CN105948050A - Calcium carbide production method and system - Google Patents
Calcium carbide production method and system Download PDFInfo
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- CN105948050A CN105948050A CN201610530774.4A CN201610530774A CN105948050A CN 105948050 A CN105948050 A CN 105948050A CN 201610530774 A CN201610530774 A CN 201610530774A CN 105948050 A CN105948050 A CN 105948050A
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 239000005997 Calcium carbide Substances 0.000 title abstract description 10
- 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 abstract description 10
- 239000007787 solid Substances 0.000 claims abstract description 51
- 238000000034 method Methods 0.000 claims abstract description 31
- 238000002156 mixing Methods 0.000 claims abstract description 28
- 239000002994 raw material Substances 0.000 claims abstract description 27
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 238000003723 Smelting Methods 0.000 claims abstract description 24
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 22
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 12
- 238000010438 heat treatment Methods 0.000 claims abstract description 12
- 238000000197 pyrolysis Methods 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 80
- 239000000567 combustion gas Substances 0.000 claims description 32
- 239000003245 coal Substances 0.000 claims description 23
- 238000003860 storage Methods 0.000 claims description 16
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 11
- 238000000465 moulding Methods 0.000 claims description 10
- 238000013467 fragmentation Methods 0.000 claims description 8
- 238000006062 fragmentation reaction Methods 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- 239000011230 binding agent Substances 0.000 claims description 5
- 239000002245 particle Substances 0.000 claims description 5
- 238000003825 pressing Methods 0.000 claims description 3
- 241001062472 Stokellia anisodon Species 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000004484 Briquette Substances 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 7
- 239000000843 powder Substances 0.000 description 5
- 239000002956 ash Substances 0.000 description 4
- 108010066057 cabin-1 Proteins 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000009413 insulation Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000011282 treatment Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 229910014813 CaC2 Inorganic materials 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000010891 electric arc Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 238000001754 furnace pyrolysis Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000003306 harvesting Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- -1 semicoke Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Carbon And Carbon Compounds (AREA)
Abstract
The invention relates to a calcium carbide production method and a calcium carbide production system. The system comprises a mixing and forming unit, a reaction furnace, a carbon-containing solid hot charging unit, an oil-gas separation unit, a gas heating furnace and a calcium carbide smelting furnace, wherein the mixing and forming unit comprises a feed opening and a discharge opening; the reaction furnace comprises a briquette inlet, a gas heat carrier inlet, an oil-gas outlet and a carbon-containing solid outlet; the oil-gas separation unit is connected with the gas heating furnace; a gas outlet of the gas heating furnace is connected with the gas heat carrier inlet of the reaction furnace; the calcium carbide smelting furnace comprises a calcium carbide raw material inlet and a calcium carbide outlet. According to the method and the system, a part of gas produced by pyrolysis is reasonably utilized, and the quality of a gas product is improved; hot charging is performed on carbon-containing solids produced by reaction, so that electric energy consumption of the calcium carbide smelting furnace is greatly reduced.
Description
Technical field
The invention mainly relates to the production field of carbide, be specifically related to the production method of a kind of Acetylenogen. and be
System.
Background technology
Carbide is as a kind of important industrial chemicals, mainly for the production of acetylene and ethynylation chemical product,
Once " mother of organic synthesis industry " it was described as.Consider from National energy distribution, " rich coal, oil-poor,
Few gas " it is the typical characteristic of China's energy resource structure, coal is the main energy sources of China, accounts for primary energy
70%, therefore, carbide produce significant for Industrial Economic Development.
Tradition carbide produces and mainly uses electrothermal way, i.e. with lump lime and block coke as raw material,
In furnace of calcium carbide by electric arc heated to 2000 degree Celsius more than, by equation CaO+3C=CaC2The reaction principle of+CO
Carry out pyrolytic semlting and produce carbide.From the requirement consideration to carbon raw, tradition carbide production technology is main
There is following defect: (1) requires that the granularity of carbon materials is at 5-30mm, fixed carbon content > 84%, ash
< 15%, it is possible to meet only coke, semicoke, petroleum coke and some high-quality anthracites of these requirements,
And these raw material reserves are extremely limited, expensive；(2) can be with 15-20% in raw material shattering process
Raw material due to granularity less than 5mm and go out of use, cause the serious waste of resource；(3) during carbide produces
Main employing block carbon raw material and Calx, mass transfer and heat transfer efficiency are low, and reaction rate is relatively low, carbide smelting
The furnace thermal efficiency is only about 50%, and power consumption is up to about 3250kWh/t carbide.Visible, carbon raw
Quality directly affects the economic indicators such as the Yield and quality of carbide, electric power unit consumption and cost.
