CN106517205A - Calcium carbide production system capable of recovering and utilizing high-temperature raw coke oven gas waste heat, and calcium carbide production method - Google Patents
Calcium carbide production system capable of recovering and utilizing high-temperature raw coke oven gas waste heat, and calcium carbide production method Download PDFInfo
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- CN106517205A CN106517205A CN201611128349.9A CN201611128349A CN106517205A CN 106517205 A CN106517205 A CN 106517205A CN 201611128349 A CN201611128349 A CN 201611128349A CN 106517205 A CN106517205 A CN 106517205A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention relates to a calcium carbide production system capable of recovering and utilizing high-temperature raw coke oven gas waste heat, and a calcium carbide production method. The system comprises a feed coal crushing system, a downer thermal decomposition furnace, a lime crushing unit, a CaC2 reactor and a moving bed heat exchanger unit. The feed coal crushing system comprises a feed coal inlet and a coal outlet; the downer thermal decomposition furnace comprises a coal inlet, a high-temperature raw coke oven gas outlet, a heating lime upper sieved material inlet and a high-temperature carbocoal and lime outlet; the lime crushing unit comprises a lime inlet, an upper sieved material outlet and a lower sieved material outlet; the moving bed heat exchanger unit comprises a lime upper sieved material inlet, a high-temperature raw coke oven gas inlet and a heating lime lower sieved material outlet; and the CaC2 reactor comprises a calcium carbide raw material inlet and a calcium carbide product outlet. According to the calcium carbide production system capable of recovering and utilizing the high-temperature raw coke oven gas waste heat, and the calcium carbide production method provided by the invention, the thermal decomposed carbocoal and heating lime are thermal-state conveyed to the CaC2 reactor for smelting the calcium carbide, and further, the system effectively utilizes the high-temperature raw coke oven gas waste heat produced by thermal decomposition, so that the cost of raw materials is reduced, and meanwhile, the energy consumption during a calcium carbide smelting process is saved.
Description
Technical field
The invention mainly relates to the production field of carbide, and in particular to a kind of production system of the carbide that raw coke oven gas is recycled
System and method.
Background technology
Carbide as a kind of important industrial chemicals, mainly for the production of acetylene and ethynylation chemical product, acetylene once by
It is described as " mother of organic synthesiss industry ".Consider from National energy distribution, " rich coal, oil-poor, few gas " is China's energy resource structure
Characteristic feature, coal are the main energy sources of China, account for the 70% of primary energy, therefore, using coal production carbide, carbide and
Water reaction obtains acetylene, and Development of Coal ethyl-acetylene chemical industry is significant for Industrial Economic Development.
Traditional carbide production mainly adopts electrothermal way, i.e., with lump lime and block coke as raw material, in furnace of calcium carbide
By electric arc heated to more than 2000 degrees Celsius, by equation CaO+3C=CaC2The reaction principle of+CO carries out pyrolytic semlting production electricity
Stone.Consider from the requirement to carbon raw, traditional carbide production technology is primarily present following defect：(1) require carbon materials
Granularity is in 5-30mm, fixed carbon content>84%th, ash<15%, disclosure satisfy that only coke, semicoke, the petroleum coke of these requirements
And some high-quality anthracites, and these raw material reserves are extremely limited, it is expensive；(2) can be with raw material shattering process
The raw material of 15-20% goes out of use as granularity is less than 5mm, causes the serious waste of resource；(3) mainly adopt in carbide production
Block carbon raw material and Calx, mass transfer and heat transfer efficiency it is low, reaction rate is relatively low, and it is only 50% left that carbide smelts furnace thermal efficiency
The right side, power consumption are up to 3250kWh/t carbides or so.It can be seen that, the quality of carbon raw directly affects the Yield and quality of carbide, electric power
The economic indicator such as unit consumption and cost.
Consider from the property of raw coal, containing ash, sulfur and other a small amount of mineral in raw coal.Most of original pit ash is all high
In the ash requirements upper limit of carbide raw material, need to raw coal be carried out sorting deliming process.Wet method can be divided into by the difference of separating medium
Sorting and two big class of dry separation, during wet split, coal is fully contacted with water, increases coal selecting product moisture and follow-up carbon
The dehydration energy of raw material；And conventional dry separation adopts normal temperature air as separating medium, the surface moisture of raw coal increased
Contact sticking probability between granule, causes actual separating effect to be deteriorated.In addition, in recent years, journey is adopted as Coal Mechanical is melted
The raising of degree, fine coal content of the raw coal in recovery process account for 40-60%, and it is left that the poor low-order coal of hardness even accounts for 70%
The right side, this is obviously runed counter to more than 5mm with the granularity of traditional carbide manufacturing technique requirent carbon raw.
And during carbide is generated, have substantial amounts of waste heat to produce, energy has been wasted if not being used
Amount.
