CN206318951U - The system that a kind of hydrogasification coupling calcium carbide is smelted - Google Patents
The system that a kind of hydrogasification coupling calcium carbide is smelted Download PDFInfo
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- CN206318951U CN206318951U CN201621332890.7U CN201621332890U CN206318951U CN 206318951 U CN206318951 U CN 206318951U CN 201621332890 U CN201621332890 U CN 201621332890U CN 206318951 U CN206318951 U CN 206318951U
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- mixed material
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- 239000005997 Calcium carbide Substances 0.000 title claims abstract description 56
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 230000008878 coupling Effects 0.000 title abstract description 9
- 238000010168 coupling process Methods 0.000 title abstract description 9
- 238000005859 coupling reaction Methods 0.000 title abstract description 9
- 239000000463 material Substances 0.000 claims abstract description 72
- 238000002309 gasification Methods 0.000 claims abstract description 71
- 239000007789 gas Substances 0.000 claims abstract description 66
- 239000000843 powder Substances 0.000 claims abstract description 49
- 239000003245 coal Substances 0.000 claims abstract description 43
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000001257 hydrogen Substances 0.000 claims abstract description 33
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 33
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 16
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 16
- 239000001301 oxygen Substances 0.000 claims abstract description 16
- 239000007787 solid Substances 0.000 claims abstract description 15
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 66
- 235000012255 calcium oxide Nutrition 0.000 claims description 33
- 239000000292 calcium oxide Substances 0.000 claims description 33
- 238000006243 chemical reaction Methods 0.000 claims description 25
- 238000003723 Smelting Methods 0.000 claims description 14
- 238000003860 storage Methods 0.000 claims description 12
- 238000004321 preservation Methods 0.000 claims description 11
- 238000005984 hydrogenation reaction Methods 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 22
- 238000000926 separation method Methods 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 239000007790 solid phase Substances 0.000 abstract description 6
- 238000010791 quenching Methods 0.000 abstract description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 abstract 2
- 241001417490 Sillaginidae Species 0.000 abstract 2
- 235000011941 Tilia x europaea Nutrition 0.000 abstract 2
- 229910052791 calcium Inorganic materials 0.000 abstract 2
- 239000011575 calcium Substances 0.000 abstract 2
- 239000004571 lime Substances 0.000 abstract 2
- 239000002817 coal dust Substances 0.000 abstract 1
- 238000000034 method Methods 0.000 description 17
- 239000000376 reactant Substances 0.000 description 8
- 239000002994 raw material Substances 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 239000000203 mixture Substances 0.000 description 5
- 239000007795 chemical reaction product Substances 0.000 description 4
- 239000000571 coke Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000035425 carbon utilization Effects 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- Carbon And Carbon Compounds (AREA)
Abstract
The utility model discloses the system that a kind of hydrogasification coupling calcium carbide is smelted.The system includes hydrogasification unit and calcium carbide smelts unit；Wherein, the hydrogasification unit includes coal nozzle, hydrogen-rich gas nozzle, oil gas vent, Quench calcium lime powder nozzle and mixed material outlet；The calcium carbide, which smelts unit, includes mixed material entrance, oxygen-rich gas nozzle, calcium carbide furnace gas outlet and calcium carbide outlet, and the mixed material entrance is connected with mixed material outlet.The hydrogasification of low order coal dust produces the system being coupled with calcium carbide during the utility model is provided, and by way of solid calcium lime powder Quench, gasification char is cooled down, while changing the running orbit of gas, the separation of gas-solid phase is realized.Meanwhile, the sensible heat of gasification char, the energy consumption of reduction calcium carbide production can be made full use of.
Description
Technical Field
The utility model belongs to the technical field of the chemical industry, especially, relate to a system that hydro-gasification coupling carbide was smelted.
Background
The coal powder hydro-gasification is a process of generating crude coal gas and semicoke by reacting coal powder and hydrogen under the conditions of high temperature and high pressure. At present, the yield of the semicoke obtained by coal powder hydro-gasification accounts for about 50% of the feeding amount (coal powder quality), the carbon content in the semicoke is up to more than 80%, and the temperature after the reaction is finished is higher, so that the semicoke must be thermally converted again to improve the carbon utilization rate of the whole process.
The coal powder hydro-gasification semicoke has the characteristics of high fixed carbon, low volatile matter, low sulfur and the like, and three secondary thermal conversion modes are adopted: one is direct combustion; the other is to return the semicoke generated by gasification to the original hydro-gasification furnace for multiple times of circulating gasification; and the other is to send the semicoke into another high-temperature entrained-flow bed gasification furnace for rapid thermal conversion. Wherein, the direct combustion mode has lower comprehensive utilization rate, the content of the semicoke volatile component generated by hydro-gasification is low, the reaction activity of regasification is lower, and the advantages and the characteristics of gasified semicoke are not fully utilized.
