CN107032354A - A kind of system and method for producing calcium carbide - Google Patents
A kind of system and method for producing calcium carbide Download PDFInfo
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- CN107032354A CN107032354A CN201710405397.6A CN201710405397A CN107032354A CN 107032354 A CN107032354 A CN 107032354A CN 201710405397 A CN201710405397 A CN 201710405397A CN 107032354 A CN107032354 A CN 107032354A
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- calcium carbide
- furnace
- coke
- gas
- blast pipe
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- 239000005997 Calcium carbide Substances 0.000 title claims abstract description 93
- 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 93
- 238000004519 manufacturing process Methods 0.000 title abstract description 21
- 239000000571 coke Substances 0.000 claims abstract description 56
- 239000011777 magnesium Substances 0.000 claims abstract description 37
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims abstract description 33
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 33
- 239000003463 adsorbent Substances 0.000 claims abstract description 28
- 238000002156 mixing Methods 0.000 claims abstract description 19
- 239000005439 thermosphere Substances 0.000 claims abstract description 16
- 150000001875 compounds Chemical class 0.000 claims abstract description 13
- 239000000779 smoke Substances 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 78
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 59
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 33
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 33
- 239000004571 lime Substances 0.000 claims description 33
- 239000000395 magnesium oxide Substances 0.000 claims description 30
- 238000001035 drying Methods 0.000 claims description 27
- 238000000034 method Methods 0.000 claims description 12
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 9
- 235000019738 Limestone Nutrition 0.000 claims description 9
- 239000006028 limestone Substances 0.000 claims description 9
- 239000003546 flue gas Substances 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000007254 oxidation reaction Methods 0.000 abstract description 12
- 230000003647 oxidation Effects 0.000 abstract description 5
- 238000001179 sorption measurement Methods 0.000 abstract description 2
- 238000005265 energy consumption Methods 0.000 abstract 1
- 239000000463 material Substances 0.000 description 16
- 239000002994 raw material Substances 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 239000012535 impurity Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 4
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Chemical compound O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- -1 magnesium nitride Chemical class 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 230000008018 melting Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229910052681 coesite Inorganic materials 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 229910052593 corundum Inorganic materials 0.000 description 2
- 229910052906 cristobalite Inorganic materials 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- 238000010079 rubber tapping Methods 0.000 description 2
- 229910052682 stishovite Inorganic materials 0.000 description 2
- 229910052905 tridymite Inorganic materials 0.000 description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 description 2
- 229910014813 CaC2 Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Abstract
The present invention discloses a kind of system and method for producing calcium carbide.The system includes mixing arrangement, furnace of calcium carbide, flue and adsorbent equipment；Furnace of calcium carbide includes body of heater, feed pipe and blast pipe；The inner chamber of body of heater includes thermosphere area, when furnace of calcium carbide works, and the temperature in thermosphere area is 1400~1600 DEG C；Blast pipe is located at thermosphere area, and blast pipe passes through the side wall and ft connection of body of heater；The feed pipe of the compound outlet connection furnace of calcium carbide of mixing arrangement, the gas outlet of the blast pipe of furnace of calcium carbide connects the inlet exhaust gas of flue, and the exhanst gas outlet of flue connects the smoke inlet of adsorbent equipment.The blast pipe of furnace of calcium carbide is arranged on thermosphere area by the present invention, it is to avoid the oxidation of magnesium vapor, semi-coke is dried using the high-temperature gas after adsorption and oxidation magnesium, production cost has been saved, reduces energy consumption.
Description
Technical field
The invention belongs to technical field of calcium carbide production, more particularly to a kind of system for improving calcium carbide production efficiency and side
Method.
Background technology
Calcium carbide is a kind of important industrial chemicals, at present, and the method for industrial production calcium carbide is mainly electrothermal way.Its first
The lime and coke for meeting calcium carbide production requirement carry out dispensing according to the specified ratio, and furnace charge then is delivered into electricity with bucket elevator
Stone stove furnace top bin, through charge tube to electric furnace charge, resistance heat of the furnace charge by electrode arc pad and furnace charge in electric furnace is anti-
Calcium carbide should be generated, calcium carbide timing is come out of the stove, puts to calcium carbide pot, after cooling, be broken into the granularity of certain specification requirement, that is, obtain
Finished product calcium carbide.