The shortcomings of to solve traditional carbide production technology to ingredient requirement harshness, highly energy-consuming, high pollution, poor benefit, widen
The scope of the carbon-based raw material of carbide, carbide production technology are further improved.
Therefore, for the problems referred to above, it is necessary to provide the production system and method for a kind of carbide, traditional carbide life can be solved
The problems such as production. art is to ingredient requirement harshness, highly energy-consuming, high pollution, poor benefit, and the waste gas in calcium carbide production process is carried out
Recycle.
The content of the invention
For the problems referred to above, the present invention is intended to provide a kind of production system of the carbide of high temperature raw coke oven gas heat recovery
And method, the purpose of the system and method be the waste heat for solving the problems, such as in carbide production technology waste, highly energy-consuming.Meanwhile, this
The bright high request that will solve the problems, such as carbide production technology to raw material.
The production system of the carbide of the high temperature raw coke oven gas heat recovery that the present invention is provided includes：The broken system of feed coal
System, down-flow fluidized bed using ECT pyrolysis oven, Calx fragmentation cell, CaC2Reactor and moving bed heat exchanger unit, wherein, the feed coal is crushed
System includes feed coal entrance and coal export, for the broken of feed coal；The down-flow fluidized bed using ECT pyrolysis oven includes portion disposed thereon
Coal entrance, the high temperature raw coke oven gas being located therein are exported, on the heating Calx of its underpart, sieve is expected entrance and is located at its bottom
High-temperature semi-coke and Calx export, for the pyrolysis of coal；The coal entrance is connected with the coal export of the feed coal crushing system；
The Calx fragmentation cell includes lime inlet, the outlet of upper sieve material and lower sieve material outlet, for the broken and screening of Calx；It is described
Moving bed heat exchanger unit includes that sieve material entrance, high temperature raw coke oven gas entrance, low temperature raw coke oven gas are exported and heated on Calx on Calx
Sieve material outlet, expects the heat exchange with pyrolysis oven high temperature raw coke oven gas for sieve on Calx；Sieve material entrance and the Calx on the Calx
The upper sieve material outlet of fragmentation cell is connected, and the high temperature raw coke oven gas entrance is exported with the high temperature raw coke oven gas of the down-flow fluidized bed using ECT pyrolysis oven
It is connected；Sieve material outlet on the heating Calx is connected with sieve material entrance on the heating Calx of the down-flow fluidized bed using ECT pyrolysis oven；It is described
CaC2Reactor includes carbide raw material entrance and the outlet of carbide material, for smelting synthesis carbide product；The carbide raw material entrance
It is connected with the high-temperature semi-coke of the down-flow fluidized bed using ECT pyrolysis oven with the lower sieve material outlet of Calx outlet, the Calx fragmentation cell respectively.
Further, above-mentioned system, the moving bed heat exchanger unit include raw material cabin, heat exchanger, sack cleaner；
The raw material cabin entrance is connected with the upper sieve material outlet of the Calx fragmentation cell；The raw material cabin outlet and the heat exchanger
Solid material inlet be connected；The solid matter outlet of the heat exchanger and the CaC2The carbide raw material entrance phase of reactor
Connection；The gas access of the heat exchanger is connected with the high temperature raw coke oven gas outlet of the down-flow fluidized bed using ECT pyrolysis oven；The heat exchanger
Gas outlet be connected with the gas access of the sack cleaner.
Said system also includes oil-water separation unit, and which includes the outlet of low temperature raw coke oven gas entrance, pyrolysis gas outlet and profit；
The low temperature raw coke oven gas entrance is connected with the low temperature raw coke oven gas outlet of the moving bed heat exchanger unit.
Said system may also include blending bunker, and which is located at the CaC2Before reactor, including sieve material entrance, height under Calx
Warm semicoke is exported with lime inlet and mixed material；Under the Calx, sieve material entrance expects with the lower sieve of the Calx fragmentation cell
Mouth is connected, and the high-temperature semi-coke is connected with Calx outlet with lime inlet with the high-temperature semi-coke of the down-flow fluidized bed using ECT pyrolysis oven, described
Mixed material is exported and the CaC2The carbide raw material entrance of reactor is connected.
The present invention also provides the production method that a kind of utilization said system carries out carbide, comprises the following steps：By feed coal
The down-flow fluidized bed using ECT pyrolysis oven is sent into after crushing by the feed coal crushing system to be pyrolyzed, high-temperature semi-coke is obtained；By Calx
After the Calx fragmentation cell crushing and screening described in, sieve material and lower sieve material are obtained；The upper sieve material is passed through the moving bed to change
Hot device unit obtains sieve material on high-temperature lime after being exchanged heat；The down-flow fluidized bed using ECT pyrolysis oven is passed through by material is sieved on the high-temperature lime
Bottom；The high-temperature semi-coke that the lower sieve material and the down-flow fluidized bed using ECT pyrolysis oven are discharged is sent into described with sieve material on high-temperature lime
CaC2Reactor is smelted, and obtains carbide；The high temperature raw coke oven gas of the down-flow fluidized bed using ECT pyrolysis oven is sent into into the moving bed heat exchange
Device unit.