Consider from the character of raw coal, containing ash, sulfur and other a small amount of mineral in raw coal.Major part raw coal
Ash be all higher than the ash requirements upper limit of carbide raw material, raw coal need to be carried out sorting deliming and process.By dividing
The difference of selected introductions matter can be divided into wet split and the big class of dry separation two, and during wet split, coal fills with water
Tap is touched, and increases coal selecting product moisture and the dehydration energy of follow-up carbon raw；And conventional dry separation
Using normal temperature air as separating medium, the surface moisture of raw coal adds the contact between granule and adheres to several
Rate, causes actual separating effect to be deteriorated.It addition, in recent years, along with carrying of Coal Mechanical recovery percent
Height, raw coal fine coal content in recovery process accounts for 40-60%, and the poor low-order coal of hardness even accounts for
About 70%, it is to run counter to that this obvious granularity with traditional carbide manufacturing technique requirent carbon raw is more than 5mm
's.
For solving tradition carbide production technology to ingredient requirement harshness, highly energy-consuming, high pollution, poor benefit etc.
Shortcoming, widens the scope of carbide carbon back raw material, and carbide production technology is further improved.
Therefore, for the problems referred to above, it is necessary to provide production method and the system of a kind of Acetylenogen., can solve
Tradition carbide production technology is to problems such as ingredient requirement harshness, highly energy-consuming, high pollution, poor benefits.
Summary of the invention
For the problems referred to above, it is desirable to provide the production method of a kind of Acetylenogen. and system, the method and
The purpose of system is the waste heat waste in solution carbide production technology, highly energy-consuming problem.Further, originally
Invention will solve the carbide production technology high request problem to raw material.
The production system of the Acetylenogen. that the present invention provides includes: batch mixing forming unit, reacting furnace, carbon containing are solid
Body heat send unit, Oil-gas Separation unit, gas-fired heater and carbide smelting furnace, and wherein, described batch mixing becomes
Type unit includes feeding mouth and discharging opening, for the molding of type ball；Described reacting furnace include type ball entrance,
Gas heat carrier entrance, oil gas vent and carbonaceous solids outlet, for the pyrolysis of type ball；Described type ball enters
Mouth is connected with the discharging opening of described batch mixing forming unit；The outlet of described carbonaceous solids and described carbonaceous solids heat
Unit is sent to be connected；Described oil gas vent is connected with described Oil-gas Separation unit；Described Oil-gas Separation unit with
Described gas-fired heater is connected；The gas outlet of described gas-fired heater carries with the air heat of described reacting furnace
Body entrance is connected；Described carbide smelting furnace includes carbide raw material entrance and carbide outlet, for the smelting of carbide
Refining；Described carbide raw material entrance send the outlet of unit to be connected with described carbonaceous solids heat.
Above-mentioned system may also include tar storage tank, the entrance of described tar storage tank and described Oil-gas Separation list
The liquid outlet of unit is connected, and the outlet of described tar storage tank is connected with the entrance of described batch mixing forming unit.
Further, above-mentioned system may also include gas booster unit, and described gas booster unit is located at
Between described Oil-gas Separation unit and described gas-fired heater.
Further, above-mentioned system may also include fragmentation cell, and described fragmentation cell is located at described batch mixing
Before forming unit.
Further, described system may also include combustion gas container, described combustion gas container and described Oil-gas Separation
The gas outlet of unit or be connected with the gas outlet of described gas booster unit.