Meanwhile, a large amount of high-quality blocky semi-coke needs to be consumed in calcium carbide production, if the hydro-gasification semi-coke can be directly used as a raw material for calcium carbide production, the low-and-medium-rank coal can be utilized in a grading and quality-dividing manner, a large amount of methane-rich gas and light tar can be obtained as byproducts while the raw material for calcium carbide production is obtained, the sensible heat of the gasification semi-coke can be fully utilized, and the energy consumption for calcium carbide production is reduced. However, the particle size of the gasified pulverized coal is small, the gasification reaction temperature is high, the obtained gasified semicoke is difficult to separate from the gas product, the existing gasification furnace generally adopts a water chilling mode to cool and separate the gasified semicoke, but the water chilling cannot fully utilize the sensible heat of the gasified semicoke and is unfavorable for the subsequent calcium carbide production, and therefore, a proper chilling method must be found to meet the requirements of the subsequent calcium carbide production.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a system and method of well low rank buggy hydro-gasification and carbide production looks coupling, mode through solid quick lime chilling, not only can cool off the gasification semicoke, change gaseous orbit, realize the purpose of gas-solid separation, and can preheat carbide raw materials for production quick lime, obtain the required high temperature mixture of carbide production, this mixture directly sends to the entrained flow through high temperature heat send the technique, adopt the oxygen heat method production carbide, the sensible heat of the mixture of can recycling, reduce the energy consumption of carbide production.
In order to realize the aim, the utility model provides a system for smelting the hydrogenation gasification coupling calcium carbide, which comprises a hydrogenation gasification unit and a calcium carbide smelting unit; wherein,
the hydro-gasification unit comprises a coal powder nozzle, a hydrogen-rich gas nozzle, an oil gas outlet, a chilled quicklime powder nozzle and a mixed material outlet; in the hydro-gasification unit, coal powder and a product of hydro-gasification reaction of hydrogen-rich gas are chilled by solid quicklime to obtain a mixed material and an oil gas product;
the calcium carbide smelting unit comprises a mixed material inlet, an oxygen-enriched gas nozzle, a calcium carbide furnace gas outlet and a calcium carbide outlet, the mixed material inlet is connected with the mixed material outlet, and the calcium carbide smelting unit is used for reacting the mixed material to generate calcium carbide.
Specifically, the device used by the hydro-gasification unit is a gasification furnace.
The device used by the calcium carbide smelting unit is an entrained flow bed.
Further, the hydro-gasification unit includes a reaction zone, a quench zone, and a mixed feed storage zone.
The reaction zone is provided with the pulverized coal nozzle, the hydrogen-rich gas nozzle and the oil gas outlet; the number of the hydrogen-rich gas nozzles is an even number, and the hydrogen-rich gas nozzles are symmetrically arranged around the pulverized coal nozzles; the pulverized coal nozzle is arranged at the top of the gasification furnace.
The chilling zone is provided with the chilling quicklime powder nozzles, the chilling quicklime powder nozzles are arranged on the furnace wall below the reaction zone, and the chilling quicklime powder nozzles are even in number and symmetrically distributed around the gasification furnace.
The mixed material storage area is provided with a mixed material baffle, a mixed material scraper and a mixed material outlet, and the mixed material outlet is arranged at the bottom end of the gasification furnace.
The system also comprises a high-temperature solid conveying unit, and the mixed material inlet is connected with the mixed material outlet through the high-temperature solid conveying unit.
Specifically, the device of the high-temperature solid conveying unit is a closed heat-preservation ladle, and the conveying mode of the closed heat-preservation ladle adopts a horizontal sliding rail and vertical lifting mode.
Preferably, the included angle of the mixed semicoke baffle and the horizontal direction is 30-75 degrees.
The utility model provides a system of middle-low rank buggy hydro-gasification and carbide production looks coupling through the mode of solid quick lime powder chilling, cools off the gasification semicoke, changes gaseous orbit simultaneously, realizes the separation of gas-solid phase. Meanwhile, sensible heat of gasified semicoke can be fully utilized to preheat calcium carbide production raw materials, the mixed material obtained after chilling is directly heated and sent to an entrained flow bed, the calcium carbide is produced by an oxygen heating method, and the energy consumption of calcium carbide production is reduced.
