CN206692332U - System for producing calcium carbide - Google Patents
System for producing calcium carbide Download PDFInfo
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- CN206692332U CN206692332U CN201720420071.6U CN201720420071U CN206692332U CN 206692332 U CN206692332 U CN 206692332U CN 201720420071 U CN201720420071 U CN 201720420071U CN 206692332 U CN206692332 U CN 206692332U
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- calcium carbide
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Abstract
It the utility model is related to a kind of system for producing calcium carbide.System for producing calcium carbide includes：The hot furnace of calcium carbide of down-flow fluidized bed using ECT pyrolysis oven, oxygen and hot precipitator, wherein, down-flow fluidized bed using ECT pyrolysis oven includes material inlet, solid material outlet and raw coke oven gas outlet, calcium carbide tail gas entrance；The hot furnace of calcium carbide of oxygen includes oxygen coal entrance, expects import, calcium carbide outlet and calcium carbide tail gas outlet admittedly, the hot furnace of calcium carbide of oxygen expects that import expects that outlet is connected admittedly with down-flow fluidized bed using ECT pyrolysis oven admittedly, and the hot furnace of calcium carbide calcium carbide tail gas outlet of oxygen is connected with the down-flow fluidized bed using ECT pyrolysis oven calcium carbide tail gas entrance；Hot precipitator includes ash-laden gas entrance, clean gas outlet, blowback air entrance and dust outlet, and ash-laden gas entrance is connected with raw coke oven gas outlet.The utility model uses new hot precipitator, and pyrolysis oil-containing gas high-temperature dust removal can be achieved, and improves pyrolysis oil quality；Other down-flow fluidized bed using ECT pyrolysis oven and the coupling of oxygen thermoelectricity stone furnace technology, make use of the calcium carbide tail gas sensible heat of the hot furnace of calcium carbide of oxygen to provide heat for pyrolysis oven, reduce system energy consumption.
Description
Technical field
It the utility model is related to calcium carbide production field, more particularly to a kind of system for producing calcium carbide.
Background technology
In traditional calcium carbide smelting process, pyrolytic process and calcium carbide smelting process are relatively independent, and two processes do not have energy
Coupling, system energy consumption are big；In addition, heat skewness in the conventional hot method furnace of calcium carbide of oxygen, its caused calcium carbide tail gas heat
It is difficult by.Produced problem easily causes the profligacy of resource in the smelting of traditional calcium carbide above, increases production cost.
It is worth noting that, in pyrolytic process, for raw coke oven gas processing, due to be wherein mingled with dust but its temperature compared with
It is high, it usually needs cooling processing is carried out first, could be carried out dust removal by filtration operation, be caused system architecture lengthy and jumbled, gas heat wave
The problems such as taking.At all because being：In existing industrial production, in the processing of dusty gas, device or side for dedusting
Method mainly has sack cleaner, electric cleaner and wet dedusting.However, these dust arresters or method all have certain lack
Fall into.Such as sack cleaner, because the material heatproof of cloth bag now only has 280 DEG C, therefore, high-temperature gas typically need to by air-cooled or
Spraying cooling, the temperature to high-temperature gas reach dedusting again after the temperature of cloth bag；Electric cleaner for another example, due to material and than electricity
The relation of resistance, the dedusting temperature of electric precipitation are usually no more than 350 DEG C, it is also desirable to which the method using cooling reaches dedusting condition；Most
Wet dedusting afterwards, dust removal process need to consume substantial amounts of water, simultaneously because containing substantial amounts of dust in high-temperature gas, therefore, lead to
Wet dedusting is crossed, the problems such as easily bringing after-treatment and the secondarily polluted water of rear end dirt mud.
Utility model content
To solve the above problems, the utility model provides a kind of system for producing calcium carbide.On the one hand, it can effectively utilize heat
Solution preocess and energy caused by calcium carbide preparation process, realize resource rational utilization；On the other hand solve high-temperature gas to be difficult to filter
The problem of dedusting.
