CN107055539A - A kind of system for producing calcium carbide and method for removing magnesia - Google Patents
A kind of system for producing calcium carbide and method for removing magnesia Download PDFInfo
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- CN107055539A CN107055539A CN201710400187.8A CN201710400187A CN107055539A CN 107055539 A CN107055539 A CN 107055539A CN 201710400187 A CN201710400187 A CN 201710400187A CN 107055539 A CN107055539 A CN 107055539A
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- calcium carbide
- furnace
- calcium
- gas
- pelletizing
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- 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 77
- 239000005997 Calcium carbide Substances 0.000 title claims abstract description 76
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 title claims abstract description 61
- 239000000395 magnesium oxide Substances 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000000197 pyrolysis Methods 0.000 claims abstract description 57
- 239000011777 magnesium Substances 0.000 claims abstract description 29
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims abstract description 27
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 27
- 239000003463 adsorbent Substances 0.000 claims abstract description 23
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- 239000005439 thermosphere Substances 0.000 claims abstract description 16
- 239000007787 solid Substances 0.000 claims abstract description 9
- 239000000779 smoke Substances 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 85
- 239000000463 material Substances 0.000 claims description 61
- 238000005453 pelletization Methods 0.000 claims description 40
- 239000003245 coal Substances 0.000 claims description 37
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 30
- 229910052791 calcium Inorganic materials 0.000 claims description 30
- 239000011575 calcium Substances 0.000 claims description 30
- 239000002994 raw material Substances 0.000 claims description 15
- 238000001035 drying Methods 0.000 claims description 12
- 239000011343 solid material Substances 0.000 claims description 12
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 11
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 11
- 239000004571 lime Substances 0.000 claims description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 8
- 239000003546 flue gas Substances 0.000 claims description 7
- 235000019738 Limestone Nutrition 0.000 claims description 4
- 239000006028 limestone Substances 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 239000002893 slag Substances 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 16
- 238000007254 oxidation reaction Methods 0.000 abstract description 11
- 230000003647 oxidation Effects 0.000 abstract description 5
- 238000001179 sorption measurement Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 7
- 239000012535 impurity Substances 0.000 description 6
- 239000000203 mixture Substances 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 230000008018 melting Effects 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
- 230000008901 benefit Effects 0.000 description 2
- -1 magnesium nitride Chemical class 0.000 description 2
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Chemical compound O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000012265 solid product Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 229910014813 CaC2 Inorganic materials 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 229910052906 cristobalite Inorganic materials 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
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- HZZOEADXZLYIHG-UHFFFAOYSA-N magnesiomagnesium Chemical compound [Mg][Mg] HZZOEADXZLYIHG-UHFFFAOYSA-N 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
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000010079 rubber tapping Methods 0.000 description 1
- 238000007493 shaping process Methods 0.000 description 1
- 229910052682 stishovite Inorganic materials 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
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Abstract
The present invention discloses a kind of system for producing calcium carbide and method for removing magnesia.The system includes pyrolysis oven, 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 solid matter outlet of pyrolysis oven connects the feed pipe of furnace of calcium carbide, and 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 system and method for the production calcium carbide of the present invention, is arranged on thermosphere area by the blast pipe of furnace of calcium carbide, it is to avoid the oxidation of magnesium vapor, by the use of the High Temperature Gas after adsorption and oxidation magnesium as the thermal source of pyrolytic reaction, has saved production cost, reduce energy consumption.
Description
Technical field
The invention belongs to technical field of calcium carbide production, more particularly to a kind of system for producing calcium carbide for removing magnesia and side
Method.
Background technology
Calcium carbide is a kind of important industrial chemicals, in the production process of calcium carbide, and the impurity in raw material is tight to Influence of production
Weight.Impurity in raw material mainly includes magnesia, silica, iron oxide, aluminum oxide etc., when furnace charge is in electric reaction in furnace generation carbon
While changing calcium, various impurity are also reacted.
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, present invention proposition is a kind of can to remove system and the side of magnesia in calcium carbide production process
Method, the blast pipe of furnace of calcium carbide is arranged on the side wall in thermosphere area, is prevented effectively from the oxidation reaction of magnesium in stove, improves production effect
Rate, while obtaining high value-added product.