Adopt the utility model discloses a system has gained following effect:
(1) the calcium carbide is produced by taking the powdery medium-low-grade coal and the powdery quick lime as raw materials, so that the applicability of the raw materials can be obviously improved, and the cost of the raw materials is reduced;
(2) the method comprises the steps of obtaining a calcium carbide production carbon source in a hydro-gasification mode, wherein the fixed carbon content of the carbon source is high, the sulfur and nitrogen content in the carbon source can be obviously reduced, and the method is favorable for improving the quality of the calcium carbide, preparing acetylene by the subsequent calcium carbide and processing and utilizing downstream; meanwhile, oil gas products generated by hydro-gasification have high quality, and mainly contain rich methane gas and light tar;
(3) quicklime powder is used as a chilling agent for hydro-gasification, not only plays a role of a chilling agent, reduces the temperature of gasified semicoke, is convenient to convey, but also can fully utilize the sensible heat of a gasification product to preheat quicklime; the mixed material is directly fed into the entrained flow bed to produce the calcium carbide by combining a high-temperature conveying technology, so that the energy consumption of the calcium carbide production can be obviously reduced.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
FIG. 1 is a flow chart of the production process of the present invention;
fig. 2 is a schematic view of the production system of the present invention.
Detailed Description
The invention will be described in more detail with reference to the following figures and examples, so that the aspects and advantages of the invention can be better understood. However, the specific embodiments and examples described below are for illustrative purposes only and are not intended to limit the present invention.
The utility model provides a method for producing coal hydrogasification coupling calcium carbide, as shown in figure 1, comprising the following steps:
the first step is as follows: coal powder hydro-gasification: coal powder and hydrogen-rich gas are respectively sprayed into a gasification furnace through a coal powder nozzle and a hydrogen-rich gas nozzle, and after full mixing, a hydro-gasification reaction is carried out to obtain methane-rich gas, light tar and gasified semicoke, and then after chilling solid quicklime, a mixed material of the gasified semicoke and the quicklime and an oil gas product are obtained;
the granularity of the coal powder is less than 100 um; the particle size of the chilled quicklime is less than 1 mm;
the mass ratio of the coal powder to the hydrogen in the hydrogen-rich gas is 1: 0.2-0.5;
the temperature of the coal powder hydro-gasification reaction is 800-1000 ℃; the reaction pressure is 2-4MPa, and the gasification time is less than 2 s;
the second step is that: high-temperature conveying of mixed materials: the mixed material obtained by mixing the gasified semicoke and the chilled quicklime powder at the bottom of the gasification furnace is directly and thermally conveyed to a calcium carbide smelting unit, the sensible heat of the mixed material is fully utilized, and the energy consumption of calcium carbide production is reduced;
the hot conveying device is a closed heat-preservation ladle;
the temperature resistance of the material of the heat-insulating steel ladle is more than 900 ℃;
the third step: calcium carbide smelting: the mixed material conveyed by the high-temperature conveying device is directly sprayed into the entrained flow bed; meanwhile, oxygen-containing gas introduced from the lower side of the entrained flow bed enables part of the gasified semicoke to be combusted to generate heat, so that the gasified semicoke reacts with quick lime to generate calcium carbide.
The reaction temperature of the gasified semicoke and the quick lime is 1700-2000 ℃.
The utility model provides a system for coal hydrogasification coupling carbide production, as figure 2:
the system described in the utility model is composed of a coal hydrogenation gasification unit 1, a high temperature heat delivery unit 2 and an oxygen thermal method calcium carbide smelting unit 3.
