one-way mode, and checker bricks as carriers of heat; one working cycle of the heat accumulating type hot blast stove is divided into a combustion period and an air supply period, in the combustion period, an air supply outlet and an air outlet are closed, fuel is combusted to generate high-temperature flue gas, and heat is released into checker bricks to be accumulated; in the air supply period, an air supply outlet and an air outlet are opened, and the introduced air is heated by the checker bricks which are subjected to heat storage; the combustion flue gas is ejected out by the circulating flue gas, and is discharged after being processed by the flue gas processing device, so that the combustion flue gas is ensured not to enter the calcining furnace.
The fuel is burnt in the heat accumulating type hot blast stove to generate smoke, one part of the smoke is mixed with combustion air required by burning, the concentration of oxygen in the air can be reduced, and thermal NO is inhibitedXThe mixed gas is used for fuel combustion supporting to realize the circulation of the flue gas, and a flow regulating valve is arranged in front of the air-flue gas mixing chamber to regulate the flow of the circulating flue gas.
CO2The gas can be used for the continuous generation of CO in the calcination process except for the flow rate required for the self-circulation pyrolysis2The gas is recycled by carbon dioxide, and a flow regulating valve 19 is arranged to regulate CO for recycling carbon dioxide2The amount of gas.
A temperature adjusting room is arranged behind the heat accumulating type hot blast stove and used for adjusting CO out of the heat accumulating type hot blast stove2The temperature at which the gas flows into the calciner. Part of CO preheated by the heat exchanger2The gas is shunted to the front end of the temperature adjusting chamber and is heated by the heat accumulating type hot blast stove2The gas is mixed, thereby achieving the purpose of temperature adjustment; at the air outlet of the heat accumulating type hot blast stove and CO2The gas shunting parts are respectively provided with a flow regulating valve, and the temperature is regulated by regulating the flow.
Example 1
As shown in fig. 1, 2 and 3, the device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas comprises a feeding machine 1, a flash dryer 2, a bag-type dust collector 4, a multi-stage preheating device, a jet pulse type entrained flow calciner, a multi-stage recovery device, a heat exchanger, a heat accumulating type hot blast furnace and the like.
The feeding machine 1 enters the flash evaporation dryer 2 through a dryer feeding hole, a gas material pipeline of the flash evaporation dryer 2 is communicated with a feeding hole arranged on the side of the primary preheating cyclone device 3, a first gas outlet pipeline is arranged above the primary preheating cyclone device 3 and communicated with a gas inlet of the bag-type dust collector 4, and a gas outlet of the bag-type dust collector 4 is sequentially connected with a dehumidifying device 15 and a fan 14; a second flow regulating valve 20 is arranged to regulate CO for resource utilization of carbon dioxide2The gas flow rate; the fan 14 and the first flow regulating valve 18 are communicated with the heat exchanger 12 to convey carbon dioxide gas, the heat exchanger 12 is communicated with a heating device through a heating gas inlet pipeline, a heating gas outlet pipeline of the heating device is communicated with a gas inlet of the jet pulse type entrained flow bed calcining furnace 8, and the gas inlet of the jet pulse type entrained flow bed calcining furnace 8 is arranged at the lower end of the main furnace.
The jet pulse type entrained flow bed calcining furnace 8 is arranged at a mixing outlet of the auxiliary furnace and is communicated with a multi-stage recovery device, the specific structure of the multi-stage recovery device is that gas-solid mixed feeding of a primary recovery cyclone device 10 is communicated with the mixing outlet of the secondary furnace, the jet pulse type entrained flow bed calcining furnace 8 is arranged at the mixing outlet of the auxiliary furnace, a fourth air outlet pipeline arranged above the primary recovery cyclone device 10 is communicated with an inlet arranged at the side surface of a secondary recovery cyclone device 9, a fifth air outlet pipeline arranged above the secondary recovery cyclone device 9 is communicated with the side surface of a tertiary recovery cyclone device 7, and the upper part of the tertiary recovery cyclone device 7 is communicated with a third air inlet pipeline of a tertiary; magnesium oxide discharge ports are arranged below the primary recovery cyclone device 10, the secondary recovery cyclone device 9 and the tertiary recovery cyclone device 7 and respectively comprise a first magnesium oxide discharge port, a second magnesium oxide discharge port and a third magnesium oxide discharge port; the three magnesium oxide discharge ports are communicated with a transition bin 11, the transition bin 11 is communicated with a bin inlet of a heat exchanger 12, and a bin outlet of the heat exchanger is communicated with an upper interface of the bin.