A kind of system for producing calcium carbide described in the utility model, including：The hot furnace of calcium carbide of down-flow fluidized bed using ECT pyrolysis oven, oxygen and high temperature
Deduster, wherein,
The down-flow fluidized bed using ECT pyrolysis oven includes material inlet, solid material outlet and raw coke oven gas outlet, calcium carbide tail gas entrance；
The hot furnace of calcium carbide of oxygen includes oxygen coal entrance, admittedly material import, calcium carbide outlet and calcium carbide tail gas outlet,
The solid material import of the hot furnace of calcium carbide of oxygen is connected with the solid material outlet of the down-flow fluidized bed using ECT pyrolysis oven, the oxygen thermoelectricity stone
The calcium carbide tail gas outlet of stove is connected with the calcium carbide tail gas entrance of the down-flow fluidized bed using ECT pyrolysis oven；
The hot precipitator is used to carry out dust removal by filtration to high temperature raw coke oven gas caused by the down-flow fluidized bed using ECT pyrolysis oven, described
Hot precipitator includes ash-laden gas entrance, clean gas outlet, blowback air entrance and dust outlet, the ash-laden gas entrance with it is described
The raw coke oven gas outlet of down-flow fluidized bed using ECT pyrolysis oven is connected.
Especially, the hot precipitator includes：Casing, dust removal and filtration component and transmission device, wherein,
The casing is provided with filter chamber and dirt pocket, and the ash-laden gas entrance and clean gas outlet are arranged on the filtering
Room, the blowback air entrance are arranged on the dirt pocket with dust outlet；
The dust removal and filtration component is embedded in the filter chamber and dirt pocket；
The ash-laden gas entrance and clean gas outlet are located at the both sides up and down of the dust removal and filtration component respectively, described anti-
Air blowing entrance is located at the both sides up and down of the dust removal and filtration component with dust outlet respectively；
The transmission device is connected with the dust removal and filtration component, and the transmission device drives the dust removal and filtration member device
Part rotates around the axis of the casing.
Further, the system also includes coke powder collection device, for collecting coke powder caused by the hot precipitator,
And it is passed through the hot furnace of calcium carbide of the oxygen.
Further, the system also includes refrigerated separation device, and it has purified gas entrance, tar outlet and heat
Vent one's spleen outlet, the purified gas entrance of the refrigerated separation device is connected with the clean gas outlet of the hot precipitator.
Specifically, the system also includes lime breaker and raw coal disintegrating machine, is respectively connecting to the down-flow fluidized bed using ECT
The material inlet of pyrolysis oven.
More specifically, the system also includes the ultra-fine preparation facilities of raw coal, it is connected to the oxygen coal of the hot furnace of calcium carbide of the oxygen
Entrance.
System for producing calcium carbide described in the utility model and method employ new hot precipitator, can handle High Temperature Gas
Body, can 500~900 DEG C of high temperature resistant, realize pyrolysis oil-containing gas high-temperature dust removal, improve pyrolysis oil quality；Dust removal and filtration component
By rotation mode Chalk-dust filtering and blowback, the dust of filtering does not accumulate, and is not easily blocked, and efficiency of dust collection is high.Under using in addition
Row bed pyrolysis oven and the coupling of oxygen thermoelectricity stone furnace technology, make use of the calcium carbide tail gas sensible heat of the hot furnace of calcium carbide of oxygen to provide heat for pyrolysis oven
Amount, reduce system energy consumption.
Brief description of the drawings
Fig. 1 is the structural representation of system for producing calcium carbide described in the utility model.
Fig. 2 is the structural representation of hot precipitator described in the utility model.
Embodiment
Below in conjunction with drawings and examples, specific embodiment of the present utility model is described in more details, with
Just the advantages of better understood when scheme and its various aspects of the present utility model.However, specific implementations described below side
Formula and embodiment are for illustrative purposes only, rather than to limitation of the present utility model.
Effectively using pyrolytic process and energy caused by calcium carbide preparation process, to realize resource rational utilization, solving high temperature
Gas is difficult to the problem of dust removal by filtration, and the utility model provides a kind of system for producing calcium carbide.