The device of the coal hydro-gasification unit 1 is a gasification furnace and comprises a reaction zone 1-1, a chilling zone 1-2 and a mixed material storage zone 1-3;
the reaction zone 1-1 is provided with a reaction coal powder nozzle 11, a hydrogen-rich gas nozzle 12 and an oil gas outlet 13; the number of the hydrogen-rich gas nozzles 12 is even, and the hydrogen-rich gas nozzles are symmetrically arranged around the pulverized coal nozzle 11; the pulverized coal nozzle 11 is arranged at the top of the gasification furnace so as to fully mix pulverized coal and hydrogen-rich gas;
the chilling zone 1-2 is provided with a chilling quicklime powder nozzle 14; the chilling quicklime powder nozzle 14 is arranged on the wall of the gasification furnace below the reaction zone 1-1 of the gasification furnace so as to fully mix the gasified semicoke and the chilling quicklime powder; the number of the chilling quicklime powder nozzles 14 is even, and the chilling quicklime powder nozzles are symmetrically distributed around the gasification furnace;
the mixed material storage area 1-3 is provided with a mixed material baffle 15, a mixed material scraper 16 and a mixed material outlet 17; the included angle between the mixed material baffle and the horizontal plane is 30-75 degrees, so that the mixed material is discharged and the gasified semicoke and the quicklime powder are mixed conveniently; the mixed material outlet is arranged at the lower end of the gasification furnace so as to increase the distance between the discharge hole and the chilling quicklime powder inlet;
the device of the high-temperature solid conveying unit 2 is a closed heat-preservation ladle;
the temperature resistance of the material of the heat-insulating steel ladle is more than 900 ℃; the conveying mode of the closed heat-preservation ladle adopts a horizontal sliding rail and vertical lifting mode;
the device of the calcium carbide smelting unit 3 is an entrained flow bed and is provided with a feeding storage bin 3-1 and a reactor body 3-2; the feeding storage bin 3-1 is provided with a mixed material inlet 31 and a gate valve 32; the reactor body 3-2 is provided with an oxygen-enriched gas nozzle 33, a calcium carbide furnace gas outlet 34 and a calcium carbide outlet 35; the mixed material inlet 31 is connected with the mixed material outlet 17 of the coal hydro-gasification unit 1 through the high-temperature solid conveying device 2.
The invention will now be described with reference to specific examples, which are intended to be illustrative only and not to be limiting in any way.
Example 1
Utilize the system of the utility model, with the granularity less than 100um buggy and the hydrogen-rich gas respectively through nozzle 11 and nozzle 12 spout into the gasifier, the buggy with the mass ratio of hydrogen in the hydrogen-rich gas is 1:0.2, buggy and hydrogen-rich gas intensive mixing in descending process to take place gasification reaction under 900 ℃, pressure 3 MPa. When the reactant downwards runs to the chilling zone 1-2, the reactant is mixed with chilled quicklime powder; reducing the temperature of the gasification reaction product to be below 650 ℃, and simultaneously realizing the separation of gas and solid phases to obtain a mixed material; the mixed material enters a closed heat-preservation ladle from a mixed material outlet 17, is directly conveyed to a feeding storage bin of the entrained flow bed at high temperature, enters the entrained flow bed, oxygen-containing gas is sprayed from the side wall of the entrained flow bed to be fully contacted with the material, part of gasified semicoke and the oxygen-containing gas are mixed and combusted in the entrained flow bed, and the material is heated to 1850 ℃ to form the calcium carbide. The calcium carbide is discharged from an outlet at the bottom of the entrained flow bed.
Example 2
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Coal powder with the granularity of less than 100um and hydrogen-rich gas are respectively sprayed into the gasification furnace through a nozzle 11 and a nozzle 12, the mass ratio of the coal powder to the hydrogen-rich gas is 1:0.5, the coal powder and the hydrogen-rich gas are fully mixed in the descending process, and gasification reaction is carried out at the temperature of 1000 ℃ and the pressure of 3 MPa. When the reactant downwards runs to the chilling zone 1-2, the reactant is mixed with chilled quicklime powder; reducing the temperature of the gasification reaction product to be below 650 ℃, and simultaneously realizing the separation of gas and solid phases to obtain a mixed material; the mixed material enters a closed heat-preservation ladle from a mixed material outlet 17, is directly conveyed to a feeding storage bin of the entrained flow bed at high temperature, enters the entrained flow bed, oxygen-containing gas is sprayed from the side wall of the entrained flow bed to be fully contacted with the material, part of gasified semicoke and the oxygen-containing gas are mixed and combusted in the entrained flow bed, and the material is heated to 1900 ℃ to form the calcium carbide. The calcium carbide is discharged from an outlet at the bottom of the entrained flow bed.
Example 3
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Coal powder with the granularity of less than 100um and hydrogen-rich gas are respectively sprayed into the gasification furnace through a nozzle 11 and a nozzle 12, the mass ratio of the coal powder to the hydrogen-rich gas is 1:0.3, the coal powder and the hydrogen-rich gas are fully mixed in the descending process, and gasification reaction is carried out at the temperature of 800 ℃ and the pressure of 2 MPa. When the reactant downwards runs to the chilling zone 1-2, the reactant is mixed with chilled quicklime powder; reducing the temperature of the gasification reaction product to be below 650 ℃, and simultaneously realizing the separation of gas and solid phases to obtain a mixed material; the mixed material enters a closed heat-preservation ladle from a mixed material outlet 17, is directly conveyed to a feeding storage bin of the entrained flow bed at high temperature, enters the entrained flow bed, oxygen-containing gas is sprayed from the side wall of the entrained flow bed to be fully contacted with the material, part of gasified semicoke and the oxygen-containing gas are mixed and combusted in the entrained flow bed, and the material is heated to 2000 ℃ to form the calcium carbide. The calcium carbide is discharged from an outlet at the bottom of the entrained flow bed.