The multi-stage preheating device comprises a first-stage preheating cyclone device 3, a second-stage preheating cyclone device 5 and a third-stage preheating cyclone device 6. Each stage of preheating cyclone device is provided with four connecting ports, a feeding port on the side surface of the primary preheating cyclone device 3 is communicated with a gas material pipeline of the flash dryer 2, a first gas outlet pipeline above the primary preheating cyclone device 3 is communicated with the bag-type dust collector 4, a feeding port on the side surface of the primary preheating cyclone device 3 is communicated with a powder outlet arranged on the west side of the bag-type dust collector 4, a first material pipeline arranged below the primary preheating cyclone device 3 is communicated with the side surface of the secondary preheating cyclone device 5, a second gas outlet pipeline connected with the flash dryer 2 is arranged above the secondary preheating cyclone device 5, a second material pipeline arranged below the secondary preheating cyclone device 5 is communicated with the side surface of the tertiary preheating cyclone device 6, and a third gas outlet pipeline arranged above the tertiary preheating cyclone device 6 is communicated with the side surface of the secondary preheating cyclone device 5; a third material pipeline below the third-stage preheating cyclone device 6 is communicated with a feeding port of the jet pulse type entrained flow bed calcining furnace 8, and the side of the third-stage preheating cyclone device 6 is communicated with a sixth air outlet pipeline of the third-stage recovery cyclone device 7.
A heat accumulating type hot blast stove of the heating device is connected with a flue gas treatment device 22, the flue gas treatment device 23 is respectively connected with a chimney 23 and an air and flue gas mixing chamber 24, a temperature adjusting chamber 17 is arranged behind the heat accumulating type hot blast stove, one end of a heating air outlet pipe is communicated with the temperature adjusting chamber 17, and an air outlet of the temperature adjusting chamber 17 is connected with an air inlet of a jet pulse type entrained flow bed calcining furnace 8.
The heat accumulating type hot blast stove consists of three top combustion heat accumulating type hot blast stoves, and the top combustion heat accumulating type hot blast stoves are respectively connected with natural gas and air; a heating air inlet pipeline of the heating device is respectively connected with a heat accumulating type hot blast stove and a temperature regulating room 17 provided with a fourth flow regulating valve 21, and a third flow regulating valve 20 is arranged on a carbon dioxide gas pipeline communicated between the heat accumulating type hot blast stove and the temperature regulating room 17; the flue gas duct between the flue gas treatment device 22 and the air-flue gas mixing 24 is provided with a fifth flow regulating valve 25.
As shown in fig. 2, the gas path of the whole device comprises a multistage recovery device for separating magnesium oxide and carbon dioxide, and the separated carbon dioxide is delivered to a multistage preheating device and a flash dryer 2 for utilizing waste heat. Then the carbon dioxide is recycled after passing through a bag-type dust collector 4 and a dehumidifying device 15 from the primary preheating cyclone device 3.
As shown in figure 3, the material path of the whole device comprises that the material is fed from a feeding machine 1 and is conveyed to a primary preheating cyclone device 3 through a flash dryer 2, a first material pipeline of the primary preheating cyclone device 3 sends the material to a secondary preheating cyclone device 5, a second material pipeline of the secondary preheating cyclone device 5 sends the material to a tertiary preheating cyclone device 6, a third material pipeline of the tertiary preheating cyclone device 6 sends the material to a feeding port below a main furnace of a jet pulse type entrained flow calciner 8, the mixture of carbon dioxide and magnesium oxide is sent to a solid mixing feed inlet of a first-stage recovery cyclone device 10 in a multistage recovery device through a mixing outlet by an auxiliary furnace, magnesium oxide discharge ports are arranged below the recovery cyclone devices in the multistage recovery device and communicated with a transition bin 11, and the transition bin 11 sends the magnesium oxide to a bin 13 through a heat exchanger 12.