The present invention provides a kind of system for producing calcium carbide for removing magnesia, including pyrolysis oven, furnace of calcium carbide, flue and absorption dress
Put；
The pyrolysis oven includes spherical material entrance and solid matter 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, the inclined air inlet for being fixed on the blast pipe of the baffle plate；
The flue includes inlet exhaust gas and exhanst gas outlet；
The adsorbent equipment includes smoke inlet；
The solid matter outlet of the pyrolysis oven connects the feed pipe of the furnace of calcium carbide, and 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 adsorbent equipment.
Further, system of the invention includes pretreatment unit, and the pretreatment unit includes drying device, roasting dress
Put and palletizing device；
The drying device includes raw coal entrance and pelletizing raw coal is exported；
The calciner includes calcium based raw material entrance and pelletizing calcium material is exported；
The palletizing device includes pelletizing raw coal entrance, pelletizing calcium material entrance and the outlet of spherical material；
The pelletizing raw coal entrance of the pelletizing raw coal outlet connection palletizing device of the drying device, the calciner
The pelletizing calcium material outlet connection palletizing device pelletizing calcium material entrance, the spherical material outlet connection of the palletizing device is described
The spherical material entrance of pyrolysis oven.
As preferred embodiments of the present invention, the adsorbent equipment also includes High Temperature Gas and exported, and the pyrolysis oven includes high temperature
Gas entrance, the High Temperature Gas entrance of the High Temperature Gas outlet connection pyrolysis oven of the adsorbent equipment.
As preferred embodiments of the present invention, the baffle plate of the blast pipe and the angle of horizontal direction are 30~60 °.
It is preferred that, the pyrolysis oven also includes being located at the pyrolysis oil gas vent at the top of the pyrolysis oven.
It is a further object of the present invention to provide a kind of method that utilization said system produces calcium carbide, comprise the following steps：
A, by spherical material send into pyrolysis oven, occur pyrolytic reaction, obtain solid material；
B, the solid material sent into furnace of calcium carbide, be heated to 2100~2300 DEG C, generation calcium carbide and the tail containing magnesium vapor
Gas；
C, the tail gas containing magnesium vapor by blast pipe discharged into the furnace of calcium carbide, then cooled down, occurred by flue
Oxidation reaction, generates the flue gas containing magnesia；
D, the flue gas is sent into adsorbent equipment, absorptive collection magnesia discharges remaining High Temperature Gas, the temperature of High Temperature Gas
Reach 1000-1200 DEG C.
Further, pyrolysis reaction temperature is 500-900 DEG C, preferably 600-800 DEG C.
As preferred scheme, step is included before step A：Raw coal is dried, pelletizing raw coal is obtained；By calcium base
Raw material is calcined, and obtains pelletizing calcium material；Pelletizing after the pelletizing raw coal and pelletizing calcium material are mixed, obtains spherical material.
Specifically, the calcium based raw material includes the one or more in lime, lime stone, white lime and carbide slag.
Further, method of the invention also includes step：The High Temperature Gas is sent into the pyrolysis oven, it is anti-as pyrolysis
The thermal source answered.
Further, the pyrolytic reaction of the step A also generates pyrolysis oil gas, collects described by being pyrolyzed oil gas vent
It is pyrolyzed oil gas.
Shaping rear profile ball is sent into pyrolysis unit, type ball is warming up to 500~900 DEG C by thermal source of high temperature calcium carbide stove exhaust
Generation pyrolytic reaction, 500~900 DEG C of high-temp solid products of output, while the pyrolysis gas and tar of by-product high added value, pyrolysis gas
It can be sold as combustion gas or material gas, tar as product or deep processing raw material, high-temp solid product is heat-fed to calcium carbide smelting
Refine unit.
The system for producing calcium carbide and method for the removing magnesia that the present invention is provided, blast pipe are arranged on the thermosphere of furnace of calcium carbide
Area, the temperature range in thermosphere area can ensure that with CO oxidation reaction does not occur for the magnesium vapor in tail gas, it is to avoid charge level caking and
Collapse the generation of material；Baffle plate is provided with the tube wall of the air inlet of blast pipe, partial cavity can be formed in the bed of material, tail gas is pooled to
In cavity, it is easy to discharge after collecting；Using dust-removal cloth-bag adsorption and oxidation magnesium, high added value byproduct can be obtained；Because pyrolysis is anti-
It is 500-900 DEG C to answer temperature, and the temperature for the high-temperature gas discharged from adsorbent equipment reaches 1000-1200 DEG C, therefore the present invention will inhale
The attached remaining High Temperature Gas of magnesia is used for the pyrolysis of spherical material, realizes the recycling of waste gas sensible heat, reduces production cost, improves
System energy utilization ratio.