In the production process of calcium carbide, the impurity in raw material is serious to Influence of production.Impurity in raw material mainly includes oxygen
Change magnesium, silica, iron oxide, aluminum oxide etc., while furnace charge generates calcium carbide in electric reaction in furnace, various impurity are also carried out
Reaction.
The reaction of various impurity not only consumes electric energy and carbon materials, and influence operation, and destruction furnace bottom, particularly magnesia exist
Melting zone is reduced into rapidly magnesium metal, and melting zone is turned into a strong high temperature reduction area, and magnesium vapor is red-hot from this
When region is largely escaped, a portion magnesium reacts immediately with carbon monoxide, and generation magnesia releases heat-flash formation high temperature, office
Portion's duricrust is destroyed, and the liquid calcium carbide with impurity is corroded furnace bottom.
In calcium carbide production process, when being reacted after the magnesium cooling of generation with oxygen, substantial amounts of heat is released, charge level caking is hindered stove
Gas is discharged, and produces branch current.Local furnace shell is also destroyed, or even is destroyed molten Candle-stub, calcium carbide flow export is blocked.Practice card
Bright, content of magnesia often increases by 1% in lime, then power gas forming amount will decline 10~15L/kWh.Also partial oxidation magnesium exists
Melting zone reacts with nitrogen, the magnesium nitride (Mg of generation3N2), make calcium carbide tacky, cause difficulty of coming out of the stove, the normal production of influence.More have very
Person, might have the generation for material phenomenon of collapsing.
The content of the invention
In order to solve the above problems, the present invention provides a kind of system and method for producing calcium carbide, by the tail of traditional furnace of calcium carbide
Gas outlet is changed to blast pipe, and blast pipe is arranged on the side wall of furnace of calcium carbide, while adsorbent equipment absorptive collection magnesia is set, can
Production efficiency is effectively improved, cost is reduced.
The present invention provides a kind of system for producing calcium carbide, including mixing arrangement, furnace of calcium carbide, flue and adsorbent equipment；
The mixing arrangement includes dry semi-coke entrance, lime inlet and compound outlet；
The furnace of calcium carbide includes body of heater, feed pipe and blast pipe；The inner chamber of the body of heater includes thermosphere area, the furnace of calcium carbide
During work, the temperature in the thermosphere area is 1400~1600 DEG C；The feed pipe is deep into the stove at the top of the body of heater
The inner chamber of body；The blast pipe is located at the thermosphere area, and the blast pipe passes through the side wall and ft connection of the body of heater；It is described
Blast pipe includes baffle plate, and the baffle plate is inclined to be fixed on the air inlet tube wall of the blast pipe；
The flue includes inlet exhaust gas and exhanst gas outlet；The adsorbent equipment includes smoke inlet；
The feed pipe of the compound outlet connection furnace of calcium carbide of the mixing arrangement, the blast pipe of the furnace of calcium carbide goes out
Gas port connects the inlet exhaust gas of the flue, and the exhanst gas outlet of the flue connects the smoke inlet of the adsorbent equipment.
Further, system of the invention also includes drying device, and the drying device includes semi-coke entrance and dry semi-coke
Outlet, the dry semi-coke entrance of the dry semi-coke outlet connection mixing arrangement of the drying device.
As preferred embodiments of the present invention, the adsorbent equipment also includes high-temperature gas and exported, and the drying device includes
High-temperature gas entrance, the high-temperature gas entrance of the high-temperature gas outlet connection drying device of the adsorbent equipment.
Further, the system also includes calciner, and the calciner includes lime stone entrance and lime is exported,
The lime inlet of the lime outlet connection mixing arrangement of the calciner.
It is preferred that, the baffle plate of the blast pipe and the angle of horizontal direction are 30~60 °.In this way, so that discharge nozzle
Bottom bed of material formation partial cavity, is conducive to calcium carbide stove exhaust to be pooled in cavity, is discharged out of the furnace from escape pipe.
By the temperature control in thermosphere area at 1400~1600 DEG C to ensure 1400~1600 DEG C of calcium carbide stove exhaust discharge temperature,
So that the magnesium vapor in gas discharges out of the furnace together with the calcium carbide stove exhaust rich in CO, it is to avoid because magnesium vapor reacts in stove with CO
(Mg+CO=MgO+C) big calorimetric is released, charge level is lumpd, hinders furnace gas to discharge, and the material etc. that collapses.