The present invention also provides for a kind of production method utilizing said system to carry out Acetylenogen., comprises the following steps:
By particle diameter, < coal of 2mm and Calx is first batch mixing aftershaping in described batch mixing forming unit, obtains type ball；Will
Described type ball is sent into described reacting furnace and is carried out pyrolytic reaction, obtains carbonaceous solids, oil gas；By described carbon containing
Solid is sent into described carbonaceous solids heat and is sent unit；Described carbonaceous solids heat is sent the carbonaceous solids in unit send
Enter described carbide smelting furnace to smelt, obtain carbide；Described oil gas is sent into described Oil-gas Separation unit
Carry out isolated tar and combustion gas；Heat in described combustion gas is sent into described gas-fired heater；By described
Combustion gas after heating sends into described reacting furnace as gas heat carrier.
In above-mentioned method, the granularity of described type ball is 5-40 millimeter, and cold pressing strength is more than 200 Ns/.
Further, above-mentioned method further comprises the steps of: to be sent into described mixed using described tar as binding agent
In material forming unit.
Further, above-mentioned method may further comprise the step of: sends a part for described combustion gas into combustion gas storage
Cabinet stores.
Further, said method may further comprise the step of: and coal and Calx are crushed to below 2mm particle diameter.
According to the technique scheme of the present invention, a part of combustion gas that can pyrolysis be produced is at gas heating
There is provided heat for reacting furnace after heating in stove, again the hot carbonaceous solids of part that pyrolytic process produces is carried out
Hot charging, reduces the energy consumption of cracking process.
Further, the tar that pyrolysis produces also can be sent in batch mixing forming unit by the present invention as binding agent
Carry out the mixed-forming of carbide raw material, improve ratio of briquetting and the type ball intensity of powder, solve carbide raw
The production. art particular/special requirement to raw material, has accomplished recycling of resource, energy-conserving and environment-protective simultaneously, has had relatively
High environmental economical profit.
Accompanying drawing explanation
Fig. 1 is the operation system structure schematic diagram of the Acetylenogen. of the embodiment of the present invention；
Fig. 2 is the production system flow chart of the Acetylenogen. of the embodiment of the present invention.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is described in more details,
So as to the advantage being more fully understood that the solution of the present invention and various aspects.But, described below
Detailed description of the invention and embodiment are only descriptive purpose rather than limitation of the present invention.
The production system sketch of the Acetylenogen. that Fig. 1 provides for the present invention.
This system includes that raw material cabin 1, fragmentation cell 2, batch mixing forming unit 3, reacting furnace 4, carbon containing are solid
Body heat send unit 5, Oil-gas Separation unit 6, gas booster unit 7, gas-fired heater 8, combustion gas container 9,
Tar storage tank 10, carbide smelting furnace 11, wherein, raw material cabin 1, fragmentation cell 2, gas booster unit 7,
Combustion gas container 9, tar storage tank 10 are not necessary to arrange.
Concrete, raw material cabin 1 is used for holding carbide raw material；Fragmentation cell 2 includes breaker, is used for
Crushing of raw material, its entrance is connected with the outlet of raw material cabin 1.Batch mixing forming unit 3 include batch mixer with
Forming machine, is provided with feeding mouth and discharging opening, for the molding of type ball.After coal and the effective molding of Calx,
The type ball formed has preferable intensity, heat stability, to rear profile ball the deep processing such as pyrolytic gasification or
Use has preferable facilitation.Additionally, the volatile matter dust when effusion in pyrolytic process also can be reduced
Carry secretly, and then improve pyrolysis oil, the quality of gas product.
Reacting furnace 4 is vertical reacting furnace, including type ball entrance, gas heat carrier entrance, oil gas vent and
Carbonaceous solids exports, for the pyrolysis of type ball.The shaft of vertical reacting furnace is upright, furnace gas in stove upwards
Motion, and in countercurrent flow between furnace charge, this is advantageous for the mass-and heat-transfer between material.Most shaft furnaces
Furnace charge directly contact with fuel.The structure of general furnace roof, has unlimited and airtight two kinds.
Wherein, the type ball entrance of reacting furnace 4 is connected with the discharging opening of batch mixing forming unit 3；Described carbon containing
Solid outlet send unit to be connected with described carbonaceous solids heat, is used for solving response system energy consumption height, energy wave
The problem taken；Described oil gas vent is connected with described Oil-gas Separation unit, for further Oil-gas Separation.