The actual implementation process comprises the following steps:
1.12t of wet magnesite material subjected to flotation is put into a flash dryer 2 through a feeding machine 1 per hour, the temperature of magnesite is 20 ℃, the feeding amount of the dried magnesite is 1t/h, the product yield of the whole light-burned magnesia system is 476kg/h, and CO is theoretically generated in the calcining process2Gas 265Nm3H is used as the reference value. Will dryThe dried magnesite powder is sequentially introduced into a primary preheating cyclone device 3, a secondary preheating cyclone device 5 and a tertiary preheating cyclone device 6 for preheating, the temperature of the magnesite powder is preheated to 150 ℃ after passing through the primary preheating cyclone device 3, the temperature of the magnesite powder is preheated to 420 ℃ after passing through the secondary preheating cyclone device 5, the temperature of the magnesite powder is preheated to 550 ℃ after passing through the tertiary preheating cyclone device 6, the temperature for magnesite pyrolysis is 400-500 ℃, when the magnesite is preheated by the preheating device, 30% of the magnesite input amount is decomposed, and the rest 70% of the magnesite is decomposed by a jet pulse type airflow bed calciner 8.
Feeding magnesite powder material with the temperature of 550 ℃ into a jet flow pulse type entrained flow bed calcining furnace 8 for calcining, wherein the calcined product is light calcined magnesia and CO2Gas, temperature 730 ℃. Introducing the calcined product into a primary recovery cyclone device 10, a secondary recovery cyclone device 9 and a tertiary recovery cyclone device 7 in sequence for gas-solid separation, and separating the 670-DEG C CO by the tertiary recovery cyclone device 72The gas flows back to the multistage cyclone preheating device and the flash dryer 2 in sequence to provide heat, CO, for preheating and drying2CO flowing out of the flash dryer 2 after residual heat utilization of the gas2The gas was 190 ℃. Due to CO2The gas will be mixed into part of the magnesite powder during the process of preheating and drying the latter, so that the CO flowing out of the flash dryer 22The gas needs to pass through a bag-type dust collector 4 to remove the doped powder. Due to the use of CO2The gas being CO in the course of drying the wet material2The gas is mixed with water vapor, so that CO coming out of the bag-type dust collector 42The gas is dehumidified at low temperature in the dehumidifier 15, and the dehumidified CO is2The gas temperature is 90 ℃, pressurized by the fan 14 and then introduced into the heat exchanger 12.
The light calcined magnesia product separated by the multi-stage cyclone recovery device enters a transition bin 11. Then is introduced into a heat exchanger 12 to react with CO2Gas heat exchange is carried out to realize the utilization of the waste heat of the product, the light-burned magnesium oxide product after heat exchange enters a storage bin 13, and CO is added2The gas was warmed to 350 ℃. Wherein a first flow control valve 18 is arranged in front of the heat exchanger 12, since CO is produced as the production continues2The gas is more and more, the concentration is gradually increased, and the rest CO can be added except for the part used for self-circulation pyrolysis2The gas is subjected to carbon dioxide resource utilization, and CO for self-heating and carbon dioxide resource utilization is regulated through the first flow regulating valve 18 and the second flow regulating valve 202The flow rate of the gas.
CO to be warmed by heat exchanger 122And introducing the gas into a heat accumulating type hot blast stove 16. The heat accumulating type hot blast stove uses natural gas as fuel and checker bricks as a carrier of high-temperature heat to heat CO2When the gas reaches the temperature for calcining the light-burned magnesia, the combustion gas generated by the combustion of the fuel is processed by the flue gas processing device 22, 10 percent of the flue gas is taken to be sent to the air-flue gas mixing chamber 24 to be mixed with combustion-supporting air for supporting the combustion of the fuel, the quantity of the circulating flue gas is controlled by the fifth flow regulating valve 25,
the rest of the flue gas is treated by the flue gas treatment device 22 and then discharged from the chimney 23. CO 22The temperature of the gas entering the heat accumulating type hot blast stove 16 is 350 ℃, the temperature is raised to 1250 ℃ after the gas is heated, and the gas flows out of the hot blast stove. Then enters a temperature adjusting room 17 for adjusting CO2The temperature of the gas flowing into the jet pulse type entrained flow calciner. Using CO at 350 deg.C entering heat accumulating hot blast stove 162The gas is adjusted, and the temperature of the adjusted incident flow pulse type entrained flow calciner is 1200 ℃. By recirculation of flue gases, NO in the combustion process is suppressedxAnd (4) generating. And CO2The gas not only provides the heat required for pyrolyzing the magnesite in the calcining process, but also leads the magnesite powder to be fluidized and calcined in the calcining furnace.