After calcium carbide stove exhaust containing magnesium vapor discharges out of the furnace, rapid drop in temperature, when exhaust temperature be down to 1200 DEG C with
Under, react：Mg+CO=MgO+C, after tail gas is by adsorbent equipment, can output high value magnesia, remaining about 1000
~1200 DEG C of high-temperature tail gas is passed through semi-coke drying unit, dries thermal source as semi-coke, makes full use of high temperature calcium carbide stove exhaust to show
Heat, improves system energy efficiency.
On the other hand, the present invention provides a kind of method that utilization said system produces calcium carbide, comprises the following steps：
A, lime and dry semi-coke mixed, obtain compound, the mass ratio of lime and dry semi-coke is 0.8~1.1:
0.5~0.7；
B, the compound sent into furnace of calcium carbide, be heated to 2100~2300 DEG C, generation calcium carbide and the tail gas containing magnesium vapor；
C, the tail gas containing magnesium vapor by blast pipe discharged into the furnace of calcium carbide, then cooled down by flue, when cold
When but to less than 1200 DEG C, occur oxidation reaction, generate the flue gas containing magnesia；
D, the flue gas is sent into adsorbent equipment, absorptive collection magnesia discharges remaining high-temperature gas.
As preferred embodiments of the present invention, step is also included before step A：Semi-coke is sent into drying device, done
It is dry, obtain the dry semi-coke.
As preferred embodiments of the present invention, step is also included before step A：Lime stone is calcined, obtains described
Lime.
The method of the present invention, in addition to step：The high-temperature gas is sent into the drying device, dried as semi-coke
Thermal source.
Further, the temperature of the high-temperature gas is 1000~1200 DEG C.
In the present invention, " dry semi-coke " refer to moisture content be ＜ 2%, such as moisture content be 1% or 2%, dry semi-coke.This hair
" semi-coke " in bright refers to that moisture content is 5~18%, such as moisture content is 5%, 18%, or 6%, semi-coke.
The system and method for the production calcium carbide of the present invention, blast pipe is arranged on the thermosphere area of furnace of calcium carbide, the temperature in thermosphere area
Degree interval can ensure that with CO oxidation reaction does not occur for magnesium vapor in tail gas, it is to avoid the generation of charge level caking and the material that collapses；Row
Baffle plate is provided with the tube wall of the air inlet of tracheae, partial cavity can be formed in the bed of material, tail gas is pooled in cavity, is easy to receive
Discharged after collection；Using dust-removal cloth-bag adsorption and oxidation magnesium, high added value byproduct can be obtained；Remaining high-temperature gas is used for semi-coke
Dry, can effectively reduce energy resource consumption.
Brief description of the drawings
Fig. 1 is the structural representation of the system of the embodiment of the present invention；
Fig. 2 is the furnace of calcium carbide structure chart of the embodiment of the present invention；
Fig. 3 is the flow chart of the method for the embodiment of the present invention.
Embodiment
Below in conjunction with drawings and examples, the embodiment to the present invention is described in more details, so as to energy
Enough more fully understand the advantage of the solution of the present invention and its various aspects.However, specific embodiments described below and implementation
Example is only the purpose of explanation, rather than limitation of the present invention.
As shown in figure 1, the embodiment of the present invention provides a kind of system for producing calcium carbide, including drying device 1, calciner 2,
Mixing arrangement 3, furnace of calcium carbide 4, flue 5 and adsorbent equipment 6.The system of the production calcium carbide is obtained by the cooperation between each device
While calcium carbide, the magnesia of high added value is have collected, the tail gas of high temperature is make use of again, production cost is saved.
Drying device 1 is in the present embodiment dryer, including semi-coke entrance 11, dry semi-coke export 12, high-temperature gas and entered
Mouth 13 and offgas outlet 14.In actual production, the water content of semi-coke is larger, it is necessary to semi-coke is dried drying device 1, obtains
Dry semi-coke.
Calciner 2 selects gas base sleeve kiln, including lime stone entrance 21, lime outlet 22 and combustion gas in the present embodiment
Import 23.After lime stone is fired, the lime needed for production calcium carbide can be obtained.Fuel gas inlet 23 is used to provide for calciner 2
Energy.