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 for removing magnesia, including pretreatment unit
1st, pyrolysis oven 2, furnace of calcium carbide 3, flue 4 and adsorbent equipment 5.The solid material of production calcium carbide is obtained using pyrolysis oven 2, it is simultaneously raw
Heat production solution oil gas.Furnace of calcium carbide 3 discharges the tail gas containing magnesium vapor while producing calcium carbide, is aoxidized after handling tail gas
Magnesium, remaining High Temperature Gas can provide heat for the pyrolytic reaction of pyrolysis oven.
Pretreatment unit 1 includes drying device 11, calciner 02 and palletizing device 13.Pretreatment unit 1 is pyrolysis oven
Raw material is provided.
Drying device 11 includes raw coal entrance 111 and pelletizing raw coal outlet 112.Drying device 11 is used for former to carbon-based raw material
Coal is dried, and obtains pelletizing raw coal.
Calciner 12 includes calcium based raw material entrance 121 and pelletizing calcium material outlet 122.Calciner 102 can be to calcium base
Material roasting, obtains pelletizing calcium material.
Palletizing device 13 includes pelletizing raw coal entrance 131, pelletizing calcium material entrance 132 and spherical material outlet 133, drying device
Pelletizing raw coal outlet 112 connect palletizing devices pelletizing raw coal entrances 131, calciner pelletizing calcium material outlet 122 connect
The pelletizing calcium material entrance 132 of palletizing device.The pelletizing calcium material that the pelletizing raw coal and calciner 12 that drying device 11 is produced are produced,
Palletizing device 13 is sent into, the spherical material needed for pyrolysis oven is obtained.
Pyrolysis oven 2 includes spherical material entrance 21, solid matter outlet 22 and pyrolysis oil gas vent 23, the ball of palletizing device 13
The spherical material entrance 21 of shape material outlet connection pyrolysis oven 2.Spherical material enters after pyrolysis oven 2, is heated and occurs pyrolytic reaction, and generation is solid
Body material and pyrolysis oil gas.Solid material discharges pyrolysis oven 2 by solid matter outlet 22.Pyrolysis oil gas is gone out by being pyrolyzed oil gas
Mouthfuls 23 are collected, and after handling the pyrolysis oil gas of collection, can obtain the oil gas product of high added value.
As depicted in figs. 1 and 2, furnace of calcium carbide 3 includes body of heater 31, electrode 32, feed pipe 33, blast pipe 34 and calcium carbide outlet
35, the solid matter outlet of pyrolysis oven 2 connects the feed pipe 33 of furnace of calcium carbide 3.Solid material is heated to height in furnace of calcium carbide 3
Temperature, reacts, and generates calcium carbide, is discharged by calcium carbide outlet 35.
The inside of body of heater 31 is cavity, and when producing calcium carbide, the temperature of the internal cavity of body of heater 31 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 311, thermosphere area 312 and reaction zone 313,
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 311 is the preheating zone of material, and material is carried out in the gas that bed of material area 311 and bottom rise
Heat exchange (calcium carbide reaction of formation：3C+CaO=CO+CaC2, the gas is CO).The temperature of reaction zone 313 at 2000 DEG C or so,
Material reacts in this region, generates calcium carbide, while reduction reaction occurs for the magnesia in impurity, generates magnesium vapor.
Electrode 32 is embedded in the top of furnace roof 31, the cavity for extending to body of heater 31, but is not contacted with furnace bottom, is the life of calcium carbide
Production provides energy.
Feed pipe 33 is deep into the inner chamber of body of heater 31 at the top of body of heater.Feed pipe 33 is used to send into material in body of heater.
Feed pipe 33 is arranged in around electrode 32, and the solid material that may be such that into body of heater is distributed in surrounding them, is conducive to improving
Production efficiency, saves the energy.