Oil-gas Separation unit 6 includes gs-oil separator, for oil gas carried out isolated liquid fuel and
Combustion gas.Gas booster unit 7 includes pressue device, for combustion gas is carried out pressurized treatments.When being not provided with
During gas booster unit 7, described Oil-gas Separation unit 6 is connected with described gas-fired heater 8.Work as setting
During gas booster unit 7, described Oil-gas Separation unit 6 depends on gas booster unit 7, gas-fired heater 8
Secondary connected.The gas heat carrier entrance phase of the gas outlet of described gas-fired heater 8 and described reacting furnace 4
Even, as gas heat carrier after a part of combustion gas that pyrolytic process produces can being heated in gas-fired heater
Heat, recycling for combustion gas is provided for reacting furnace.
Compressed gas after pressurization can be utilized respectively by gas booster unit 7, and a part sends into combustion gas container 9
Storage, a part is sent to gas-fired heater 8 and heats.
Above-mentioned system may also include tar storage tank 10, and the entrance of described tar storage tank 10 divides with described oil gas
Liquid outlet from unit 6 is connected, and is used for storing liquid tar.The outlet of described tar storage tank 10 and institute
The entrance stating batch mixing forming unit 3 is connected, for tar is inputted batch mixing forming unit as binding agent,
Make coal and Calx molding effectively, so that the type ball formed has preferable intensity, heat stability, reach
Production requirement to carbide raw material.Certainly, the liquid outlet of Oil-gas Separation unit 6 can directly become with batch mixing
The entrance of type unit 3 is connected, and saves the setting of tar storage tank 10.
The gas outlet of gas booster unit 7 can be connected with combustion gas container 9 and gas-fired heater 8 respectively,
The gas outlet of gas-fired heater 8 is connected with the gas heat carrier entrance of described reacting furnace 4.When not setting combustion
During gas presser unit 7, combustion gas container 9 can directly gas outlet with Oil-gas Separation unit 6 be connected.
The carbonaceous solids outlet of reacting furnace 4 send the entrance of unit 5 to be connected with described carbonaceous solids heat, carbon containing
Solid thermal send the outlet of unit 5 to be connected with the entrance of carbide smelting furnace 11, and the smelting for carbide produces.
Wherein, carbonaceous solids heat send unit 5, carbonaceous solids is filled the most afterwards from the solids exit mouth of reacting furnace
Enter in carbonaceous solids heat-insulation conveying device, it is possible to reduce the heat loss of carbonaceous solids, be greatly saved carbide
The power consumption of smelting furnace, and then reduce the processing cost of carbide.
As in figure 2 it is shown, the concrete operation step of the production method of the Acetylenogen. of present invention offer is as follows:
Raw material is crushed: coal, Calx are crushed to below 2mm particle diameter；
Powder batch mixing molding: the coal after crushing and Calx elder generation batch mixing aftershaping, obtains type ball, after molding
The granularity of type ball is 5-40 millimeter, and cold pressing strength is more than 200 Ns/；
Reacting furnace processes, and type ball carries out in reacting furnace pyrolysis processing.Reaction temperature is Celsius at 500-950
Degree, obtains the product such as carbonaceous solids, combustion gas after pyrolysis；
Carbonaceous solids hot charging processes, and from the solids exit mouth of reacting furnace, carbonaceous solids is loaded carbon containing the most afterwards
In solid heat-insulation conveying device, reduce the heat loss of carbonaceous solids；
Carbide smelting furnace is smelted: the carbonaceous solids in heat-insulation conveying device is sent into carbide smelting furnace and carries out smelting
Refining, smelting temperature is more than 1700 degrees Celsius；
Gas booster, carries out pressurized treatments in pressue device by combustion gas, and by the compressed gas after pressurization
It is utilized respectively, is partly into the storage of combustion gas container, is partly into gas-fired heater and heats；
Gas heating, heats a part of compressed gas in heating furnace, and the Control for Kiln Temperature of heating furnace is 700
More than degree Celsius, combustion gas be mainly composed of acetylene, methane, carbon monoxide, carbon dioxide etc..
Tar is used for molding, and as binding agent, the tar produced in reacting furnace pyrolytic process is used for powder
Molding.
Above-mentioned steps is not all of necessary, broken, the gas booster of such as raw material, recycling of tar
Etc. arranging according to practical situation.