As shown in figure 1, the system includes：Hot precipitator 1, down-flow fluidized bed using ECT pyrolysis oven 2 and the hot furnace of calcium carbide 3 of oxygen.This practicality
New to be coupled using 2 technique of furnace of calcium carbide 3 hot with oxygen of down-flow fluidized bed using ECT pyrolysis oven, the calcium carbide tail gas sensible heat that make use of the hot furnace of calcium carbide 3 of oxygen is
Down-flow fluidized bed using ECT pyrolysis oven 2 provides heat, reduces the energy consumption of system.
Specifically, as shown in figure 1, the down-flow fluidized bed using ECT pyrolysis oven 2 includes material inlet, solid material exports and raw coke oven gas goes out
Mouth, calcium carbide tail gas entrance.To improve reaction efficiency, the less feed coal of particle diameter and lime need to be sent into down-flow fluidized bed using ECT pyrolysis oven 2, its
The particle diameter of middle coal is 1mm~3mm, and the particle diameter of lime is less than 3mm, and pyrolytic reaction occurs at 450~900 DEG C, and generation high temperature is waste
Coal gas and high-temperature semi-coke, its high temperature raw coke oven gas export discharge by the raw coke oven gas at the top of down-flow fluidized bed using ECT pyrolysis oven 2, then sent
Enter the hot precipitator 1；Hot high-temperature semi-coke and lime are exported by solid material and produced, then passes to the hot furnace of calcium carbide of the oxygen
3.Feed coal can be crushed by raw coal disintegrating machine 6, obtain the coal that particle diameter is 1mm~3mm, and lime can pass through lime
Breaker 7 is crushed, and obtains the lime that particle diameter is less than 3mm, raw coal disintegrating machine 6 and lime breaker 7 connect respectively
To the material inlet, the coal grain that the particle diameter after crushing is 1mm~3mm is together sent into descending with lime of the particle diameter less than 3mm
Bed pyrolysis oven 2.Regenerative radiant tube burner 9 is may be provided with the down-flow fluidized bed using ECT pyrolysis oven 2, can be passed through combustion gas in it is fired
Burn, for carrying out auxiliary heating to down-flow fluidized bed using ECT pyrolysis oven 2.
Take feed coal and lime to be together sent into down-flow fluidized bed using ECT pyrolysis oven 2, make use of the catalytic effect of lime, increase gas production
Amount, the especially content of methane gas and hydrogen and are directly separated and do gas product methane gas.
As shown in figure 1, the hot furnace of calcium carbide 3 of oxygen includes oxygen coal entrance, expects import, calcium carbide outlet and calcium carbide tail gas admittedly
Outlet, described to expect that import is connected with the solid material outlet admittedly, the calcium carbide tail gas outlet is connected with the calcium carbide tail gas entrance.Directly
Connect and high-temperature semi-coke and lime are sent into the hot furnace of calcium carbide 3 of oxygen, reduce the oxygen and consumption of coal amount of the hot furnace of calcium carbide 3 of oxygen.
As shown in figure 1, in the case where oxygen is as carrier gas, microfine coal is ejected into through nozzle or other modes described
Oxidation reaction, which occurs, for the hot furnace of calcium carbide 3 of oxygen, microfine coal and oxygen can provide heat.The particle diameter of superfine powder is generally less than 200um, its
It can be made by the way that coal dust of the particle diameter in raw coal disintegrating machine 6 less than 1mm is sent into the ultra-fine preparation facilities 8 of raw coal.Control oxygen heat
The furnace temperature of furnace of calcium carbide 3 is at 1700 DEG C~2200 DEG C so that into the hot furnace of calcium carbide 3 of oxygen high-temperature semi-coke and lime 1700 DEG C~
At a temperature of 2200 DEG C, occur melting or partial melting reaction generation calcium carbide and calcium carbide tail gas, calcium carbide by the hot furnace of calcium carbide 3 of oxygen electricity
Stone outlet discharge, calcium carbide tail gas are exported by calcium carbide tail gas and produced, and down-flow fluidized bed using ECT is sent into from the calcium carbide tail gas entrance of down-flow fluidized bed using ECT pyrolysis oven 2
Pyrolysis oven 2.The temperature of usual calcium carbide tail gas is higher than 800 DEG C, its enter after the down-flow fluidized bed using ECT pyrolysis oven 2 with feed coal and lime
Exchanged heat, heat is provided for pyrolytic reaction.The product such as pyrolytic reaction generation raw coke oven gas (oil, gas and water etc.) and semicoke, raw coke oven gas
Calcium carbide tail gas after being exchanged heat is carried to the raw coke oven gas of down-flow fluidized bed using ECT pyrolysis oven and exported, further same to be passed through hot precipitator 1, and now
Raw coke oven gas and the temperature of calcium carbide tail gas be generally 600~650 DEG C.