Blast pipe 34 is located at thermosphere area 312, for extracting the tail gas containing magnesium vapor out.Blast pipe 34 passes through the side wall of body of heater 31
With ft connection.Blast pipe 34 includes baffle plate, and the baffle plate is inclined to be fixed on the air inlet tube wall of blast pipe 34.Baffle plate with
The angle of horizontal plane is 30~60 °, and such design can be easy to tail gas to be pooled to cavity in material bed middle formation cavity area
Region, is discharged to outside stove from blast pipe.
Flue 4 includes inlet exhaust gas 41 and exhanst gas outlet 42, and the blast pipe 34 of furnace of calcium carbide connects the inlet exhaust gas of flue 4
41.The tail gas containing magnesium vapor for discharging body of heater by blast pipe 34 enters flue 4, 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 5 includes smoke inlet 51, High Temperature Gas outlet 52 and products export 53, and the exhanst gas outlet 42 of flue 4 connects
Connect the smoke inlet 51 of adsorbent equipment 5.The magnesia produced in flue 4 together enters adsorbent equipment 5, absorption dress with other tail gas
Putting 5 has adsorption function, and adsorbable collection magnesia discharges remaining gas.The device of the embodiment of the present invention, not only avoid
The influence that magnesium addition is produced to calcium carbide is aoxidized in carbide raw material, and collects the accessory substance magnesia of high added value, is obtained more
Big economic benefit.The magnesia that adsorbent equipment 5 is collected is discharged by products export 53.
High Temperature Gas entrance 24 is additionally provided with pyrolysis oven 2, the High Temperature Gas outlet 52 of adsorbent equipment 5 connects the high temperature of pyrolysis oven 2
Gas entrance 24.After the absorptive collection magnesia of adsorbent equipment 5, remaining high-temperature tail gas is sent into pyrolysis oven 2, pyrolytic reaction is used as
Thermal source, realize the recycling of remaining High Temperature Gas, save production cost.
As shown in figure 3, on the other hand, the embodiment of the present invention provides a kind of method that utilization said system produces calcium carbide, bag
Include following steps：
1st, low order raw coal in powdery is dried, after powdered calcium based raw material is calcined, be well mixed, pelletizing raw coal and
The mass ratio of pelletizing calcium material is 0.6~1.4:1, preferably 0.8~1:1；Mixture carries out pelletizing, obtains spherical material.
2nd, spherical material is sent into pyrolysis oven, 500~900 DEG C of generation pyrolytic reactions obtain solid material and pyrolysis oil gas.
3rd, solid material is sent into furnace of calcium carbide, is heated to 2100~2300 DEG C, generate calcium carbide and the tail gas containing magnesium vapor；Will
Calcium carbide stove exhaust outlet is arranged on lower section in the bed of material so that 1400 DEG C of calcium carbide stove exhaust temperature ＞.
4th, the tail gas containing magnesium vapor is discharged into the furnace of calcium carbide by blast pipe, then cooled down by flue, at 1200 DEG C
Oxidation reaction is occurred below, the flue gas containing magnesia is generated.
5th, flue gas is sent into adsorbent equipment, absorptive collection magnesia discharges remaining High Temperature Gas.
6th, remaining about 1000~1200 DEG C of high temperature calcium carbide stove exhaust sends into pyrolysis unit by pipeline, is used as pyrolysis-type
Ball thermal source.
Specifically, in the embodiment of the present invention, the calcium based raw material is included in lime, lime stone, white lime and carbide slag
It is one or more.
The pyrolysis oil gas obtained in above-mentioned steps 2, can further be finished, obtain high added value oil gas into
Product.
Embodiment 1
Middle low order fine coal, using somewhere jet coal, composition such as table 1, in table 1, As-received refers to the state for receiving coal, one
As coal a large amount of water can be sprayed in exploitation and transportation, so, the measure of full water is the coal of As-received；Butt refer to by
The coal benchmark that coal is obtained after fully drying, now substantially without moisture in coal.
The jet coal composition of table 1
| Project | Unit | Numerical value | Remarks |
| Quan Shui | Wt% | 5.33 | As-received |
| Fixed carbon | Wt% | 55.7 | Butt |
| Volatile matter | Wt% | 37.2 | Butt |
| Ash content | Wt% | 7.1 | Butt |
Lime stone is calcined, lime, stone ash composition such as table 2 is obtained：
The lime composition of table 2
| 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 |
1st, after jet coal is dried, it is well mixed with lime, the mass ratio of jet coal and lime is 0.93：1, mixed
Material, pelletizing processing is carried out to mixed material, obtains spherical material.