Example 4
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Coal powder with the granularity of less than 100um and hydrogen-rich gas are respectively sprayed into the gasification furnace through a nozzle 11 and a nozzle 12, the mass ratio of the coal powder to the hydrogen-rich gas is 1:0.4, the coal powder and the hydrogen-rich gas are fully mixed in the descending process, and gasification reaction is carried out at 850 ℃ and under the pressure of 4 MPa. When the reactant downwards runs to the chilling zone 1-2, the reactant is mixed with chilled quicklime powder; reducing the temperature of the gasification reaction product to be below 650 ℃, and simultaneously realizing the separation of gas and solid phases to obtain a mixed material; the mixed material enters a closed heat-preservation ladle from a mixed material outlet 17, is directly conveyed to a feeding storage bin of the entrained flow bed at high temperature, enters the entrained flow bed, oxygen-containing gas is sprayed from the side wall of the entrained flow bed to be fully contacted with the material, part of gasified semicoke and the oxygen-containing gas are mixed and combusted in the entrained flow bed, and the material is heated to 1700 ℃ to form the calcium carbide. The calcium carbide is discharged from an outlet at the bottom of the entrained flow bed.
Claims (6)
1. A system for coupled hydrogenation gasification and calcium carbide smelting comprises a hydrogenation gasification unit and a calcium carbide smelting unit; wherein,
the hydro-gasification unit comprises a coal powder nozzle, a hydrogen-rich gas nozzle, an oil gas outlet, a chilled quicklime powder nozzle and a mixed material outlet; in the hydro-gasification unit, coal powder and a product of hydro-gasification reaction of hydrogen-rich gas are chilled by solid quicklime to obtain a mixed material and an oil gas product;
the calcium carbide smelting unit comprises a mixed material inlet, an oxygen-enriched gas nozzle, a calcium carbide furnace gas outlet and a calcium carbide outlet, the mixed material inlet is connected with the mixed material outlet, and the calcium carbide smelting unit is used for reacting the mixed material to generate calcium carbide.
2. The system of claim 1,
the device used by the hydro-gasification unit is a gasification furnace,
the device used by the calcium carbide smelting unit is an entrained flow bed.
3. The system of claim 2,
the hydro-gasification unit comprises a reaction zone, a chilling zone and a mixed material storage zone;
the reaction zone is provided with the pulverized coal nozzle, the hydrogen-rich gas nozzle and the oil gas outlet; the number of the hydrogen-rich gas nozzles is an even number, and the hydrogen-rich gas nozzles are symmetrically arranged around the pulverized coal nozzles; the pulverized coal nozzle is arranged at the top of the gasification furnace;
the chilling zone is provided with the chilling quicklime powder nozzles, the chilling quicklime powder nozzles are arranged on the furnace wall below the reaction zone, and the chilling quicklime powder nozzles are even in number and symmetrically distributed around the gasification furnace;
the mixed material storage area is provided with a mixed material baffle, a mixed material scraper and a mixed material outlet, and the mixed material outlet is arranged at the bottom end of the gasification furnace.
4. The system of claim 3,
the system also comprises a high-temperature solid conveying unit, and the mixed material inlet is connected with the mixed material outlet through the high-temperature solid conveying unit.
5. The system of claim 4,
the device of the high-temperature solid conveying unit is a closed heat-preservation ladle, and the conveying mode of the closed heat-preservation ladle adopts a horizontal sliding rail and vertical lifting mode.
6. The system of claim 3 wherein the mixing material baffle is angled from 30 to 75 ° from horizontal.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201621332890.7U CN206318951U (en) | 2016-12-06 | 2016-12-06 | The system that a kind of hydrogasification coupling calcium carbide is smelted |
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| CN201621332890.7U CN206318951U (en) | 2016-12-06 | 2016-12-06 | The system that a kind of hydrogasification coupling calcium carbide is smelted |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106479573A (en) * | 2016-12-06 | 2017-03-08 | 北京神雾环境能源科技集团股份有限公司 | A kind of hydrogasification couples the system and method that carbide is smelted |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106479573A (en) * | 2016-12-06 | 2017-03-08 | 北京神雾环境能源科技集团股份有限公司 | A kind of hydrogasification couples the system and method that carbide is smelted |
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