Down-flow fluidized bed using ECT pyrolysis oven 2 using the hot furnace of calcium carbide 3 of oxygen calcium carbide tail gas as heat carrier heat based on, heat accumulation type radiant tube
The heating of burner 9 can be used as auxiliary heating tool.The technique has two big benefits, first, the calcium carbide tail gas 80% of the hot furnace of calcium carbide 3 of oxygen
It is above the available gas components such as carbon monoxide, hydrogen, as the heat carrier of down-flow fluidized bed using ECT pyrolysis oven 2, is not mixed into inert gas,
Raw coke oven gas purity is high, quality better, can be used as fuel and industrial chemicals；Second, using supplemented by regenerative radiant tube burner 9, can
The isolation of flue gas and pyrolysis gas, pyrolysis gas purity height, the quality better of acquisition are realized, while regenerative radiant tube burner 9 can spirit
Arrangement living, as auxiliary heat supplying, it is advantageously implemented the temperature field allotment of down-flow fluidized bed using ECT pyrolysis oven 2.
As depicted in figs. 1 and 2, the hot precipitator 1 include ash-laden gas entrance, clean gas outlet, blowback air entrance with
Dust outlet, the ash-laden gas entrance are connected with raw coke oven gas outlet.
Especially, the hot precipitator includes：Casing 11, dust removal and filtration component 12 and transmission device (not shown).
As shown in Fig. 2 the casing 11 is provided with filter chamber 111 and dirt pocket 112, the filter chamber 111, which is provided with, to be contained
Dust and gas entrance 1111 and clean gas outlet 1112, the dirt pocket 112 are provided with blowback air entrance 1121 and dust outlet 1122.
As shown in Fig. 2 the dust removal and filtration component 12 is embedded in the filter chamber 111 and dirt pocket 112；Hot precipitator
1 is rotary metal sintered filter, and dust removal and filtration component 12 can be metal sintering filter cake, and preferably superalloy powder burns
Knot, when its duct is 0.5~70 μm, and porosity is 15~50%, pass through dust content ＜ in raw coke oven gas after hot precipitator
0.5% (Wt).
As shown in Fig. 2 the ash-laden gas entrance 1111 and clean gas outlet 1112 are located at the dust removal and filtration member device respectively
The both sides up and down of part 12, the blowback air entrance 1121 is with dust outlet 1122 respectively positioned at the dust removal and filtration component 12
Upper and lower both sides；
As shown in Fig. 2 the transmission device is connected with the dust removal and filtration component, removed described in the transmission device drive
Dirt filters component 12 and rotated around the axis of the casing 11.The transmission device can pass through gear and dust removal and filtration member
The engagement connection of device 12, it is not excluded that can be rotated by other kind of drive dust removal and filtration components.
The dust removal and filtration component 12 is exotic material, and it can be metal sintering filter cake, it is preferable that optional metal
Powder sintered, especially superalloy powder sinters, because it has good high-temperature stability so that described in the utility model
Hot precipitator 1 can be in 500~900 DEG C of high-effective dust-removings.
As depicted in figs. 1 and 2, raw coke oven gas is passed through the dust removal and filtration component 1 from the ash-laden gas entrance 1111, passed through
Dedusting is carried out to the dusty gas by the dust removal and filtration component 1, is purified gas from the clean gas outlet 1112
Discharge；The dust removal and filtration component 1 is driven to be rotated around the axis of the casing 11 by transmission device；Enter from the blowback air
Mouth 1121 is blown into blowback air, and the dust (i.e. coke powder) in the dust removal and filtration component 1 is blown out from the dust outlet 1122.