2nd, spherical material is delivered into pyrolysis oven, spherical material is heated to by the High Temperature Gas discharged using adsorbent equipment as pyrolysis thermal source
700 DEG C or so, occur the pyrolysis gas and pyrolysis oil of pyrolytic reaction, output solid material and high added value.
3rd, high-temp solid material is delivered in closed calcium carbide furnace, material is heated to 2200 DEG C by the heat release of electrode open arc
Left and right, produces calcium carbide, while the tail gas containing magnesium vapor of the high temperature of output；Tail gas is by being arranged at furnace of calcium carbide side middle and lower part
Blast pipe discharge furnace of calcium carbide outside, blast pipe top sets the downward baffle plate of level, and baffle plate is 45 °, calcium carbide with horizontal line angle
The tail gas tapping temperature containing magnesium vapor is 1500 DEG C or so in stove.
4th, after the tail gas containing magnesium vapor is by flue, temperature is down to 1200 DEG C or so, and oxidation reaction, generation oxidation occur for magnesium
Magnesium.
5th, the flue gas containing magnesia enters adsorbent equipment, obtains the high added value magnesium oxide product of by-product content about 60%.
Contain calcium carbide 81.26%, gas forming amount 302L/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 for removing magnesia, it is characterised in that including pyrolysis oven, furnace of calcium carbide, flue and absorption dress
Put；
The pyrolysis oven includes spherical material entrance and solid matter 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, the inclined air inlet for being fixed on the blast pipe of the baffle plate；
The flue includes inlet exhaust gas and exhanst gas outlet；
The adsorbent equipment includes smoke inlet；
The solid matter outlet of the pyrolysis oven connects the feed pipe of the furnace of calcium carbide, 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 adsorbent equipment.
2. system according to claim 1, it is characterised in that further comprise pretreatment unit, the pretreatment unit
Including drying device, calciner and palletizing device；
The drying device includes raw coal entrance and pelletizing raw coal is exported；
The calciner includes calcium based raw material entrance and pelletizing calcium material is exported；
The palletizing device includes pelletizing raw coal entrance, pelletizing calcium material entrance and the outlet of spherical material；
The pelletizing raw coal entrance of the pelletizing raw coal outlet connection palletizing device of the drying device, the calciner is made
The pelletizing calcium material entrance of the ball calcium material outlet connection palletizing device, the spherical material outlet connection pyrolysis of the palletizing device
The spherical material entrance of stove.
3. system according to claim 1, it is characterised in that the adsorbent equipment also includes High Temperature Gas and exported, the heat
Solving stove includes High Temperature Gas entrance, the High Temperature Gas entrance of the High Temperature Gas outlet connection pyrolysis oven of the adsorbent equipment.
4. 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 °.
5. system according to claim 1, it is characterised in that the pyrolysis oven also includes being located at the top of the pyrolysis oven
It is pyrolyzed oil gas vent.
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, by spherical material send into pyrolysis oven, occur pyrolytic reaction, obtain solid material；
B, the solid material 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 include step before step A：Raw coal is dried,
Obtain pelletizing raw coal；Calcium based raw material is calcined, pelletizing calcium material is obtained；Made after the pelletizing raw coal and pelletizing calcium material are mixed
Ball, obtains spherical material.
8. method according to claim 7, it is characterised in that the calcium based raw material include lime, lime stone, white lime and
One or more in carbide slag.
9. method according to claim 6, it is characterised in that also including step：The High Temperature Gas is sent into the pyrolysis
Stove, is used as the thermal source of pyrolytic reaction.
10. method according to claim 6, it is characterised in that the pyrolytic reaction of the step A also generates pyrolysis oil gas,
The pyrolysis oil gas is collected by being pyrolyzed oil gas vent.
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| CN107986279A (en) * | 2017-12-22 | 2018-05-04 | 中国科学院上海高等研究院 | A kind of microwave furnace of calcium carbide reactor and prepare the method for calcium carbide using it |
| CN113739594A (en) * | 2021-09-22 | 2021-12-03 | 新疆宜化化工有限公司 | Automatic breaking process and device for preventing hardening of materials in calcium carbide furnace |
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