The blending bunker that mixing arrangement 3 is selected, including dry semi-coke entrance 31, lime inlet 32 and compound outlet 33, are dried
The dry semi-coke outlet 12 of device 1 connects the dry semi-coke entrance 31 of mixing arrangement 3, the connection mixing of lime outlet 22 of calciner 2
The lime inlet 32 of device 3.Mixing arrangement 3 is mixed dry semi-coke and lime, compound is obtained, for producing calcium carbide.
As shown in Fig. 2 furnace of calcium carbide 4 includes body of heater 41, electrode 42, feed pipe 43, blast pipe 44 and calcium carbide outlet 45, mixing
The compound outlet 33 of device 3 connects the feed pipe 43 of furnace of calcium carbide.Furnace of calcium carbide utilizes blast pipe 44 by the tail gas containing magnesium vapor
Discharge body of heater, it is to avoid the oxidation reaction of magnesia and CO in body of heater.
The inside of body of heater 41 is cavity, and when producing calcium carbide, the temperature of the internal cavity of body of heater 41 is gradually reduced from bottom to top.Root
According to cavity temperature during production calcium carbide, cavity is from top to bottom divided into bed of material area 411, thermosphere area 412 and reaction zone 413,
The temperature in thermosphere area is 1400~1600 DEG C.In 1400~1600 DEG C of temperature range, it is ensured that the magnesium vapor in tail gas is not
Occurs oxidation reaction with CO.Bed of material area 411 is the preheating zone of material, the gas (calcium carbide that material rises in bed of material area 411 and bottom
Reaction of formation：3C+CaO=CO+CaC2, the gas is CO) and carry out heat exchange.The temperature of reaction zone 413 is in 2200 DEG C or so, thing
Material reacts in this region, generates calcium carbide, while reduction reaction occurs for the magnesia in impurity, generates magnesium vapor.
Electrode 42 is embedded in the top of furnace roof 41, the cavity for extending to body of heater, but is not contacted with furnace bottom, is the production of calcium carbide
Energy is provided.
Feed pipe 43 is deep into the inner chamber of body of heater 41 at the top of body of heater.Feed pipe 43 is used to send into material in body of heater.
Feed pipe 43 is arranged symmetrically on the both sides of electrode 42, and the material that may be such that into body of heater is uniformly heated, and is conducive to improving and gives birth to
Efficiency is produced, the energy is saved.
Blast pipe 44 is located at thermosphere area 412, for extracting the tail gas containing magnesium vapor out.Blast pipe 44 passes through the side wall of body of heater 41
With ft connection.Blast pipe 44 includes baffle plate, and the baffle plate is inclined to be fixed on the air inlet tube wall of blast pipe 44.Baffle plate with
The angle of horizontal plane is 30~60 °, and such design can be in material bed middle formation cavity area, and be easy to tail gas is pooled to sky
Cavity region, is discharged to outside stove from blast pipe.
Body of heater is discharged for calcium carbide in the bottom of furnace of calcium carbide 4 provided with calcium carbide outlet 45.
Flue 5 includes inlet exhaust gas 51 and exhanst gas outlet 52, and the blast pipe 44 of furnace of calcium carbide connects the inlet exhaust gas of flue 5
51.The tail gas containing magnesium vapor for discharging body of heater by blast pipe 44 enters flue 5, rapid drop in temperature, when containing magnesium vapor
Exhaust temperature when being down to less than 1200 DEG C, react：Mg+CO=MgO+C, generates magnesia.
Adsorbent equipment 6 includes smoke inlet 61 and high-temperature gas outlet 62, the connection adsorbent equipment of exhanst gas outlet 52 of flue 5
6 smoke inlet 61.The magnesia produced in flue 5 together enters adsorbent equipment 6 with other tail gas, and adsorbent equipment 6, which has, to be inhaled
Attached function, adsorbable collection magnesia discharges remaining gas.The device of the embodiment of the present invention, not only avoid carbide raw material
The influence that middle oxidation magnesium addition is produced to calcium carbide, and the accessory substance magnesia of high added value is collected, obtain bigger economy
Benefit.
The high-temperature gas outlet 62 of adsorbent equipment 6 connects the high-temperature gas entrance 13 of drying device 1.Adsorbent equipment 6 is adsorbed
After magnesia, remaining high-temperature gas can be transported to drying device 1, as the heat energy for drying semi-coke, realize high-temperature tail gas
Recycle.The offgas outlet 14 of drying device 1 can connect the fuel gas inlet 23 of calciner 2, and tail gas is as combustible gas, for roasting
Device 2 provides energy.