Therefore, hot precipitator 1 can be directly realized by the dust removal by filtration of 600~650 DEG C of gas, in no cooling down bar
Under part, carry out the separation of raw coke oven gas and coke powder, dustiness is few in raw coke oven gas, more avoid in later stage Process of Tar Processing tar and
The separation of coke powder, tar quality can be improved.
The system also includes coke powder collection device 4 and refrigerated separation device 5, and refrigerated separation device 5 enters with purified gas
Mouth, tar outlet and pyrolysis gas outlet, the purified gas entrance are connected with the clean gas outlet.High temperature after separation is waste
Coal gas is sent into refrigerated separation device 5.Coke powder collection device 4 collects coke powder caused by the hot precipitator 1, and is passed through the oxygen
Hot furnace of calcium carbide 2, continue to smelt production calcium carbide product as raw material.Whole calcium carbide preparation process does not have dust emission, realizes material
Complete utilization.
The utility model further relates to a kind of method that calcium carbide is produced using said system, comprises the following steps：
Raw material lime and coal are sent into the down-flow fluidized bed using ECT pyrolysis oven 2 to be pyrolyzed, obtain high temperature raw coke oven gas, high-temperature semi-coke and
Lime, discharge high temperature raw coke oven gas is exported from raw coke oven gas, discharge high-temperature semi-coke and lime are exported from solid material；
The high temperature raw coke oven gas is passed through the hot precipitator 1 and is blown into blowback air from the blowback air entrance, is carried out
The high temperature raw coke oven gas dust removal by filtration, the high temperature raw coke oven gas after clean gas outlet discharge dust removal by filtration, from the dust
Outlet discharge coke powder；
The high-temperature semi-coke and lime are passed through the hot furnace of calcium carbide 3 of the oxygen, and will be made from the oxygen coal entrance with oxygen
Spray to the hot furnace of calcium carbide of the oxygen for the microfine coal of carrier gas and prepare calcium carbide.
System for producing calcium carbide described in the utility model and method employ new hot precipitator, can handle High Temperature Gas
Body, can 500~900 DEG C of high temperature resistant；Dust removal and filtration component does not have by rotation mode Chalk-dust filtering and blowback, the dust of filtering
Accumulation, is not easily blocked, and efficiency of dust collection is high.
Further, methods described is further comprising the steps of：
Coke powder caused by the hot precipitator 1 is collected with the coke powder collection device 4, and is passed through the hot furnace of calcium carbide of the oxygen
3 to prepare calcium carbide.
Down-flow fluidized bed using ECT pyrolysis oven and the coupling of oxygen thermoelectricity stone furnace technology, the calcium carbide tail gas sensible heat that make use of the hot furnace of calcium carbide of oxygen are pyrolysis
Stove provides heat, reduces system energy consumption.
Further, methods described is further comprising the steps of：
High temperature raw coke oven gas after dust removal by filtration is passed through the refrigerated separation device 5, carries out the cooling point of high temperature raw coke oven gas
From obtaining tar and pyrolysis gas.
Further, methods described is further comprising the steps of：
Break process is carried out to raw material lime with the lime breaker 7, with the raw coal disintegrating machine 6 to feed coal
Carry out break process, and will it is broken after lime and particle diameter be that 1~3mm coal grains are passed through the down-flow fluidized bed using ECT pyrolysis oven 2；
The coal grain of the particle diameter ＜ 1mm after crushing is handled with the ultra-fine preparation facilities 8 of the raw coal, prepares fine Coal
Powder.
It should be noted that each embodiment above by reference to described by accompanying drawing is only illustrating the utility model rather than limit
The scope of the utility model processed, it will be understood by those within the art that, do not departing from spirit of the present utility model and model
The modification carried out on the premise of enclosing to the utility model or equivalent substitution, all should cover within the scope of the utility model.
In addition, unless stated otherwise, then all or part of of any embodiment can be with reference to the whole or one of any other embodiment
Part uses.