The produced light-burned magnesia has no overburning and underburning phenomena, and the magnesia content in the product is not less than 96 percent; the content of silicon dioxide is not more than 0.5 percent; the content of calcium oxide is not more than 1.0%; the ignition loss is 1-2%; the activity of the light-burned magnesium oxide is measured to be 30-80 s by a citric acid method; the data prove that the produced light-burned magnesium oxide product meets the requirements of national standards. The product recovery rate of the whole system is more than or equal to 99.9 percent through a multi-stage recovery device; CO for resource utilization of carbon dioxide2The gas purity can reach more than 99 percent, and the industrial application is satisfied；CO2The gas emission is reduced by about 75 percent compared with the traditional direct-combustion light-burned magnesia production system.
Compared with the prior art, the device does not additionally arrange a burner and pyrolyzes CO generated by magnesite2The temperature of the gas is increased after being heated by a heat accumulating type hot blast stove, so that the high temperature CO is obtained2Gas is introduced into the calcining furnace to calcine magnesite, thereby solving the problem of CO generated during the pyrolysis of the magnesite2Problems with gas emissions; the waste heat of the flue gas generated by calcination and the waste heat of the generated product are fully utilized, and the consumption of fuel in the heat accumulating type hot blast stove is reduced. The utility model discloses a light-burned magnesia apparatus for producing's advantage mainly embodies in green's aspect, compares with the current technology that utilizes combustor direct combustion pyrolysis magnesite to produce light-burned magnesia the utility model discloses an in the light-burned magnesia production process, CO2The gas emission is reduced by about 75%.
The device has the following characteristics:
1. the magnesite powder is calcined by adopting a jet pulse type entrained flow calciner, so that the calcining quality is improved and the energy consumption is reduced. In the feeding part, CO is fed in a jet pulse mode2The gas velocity sharply rises at the throat of the jet part of the main furnace to form high-speed fluid, at the moment, the kinetic energy is increased, the pressure intensity in the furnace is reduced, powder at the feeding port can be sucked into the furnace, and compared with the feeding mode of the traditional calcining furnace, the energy consumption is reduced by 40%; the main furnace adopts a dumbbell-like structure, so that the disturbance of air flow is enhanced, the effect of three transmissions and one reaction between gas and solid in the furnace is promoted, the reaction rate is increased, and the calcining quality is improved.
2. Rational utilization of generated CO2The waste heat of gas and products is CO for drying and preheating materials before entering a heat accumulating type hot blast furnace2The preheating of the gas provides heat, and the fuel consumption of the heat accumulating type hot blast stove is greatly reduced.
3. The flue gas generated by burning the fuel in the heat accumulating type hot blast furnace is mixed with the combustion air to realize the recycling of the flue gas, the concentration of oxygen is diluted, the burning speed is reduced, the overhigh temperature in the furnace is prevented, and the generation of NOx is inhibited.
4. Benefit toUsing CO generated in the process of calcining magnesite2By CO2The self-circulation pyrolysis method for preparing the light-burned magnesium oxide not only ensures the reasonable operation of the production flow, but also reduces CO2And may be used in addition to CO for pyrolysis2Other than the remaining part of CO2CO enriched for other industrial uses2The whole production system is environment-friendly and green, the technology is advanced, and the production efficiency is high.