From such scheme, the production system of the Acetylenogen. that the present invention provides and method, by being pyrolyzed
A part of combustion gas that process produces provides for reacting furnace as gas heat carrier after heating in gas-fired heater
Heat, has accomplished recycling of resource；The tar produced by cracking process is as the bonding of forming process
Agent, improves ratio of briquetting and the type ball intensity of powder；The carbonaceous solids produced from reacting furnace is carried out hot charging,
And the carbonaceous solids of hot charging is sent in carbide smelting furnace, it is greatly saved the power consumption of carbide smelting furnace,
And then reduce carbide processing cost.
Below in conjunction with specific embodiment, technical scheme is described.
In following embodiment, institute's taking technique condition value is exemplary, and its desirable numerical range is the most aforementioned
Shown in description.
Embodiment 1
The raw material such as coal and Calx entrance raw material fragmentation cell is crushed, is crushed to below 1mm, enters
Powder batch mixing forming unit carries out batch mixing molding, and moulded coal enters reacting furnace, sets reaction temperature and reacts,
Producing carbonaceous solids and combustion gas, carbonaceous solids is reacted in carbide smelting furnace, produces Acetylenogen., i.e.
Carbide.
The carbonaceous solids of the present embodiment is mining area, Inner Mongol brown coal, and the granularity of break up coal is below 2mm, type
The size of ball is 18mm*18mm*38mm, 4mmx4mmx10mm, 30mmx30mmx50mm, and reaction temperature is respectively
500 DEG C, 720 DEG C is 950 DEG C, and gas heating temperature is 800 DEG C.The carbon containing that raw material and reacting furnace produce is solid
The analysis result meansigma methods of body such as table 1-table 2.The average reaction temperature of carbide smelting furnace is 1900 degrees Celsius,
The average gas forming amount of carbide product is 310 liters/kilogram.
Table 1: feedstock analysis result
Table 2 carbonaceous solids analysis result
Wherein, the M in tableadRepresent air-dried moisture；AadRepresent and be dried base ash；VadRepresent sky
Air dry dry base volatile matter；FCadRepresent air-dried basis fixed carbon.
S in tablet,adRepresent air-dried basis total sulphur content；CadRepresent air-dried basis carbon content；HadRepresent
Air-dried basis hydrogen content；NadRepresent air-dried basis nitrogen content；OadRepresent air-dried basis oxygen content.
As seen from the above-described embodiment, technical scheme can effectively utilize combustion gas and the carbon containing of pyrolysis generation
The calorific value of solid, develops towards the maximized direction of resource and Energy harvesting, to whole calcium carbide industry and society
Positive effect can be suffered from by environment.
Last it is noted that obvious, above-described embodiment is only by clearly demonstrating the act that the present invention is made
Example, and not restriction to embodiment.For those of ordinary skill in the field, above-mentioned
Can also make other changes in different forms on the basis of explanation.Here without also cannot be to institute
Some embodiments give exhaustive.And the obvious change thus amplified out or variation are still in this
Among the protection domain of invention.
Claims (10)
1. a production system for Acetylenogen., described system includes batch mixing forming unit, reacting furnace, carbon containing
Solid thermal send unit, Oil-gas Separation unit, gas-fired heater and carbide smelting furnace, wherein,
Described batch mixing forming unit includes feeding mouth and discharging opening, for the molding of type ball；
Described reacting furnace includes type ball entrance, gas heat carrier entrance, oil gas vent and carbonaceous solids outlet,
Pyrolysis for type ball；Described type ball entrance is connected with the discharging opening of described batch mixing forming unit；Described contain
Carbon solid outlet send unit to be connected with described carbonaceous solids heat；Described oil gas vent and described Oil-gas Separation list
Unit is connected；
Described Oil-gas Separation unit is connected with described gas-fired heater；The gas outlet of described gas-fired heater
It is connected with the gas heat carrier entrance of described reacting furnace；
Described carbide smelting furnace includes carbide raw material entrance and carbide outlet, for the smelting of carbide；Described
Carbide raw material entrance send the outlet of unit to be connected with described carbonaceous solids heat.
System the most according to claim 1, it is characterised in that described system also includes tar storage tank,
The entrance of described tar storage tank is connected with the liquid outlet of described Oil-gas Separation unit, described tar storage tank
Outlet is connected with the entrance of described batch mixing forming unit.