As shown in figure 3, the another object of the embodiment of the present invention is to provide a kind of method that utilization said system produces calcium carbide,
Comprise the following steps：
1st, semi-coke is sent into drying device, be dried, obtain dry semi-coke；Lime stone is calcined, lime is obtained.
2nd, lime and dry semi-coke are mixed, acquisition compound, the mass ratio of lime and dry semi-coke is 0.8~1.1:
0.5~0.7.
3rd, furnace of calcium carbide is fed the mixture into, 2100~2300 DEG C are heated to, calcium carbide and the tail gas containing magnesium vapor is generated.
4th, the tail gas containing magnesium vapor is discharged into furnace of calcium carbide by blast pipe, then cooled down by flue, occur oxidation reaction,
Generate the flue gas containing magnesia.
5th, flue gas is sent into adsorbent equipment, absorptive collection magnesia discharges remaining high-temperature gas.
6th, high-temperature gas is sent into drying device, the thermal source dried as semi-coke, the temperature of high-temperature gas for 1000~
1200℃。
Embodiment 1
1st, the moisture content 6~12% of semi-coke, block semi-coke is dried using chain-and-slat drying machine, the height discharged with adsorbent equipment
Wet body is thermal source, and semi-coke moisture content is 1~2% after drying, and lime stone is calcined using gas base sleeve kiln, and fuel is to dry semi-coke
Tail gas afterwards.Lime composition is as shown in table 1 below after roasting.
The lime constituent analysis of table 1
| TFe/% | CaO/% | MgO/% | SiO2/ % | Al2O3/ % | MnO2/ % | SO3/ % | P2O5/ % | Other/% |
| 0.32 | 91.7 | 2.41 | 1.62 | 0.55 | 0.11 | 0.02 | 0.03 | 3.24 |
2nd, dried block semi-coke and the block lime being calcined out are well mixed, the mass ratio of lime and semi-coke is
0.8：0.5, mixed material is sent into furnace of calcium carbide through conveying device.
3rd, furnace of calcium carbide heats raw material using the heat release of electrode open arc, and raw material is heated into 2300 DEG C or so, produces calcium carbide, simultaneously
Tail gas of the output containing magnesium vapor, is discharged outside furnace of calcium carbide, blast pipe top by the blast pipe for being arranged at furnace of calcium carbide side middle and lower part
The downward baffle plate of setting level, baffle plate is 60 ° with horizontal line angle.
4th, the tail gas tapping temperature containing magnesium vapor is 1600 DEG C or so, and after flue, exhaust temperature is down to 1200 DEG C of left sides
Oxidation reaction occurs for the magnesium in the right side, tail gas, generates magnesia.
5th, the flue gas of the magnesia containing magnesium enters adsorbent equipment, obtains the high added value magnesia production of by-product content about 64%
Product.Contain calcium carbide 81.24%, gas forming amount 306L/kg in product calcium carbide.
Embodiment 2
1st, the moisture content 6~12% of semi-coke, block semi-coke is dried using chain-and-slat drying machine, the height discharged with adsorbent equipment
Wet body is thermal source, and semi-coke moisture content is 1~2% after drying, and lime stone is calcined using gas base sleeve kiln, and fuel is to dry semi-coke
Tail gas afterwards.Lime composition is as shown in table 1 below after roasting.
The lime constituent analysis of table 1
| TFe/% | CaO/% | MgO/% | SiO2/ % | Al2O3/ % | MnO2/ % | SO3/ % | P2O5/ % | Other/% |
| 0.31 | 91.5 | 2.44 | 1.62 | 0.52 | 0.11 | 0.03 | 0.03 | 3.26 |
2nd, dried block semi-coke and the block lime being calcined out are well mixed, the mass ratio of lime and semi-coke is
1.1：0.7, mixed material is sent into furnace of calcium carbide through conveying device.
3rd, furnace of calcium carbide heats raw material using the heat release of electrode open arc, and raw material is heated into 2100 DEG C or so, produces calcium carbide, simultaneously
Tail gas of the output containing magnesium vapor, is discharged outside furnace of calcium carbide, blast pipe top by the blast pipe for being arranged at furnace of calcium carbide side middle and lower part
The downward baffle plate of setting level, baffle plate is 45 ° with horizontal line angle.