Claims (10)
1. Flue gas self-loopa pyrolysis preparation light burns device of magnesium oxide and enrichment carbon dioxide, its characterized in that: the gas path of the feeding drying device is sequentially connected with a primary preheating cyclone device (3), a multi-stage recovery device and a multi-stage preheating device and then returns to the flash dryer (2), and the material path of the feeding drying device is connected to a storage bin (13) through the multi-stage preheating device, a jet pulse type entrained flow bed calcining furnace (8), the multi-stage recovery device, a transition storage bin (11) and a heat exchanger (12); one end of a gas path of the heat exchanger (12) is connected with the first flow regulating valve (18), and the other end of the gas path of the heat exchanger (12) is connected with the jet pulse type entrained flow bed calcining furnace (8) through a heating device.
2. The apparatus for preparing light-burned magnesia and enriching carbon dioxide by flue gas self-circulation pyrolysis according to claim 1, characterized in that: a feeding machine (1) of the feeding drying device is communicated with a flash dryer (2), and the flash dryer (2) is communicated with a primary preheating cyclone device (3) of the multi-stage preheating device.
3. The apparatus for preparing light-burned magnesia and enriching carbon dioxide by flue gas self-circulation pyrolysis according to claim 1, characterized in that: the gas path pipeline of the multi-stage preheating device sequentially passes through a three-stage preheating cyclone device (6), a two-stage preheating cyclone device (5), a flash evaporation dryer (2) and a one-stage preheating cyclone device (3); a material path pipeline in the multi-stage preheating device sequentially passes through the primary preheating cyclone device (3), the secondary preheating cyclone device (5) and the tertiary preheating cyclone device (6).
4. The apparatus for preparing light-burned magnesia and enriching carbon dioxide by flue gas self-circulation pyrolysis according to claim 1 or 3, characterized in that: a gas material pipeline of the flash dryer (2) is sequentially connected with a first material pipeline of a first-stage preheating cyclone device (3) of the multi-stage preheating device, a second material pipeline of a second-stage preheating cyclone device (5) and a third material pipeline of a third-stage preheating cyclone device (6); a third material pipeline of the three-stage preheating cyclone device (6) is connected with a feeding port of the jet pulse type entrained flow bed calcining furnace (8);
the gas path in the multi-stage preheating device returns to the primary preheating cyclone device (3) through a third gas outlet pipeline of the three-stage preheating cyclone device (6), a second gas outlet pipeline of the secondary preheating cyclone device (5) and a gas material pipeline of the flash dryer (2) in sequence;
a first air outlet pipeline of the primary preheating cyclone device (3), a bag-type dust collector (4) and a dehumidifying device (16);
the powder outlet of the bag-type dust collector (4) is communicated with the feeding port of the primary preheating cyclone device (3).
5. The apparatus for preparing light-burned magnesia and enriching carbon dioxide by flue gas self-circulation pyrolysis according to claim 1, characterized in that: the gas pipeline in the multistage recovery device sequentially passes through the primary recovery cyclone device (10), the secondary recovery cyclone device (9) and the tertiary recovery cyclone device (7), and the material path pipeline in the multistage recovery device is respectively connected with the transition bin (11).
6. The apparatus for preparing light-burned magnesia and enriching carbon dioxide by flue gas self-circulation pyrolysis according to claim 5, is characterized in that: a gas-solid mixing feed inlet of the primary recovery cyclone device (10) is communicated with a mixing outlet of the jet flow pulse type entrained flow bed calcining furnace (8),
gas pipelines in the multi-stage recovery device sequentially pass through a fourth gas outlet pipeline of the primary recovery cyclone device (10), a fifth gas outlet pipeline of the secondary recovery cyclone device (9), a sixth gas outlet pipeline of the tertiary recovery cyclone device (7), and the sixth gas outlet pipeline of the recovery cyclone device (7) is connected with the tertiary preheating cyclone device (6);
a first magnesium oxide discharge port of the first-stage recovery cyclone device (10), a second magnesium oxide discharge port of the second-stage recovery cyclone device (9) and a third magnesium oxide discharge port of the third-stage recovery cyclone device (7) are connected with the transition bin (11).
7. The apparatus for preparing light-burned magnesia and enriching carbon dioxide by flue gas self-circulation pyrolysis according to claim 1, characterized in that: a heat accumulating type hot blast stove of the heating device is connected with a flue gas treatment device (22), the flue gas treatment device (22) is respectively connected with a chimney (23) and an air and flue gas mixing chamber (24), a temperature adjusting chamber (17) is arranged behind the heat accumulating type hot blast stove, one end of a heating air outlet pipe is communicated to the temperature adjusting chamber (17), and an air outlet of the temperature adjusting chamber (17) is connected with an air inlet of a jet pulse type entrained flow bed calcining furnace (8).