System the most according to claim 1, it is characterised in that described system also includes gas booster
Unit, described gas booster unit is located between described Oil-gas Separation unit and described gas-fired heater.
System the most according to claim 1, it is characterised in that described system also includes fragmentation cell,
Before described fragmentation cell is located at described batch mixing forming unit.
System the most according to claim 3, it is characterised in that described system also includes combustion gas container,
The gas outlet of described combustion gas container and described Oil-gas Separation unit or the combustion gas with described gas booster unit
Outlet is connected.
6. utilize the method that system described in any one of claim 1 to 5 carries out Acetylenogen. production, bag
Include following steps:
By particle diameter, < coal of 2mm and Calx is first batch mixing aftershaping in described batch mixing forming unit, obtains type ball；
The described type ball described reacting furnace of feeding is carried out pyrolytic reaction, obtains carbonaceous solids, oil gas；
Unit is sent by the described carbonaceous solids described carbonaceous solids heat of feeding；
Described carbonaceous solids heat is sent the carbonaceous solids in unit send into described carbide smelting furnace smelt,
Obtain carbide；
The described oil gas described Oil-gas Separation unit of feeding is carried out isolated tar and combustion gas；
Heat in described combustion gas is sent into described gas-fired heater；
Combustion gas after described heating is sent into described reacting furnace as gas heat carrier.
Method the most according to claim 6, it is characterised in that the granularity of described type ball is 5-40
Millimeter, cold pressing strength is more than 200 Ns/.
Method the most according to claim 6, it is characterised in that described method further comprises the steps of:
Described tar is sent in described batch mixing forming unit as binding agent.
Method the most according to claim 6, it is characterised in that described method further comprises the steps of:
A part for described combustion gas is sent into the storage of combustion gas container.
Method the most according to claim 6, it is characterised in that described method further comprises the steps of:
Coal and Calx are crushed to below 2mm particle diameter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610530774.4A CN105948050B (en) | 2016-07-06 | 2016-07-06 | A kind of production method and system of calcium carbide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610530774.4A CN105948050B (en) | 2016-07-06 | 2016-07-06 | A kind of production method and system of calcium carbide |
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| Publication Number | Publication Date |
|---|---|
| CN105948050A true CN105948050A (en) | 2016-09-21 |
| CN105948050B CN105948050B (en) | 2018-07-24 |
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| CN201610530774.4A Active CN105948050B (en) | 2016-07-06 | 2016-07-06 | A kind of production method and system of calcium carbide |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106517204A (en) * | 2016-11-16 | 2017-03-22 | 神雾环保技术股份有限公司 | Special system and method for forming calcium carbide raw material |
| CN106635164A (en) * | 2016-11-07 | 2017-05-10 | 中国石油大学(华东) | Process for producing acetylene through lime carbon pellet in-situ reaction |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103708455A (en) * | 2013-12-25 | 2014-04-09 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing calcium carbide |
| CN104556037A (en) * | 2014-12-30 | 2015-04-29 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing calcium carbide |
| CN105668568A (en) * | 2016-01-04 | 2016-06-15 | 神雾环保技术股份有限公司 | System and method for production of calcium carbide |
| CN205953532U (en) * | 2016-07-06 | 2017-02-15 | 神雾环保技术股份有限公司 | Production system of calcium carbide |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103708455A (en) * | 2013-12-25 | 2014-04-09 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing calcium carbide |
| CN104556037A (en) * | 2014-12-30 | 2015-04-29 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing calcium carbide |
| CN105668568A (en) * | 2016-01-04 | 2016-06-15 | 神雾环保技术股份有限公司 | System and method for production of calcium carbide |
| CN205953532U (en) * | 2016-07-06 | 2017-02-15 | 神雾环保技术股份有限公司 | Production system of calcium carbide |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106635164A (en) * | 2016-11-07 | 2017-05-10 | 中国石油大学(华东) | Process for producing acetylene through lime carbon pellet in-situ reaction |
| CN106517204A (en) * | 2016-11-16 | 2017-03-22 | 神雾环保技术股份有限公司 | Special system and method for forming calcium carbide raw material |
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