4th, the tail gas tapping temperature containing magnesium vapor is 1500 DEG C or so, and after flue, calcium carbide stove exhaust temperature is down to
1000 DEG C or so, oxidation reaction occurs for the magnesium in tail gas, generates magnesia.
5th, the flue gas containing magnesia enters adsorbent equipment, obtains the high added value magnesium oxide product of by-product content about 63%.
Contain calcium carbide 81.42%, gas forming amount 303L/kg in product calcium carbide.
It should be noted that each embodiment above by reference to described by accompanying drawing is only to illustrate rather than limitation originally
The scope of invention, it will be understood by those within the art that, it is right under the premise without departing from the spirit and scope of the present invention
Modification or equivalent substitution that the present invention is carried out, all should cover within the scope of the present invention.In addition, signified unless the context
Outside, the word occurred in the singular includes plural form, and vice versa.In addition, unless stated otherwise, then any embodiment
All or part of can combine all or part of of any other embodiment to use.
Claims (10)
1. a kind of system for producing calcium carbide, it is characterised in that including mixing arrangement, furnace of calcium carbide, flue and adsorbent equipment；
The mixing arrangement includes dry semi-coke entrance, lime inlet and compound outlet；
The furnace of calcium carbide includes body of heater, feed pipe and blast pipe；The inner chamber of the body of heater includes thermosphere area, the furnace of calcium carbide work
When, the temperature in the thermosphere area is 1400~1600 DEG C；The feed pipe is deep into the body of heater at the top of the body of heater
Inner chamber；The blast pipe is located at the thermosphere area, and the blast pipe passes through the side wall and ft connection of the body of heater；The exhaust
Pipe includes baffle plate, and the baffle plate is inclined to be fixed on the air inlet tube wall of the blast pipe；
The flue includes inlet exhaust gas and exhanst gas outlet；
The adsorbent equipment includes smoke inlet；
The feed pipe of the compound outlet connection furnace of calcium carbide of the mixing arrangement, the gas outlet of the blast pipe of the furnace of calcium carbide
The inlet exhaust gas of the flue is connected, the exhanst gas outlet of the flue connects the smoke inlet of the adsorbent equipment.
2. system according to claim 1, it is characterised in that further comprise drying device, the drying device includes
Semi-coke entrance and the outlet of dry semi-coke, the dry semi-coke entrance of the dry semi-coke outlet connection mixing arrangement of the drying device.
3. system according to claim 2, it is characterised in that the adsorbent equipment also includes high-temperature gas and exported, described
Drying device includes high-temperature gas entrance, the high-temperature gas of the high-temperature gas outlet connection drying device of the adsorbent equipment
Entrance.
4. system according to claim 1, it is characterised in that further comprise calciner, the calciner includes
Lime stone entrance and lime outlet, the lime inlet of the lime outlet connection mixing arrangement of the calciner.
5. system according to claim 1, it is characterised in that the baffle plate of the blast pipe and the angle of horizontal direction are 30
~60 °.
6. a kind of method that any system of utilization Claims 1 to 55 produces calcium carbide, it is characterised in that including step：
A, lime and dry semi-coke mixed, obtain compound, the mass ratio of lime and dry semi-coke is 0.8~1.1:0.5~
0.7；
B, the compound sent into furnace of calcium carbide, be heated to 2100~2300 DEG C, generation calcium carbide and the tail gas containing magnesium vapor；
C, the tail gas containing magnesium vapor by blast pipe discharged into the furnace of calcium carbide, then cooled down, aoxidized by flue
Reaction, generates the flue gas containing magnesia；
D, the flue gas is sent into adsorbent equipment, absorptive collection magnesia discharges remaining high-temperature gas.
7. method according to claim 6, it is characterised in that also include step before step A：Semi-coke is sent into drying
Device, is dried, and obtains the dry semi-coke.
8. method according to claim 6, it is characterised in that also include step before step A：Lime stone is roasted
Burn, obtain the lime.
9. method according to claim 7, it is characterised in that also including step：High-temperature gas feeding is described dry
Dry device, the thermal source dried as semi-coke.
10. method according to claim 9, it is characterised in that the temperature of the high-temperature gas is 1000~1200 DEG C.
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