8. The apparatus for preparing light-burned magnesia and enriching carbon dioxide by flue gas self-circulation pyrolysis according to claim 7, is characterized in that: the heat accumulating type hot blast stove consists of three top combustion heat accumulating type hot blast stoves, and the top combustion heat accumulating type hot blast stoves are respectively connected with natural gas and air;
a heating air inlet pipeline of the heating device is respectively connected with the heat accumulating type hot blast stove and a temperature regulating room (17) provided with a fourth flow regulating valve (21), and a third flow regulating valve (20) is arranged on a carbon dioxide gas pipeline communicated between the heat accumulating type hot blast stove and the temperature regulating room (17);
a fifth flow regulating valve (25) is arranged on a flue gas pipeline between the flue gas treatment device (22) and the air and flue gas mixing chamber (24).
9. The apparatus for preparing light-burned magnesia and enriching carbon dioxide by flue gas self-circulation pyrolysis according to claim 1, characterized in that: the furnace type adopted by the jet pulse type entrained flow bed calcining furnace (8) is an inverted U shape, the furnace body is provided with a feeding port (801), an air inlet (802) and a mixing outlet (803), one side of the feeding port (801) and one side of the air inlet (802) are a main furnace (804) of the jet pulse type entrained flow bed calcining furnace (8), one side of the mixing outlet (803) is an auxiliary furnace (805) of the jet pulse type entrained flow bed calcining furnace (8), the main furnace (804) and the auxiliary furnace (805) are communicated above, and the jet pulse part of the main furnace (804) adopts a dumbbell-like structure; the main furnace jet flow section (806) is arranged below the main furnace (804), the main furnace pulse section (807) is arranged above the main furnace jet flow section (806), the main furnace jet flow section (806) is communicated with the main furnace pulse section (807), two feeding ports (801) opposite in position are arranged at the throat of the main furnace jet flow section (806) on the main furnace (804), the gas inlet (802) is arranged at the bottom of the main furnace (804), and the mixing outlet (803) is arranged below the auxiliary furnace (805).
10. The apparatus for preparing light-burned magnesia and enriching carbon dioxide by flue gas self-circulation pyrolysis according to claim 9, characterized in that: the ratio of the throat of the jet flow section (806) of the main furnace to the furnace diameter of the main furnace (804) ranges from 0.4 to 0.5, and the inclination angle of the feeding port (801) relative to the vertical direction of the main furnace (804) ranges from 30 to 35 degrees.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111777340A (en) * | 2020-08-20 | 2020-10-16 | 辽宁圣世资源环境科技有限公司 | Device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas |
| CN114634316A (en) * | 2022-03-30 | 2022-06-17 | 营口益嘉镁业科技有限公司 | Heat exchange device for recycling waste heat generated in production of high-purity magnesium oxide |
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2020
- 2020-08-20 CN CN202021746223.XU patent/CN212504610U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111777340A (en) * | 2020-08-20 | 2020-10-16 | 辽宁圣世资源环境科技有限公司 | Device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas |
| CN111777340B (en) * | 2020-08-20 | 2024-04-23 | 辽宁东大粉体工程技术有限公司 | Device for preparing light burned magnesia and enriching carbon dioxide by smoke self-circulation pyrolysis |
| CN114634316A (en) * | 2022-03-30 | 2022-06-17 | 营口益嘉镁业科技有限公司 | Heat exchange device for recycling waste heat generated in production of high-purity magnesium oxide |
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Effective date of registration: 20230918 Address after: No.19 Caita Street, Shenhe District, Shenyang, Liaoning 110069 Patentee after: LIAONING NORTHEAST UNIVERSITY POWDER PROJECT TECHNOLOGY CO.,LTD. Address before: 110027 No.20, 4th Street, economic and Technological Development Zone, Tiexi District, Shenyang City, Liaoning Province Patentee before: Liaoning Shengshi resources and Environment Technology Co.,Ltd. |