Claims (9)
- A kind of 1. system for producing calcium carbide, it is characterised in that including：The hot furnace of calcium carbide of down-flow fluidized bed using ECT pyrolysis oven, oxygen and hot precipitator, Wherein,The down-flow fluidized bed using ECT pyrolysis oven includes material inlet, solid material outlet and raw coke oven gas outlet, calcium carbide tail gas entrance；The hot furnace of calcium carbide of oxygen includes oxygen coal entrance, expects import, calcium carbide outlet and calcium carbide tail gas outlet, the oxygen thermoelectricity admittedly The solid material outlet of the solid material import of stone stove and the down-flow fluidized bed using ECT pyrolysis oven is connected, the calcium carbide tail gas outlet of the hot furnace of calcium carbide of oxygen and The calcium carbide tail gas entrance of the down-flow fluidized bed using ECT pyrolysis oven is connected；The hot precipitator is used to carry out dust removal by filtration, the high temperature to high temperature raw coke oven gas caused by the down-flow fluidized bed using ECT pyrolysis oven Deduster includes ash-laden gas entrance, clean gas outlet, blowback air entrance and dust outlet, the ash-laden gas entrance with it is described descending The raw coke oven gas outlet of bed pyrolysis oven is connected.
- 2. the system as claimed in claim 1, it is characterised in that the hot precipitator includes casing, and the casing is provided with Filter chamber and dirt pocket, the ash-laden gas entrance and clean gas outlet are arranged on the filter chamber, the blowback air entrance and powder Dirt outlet is arranged on the dirt pocket.
- 3. system as claimed in claim 2, it is characterised in that the hot precipitator includes dust removal and filtration component, described Dust removal and filtration component is embedded in the filter chamber and dirt pocket；WhereinThe ash-laden gas entrance and clean gas outlet are located at the both sides up and down of the dust removal and filtration component, the blowback air respectively Entrance is located at the both sides up and down of the dust removal and filtration component with dust outlet respectively.
- 4. system as claimed in claim 3, it is characterised in that the hot precipitator includes transmission device, and it is removed with described Dirt filtering component connection, the transmission device drive the dust removal and filtration component to be rotated around the axis of the casing.
- 5. the system as claimed in claim 1, it is characterised in that the system also includes coke powder collection device, described for collecting Coke powder caused by hot precipitator, and it is passed through the hot furnace of calcium carbide of the oxygen.
- 6. the system as claimed in claim 1, it is characterised in that the system also includes refrigerated separation device, and it has purified gas Entrance, tar outlet and pyrolysis gas outlet, the purified gas entrance of the refrigerated separation device are net with the hot precipitator Change gas outlet to be connected.
- 7. the system as claimed in claim 1, it is characterised in that the system also includes lime breaker, and it is connected to described The material inlet of down-flow fluidized bed using ECT pyrolysis oven.
- 8. the system as claimed in claim 1, it is characterised in that the system also includes raw coal disintegrating machine, and it is connected to described The material inlet of down-flow fluidized bed using ECT pyrolysis oven.
- 9. the system as claimed in claim 1, it is characterised in that the system also includes the ultra-fine preparation facilities of raw coal, and it is connected to The oxygen coal entrance of the hot furnace of calcium carbide of oxygen.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720420071.6U CN206692332U (en) | 2017-04-20 | 2017-04-20 | System for producing calcium carbide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720420071.6U CN206692332U (en) | 2017-04-20 | 2017-04-20 | System for producing calcium carbide |
Publications (1)
| Publication Number | Publication Date |
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| CN206692332U true CN206692332U (en) | 2017-12-01 |
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ID=60445714
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| Application Number | Title | Priority Date | Filing Date |
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| CN201720420071.6U Expired - Fee Related CN206692332U (en) | 2017-04-20 | 2017-04-20 | System for producing calcium carbide |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107055536A (en) * | 2017-04-20 | 2017-08-18 | 神雾环保技术股份有限公司 | System for producing calcium carbide and method |
-
2017
- 2017-04-20 CN CN201720420071.6U patent/CN206692332U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107055536A (en) * | 2017-04-20 | 2017-08-18 | 神雾环保技术股份有限公司 | System for producing calcium carbide and method |
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