Above-mentioned method, the temperature of the high temperature raw coke oven gas that the down-flow fluidized bed using ECT pyrolysis oven is produced is more than 800 DEG C.
Above-mentioned method, the temperature of the low temperature raw coke oven gas after heat exchange is 110-140 DEG C.
Above-mentioned method, it is described it is lower sieve material particle diameter ＜ 1mm, it is described it is upper sieve material particle diameter be 1mm-3mm, the feed coal
Particle diameter ＜ 3mm after broken.
Above-mentioned method, methods described also include step：The low temperature raw coke oven gas that the moving bed heat exchanger unit is discharged
Separated by oil-water separation unit, obtained pyrolysis gas and tar.
Above-mentioned technical proposal of the invention, can solve traditional carbide production technology to ingredient requirement harshness, high consumption
The problems such as energy, high pollution, poor benefit, and the waste gas in calcium carbide production process is recycled, reduce carbide and produced
The energy consumption of journey.
Description of the drawings
Fig. 1 is the production system flow chart of the carbide of the embodiment of the present invention.
Specific embodiment
Below in conjunction with drawings and Examples, the specific embodiment of the present invention is described in more details, so as to energy
The advantage of the solution of the present invention and various aspects is more fully understood enough.However, specific embodiments described below and enforcement
Example is only descriptive purpose, rather than limitation of the present invention.
The production system flow chart of the carbide of the high temperature raw coke oven gas heat recovery that Fig. 1 is provided for the present invention.
The system mainly includes feed coal crushing system, down-flow fluidized bed using ECT pyrolysis oven, Calx fragmentation cell, CaC2Reactor and shifting
Dynamic bed heat exchanger unit, is re-fed into the pyrolysis of down-flow fluidized bed using ECT pyrolysis oven, using stone after feed coal being crushed using feed coal crushing system
After grey fragmentation cell crushes Calx raw material, then coal dust is mixed feeding CaC with pulverized limestone2Reactor smelts synthesis carbide.Its
In, the recycling of high temperature raw coke oven gas energy is realized in moving bed heat exchanger unit.The present invention focus on break
Conventional each unit and CaC2The technique framework of reactor isolated operation, realizes the coupling of energy in production process, to producing
The heat produced in journey is recycled, and reduces CaC2The energy consumption of synthetic reaction, improves the efficiency of system.
Specifically, feed coal crushing system includes feed coal entrance and coal export, for the broken of feed coal.
Coal entrance that the down-flow fluidized bed using ECT pyrolysis oven includes portion disposed thereon, the high temperature raw coke oven gas being located therein outlet, position
Material entrance is sieved on the heating Calx of its underpart and the high-temperature semi-coke positioned at its bottom is exported with Calx, for the pyrolysis of coal；Institute
The coal export that coal entrance is stated with the feed coal crushing system is connected.
On heating Calx, sieve expects entrance for sieve material on the Calx after heat exchange is passed through down-flow fluidized bed using ECT pyrolysis oven again, its purpose
It is：First, for Calx is carried out post bake cracking with the tar that adsorbs in pyrolysis oil gas heat transfer process so as to which light component becomes
Pyrolysis gas, heavy constituent become fixed carbon.2nd, the Calx after heat exchanging carries out post bake, improves the Calx temperature into furnace of calcium carbide
Degree, saves furnace of calcium carbide power consumption.3rd, in Calx and high-temperature oil gas heat transfer process, the moisture content in high temperature raw coke oven gas can be absorbed, generates hydrogen
Calcium oxide, in pyrolysis oven, post bake makes which resolve into Calx (calcium oxide).
The Calx fragmentation cell includes lime inlet, the outlet of upper sieve material and lower sieve material outlet, for the broken of Calx with
Screening.
It should be noted that upper sieve material herein refers to lime particle or lime block, lower sieve material refers to pulverized limestone.
The moving bed heat exchanger unit includes sieve material entrance, high temperature raw coke oven gas entrance, the outlet of low temperature raw coke oven gas on Calx
Export with sieve material on heating Calx, for the heat exchange for sieving material and pyrolysis oven high temperature raw coke oven gas on Calx；On the Calx sieve expect into
Mouthful it is connected with the upper sieve material outlet of the Calx fragmentation cell, the height of the high temperature raw coke oven gas entrance and the down-flow fluidized bed using ECT pyrolysis oven
Warm raw coke oven gas outlet is connected；The outlet of sieve material and sieve material entrance on the heating Calx of the down-flow fluidized bed using ECT pyrolysis oven on the heating Calx
It is connected.
Specifically, the moving bed heat exchanger unit can further include raw material cabin, heat exchanger, sack cleaner；It is described
Raw material cabin entrance is connected with the upper sieve material outlet of the Calx fragmentation cell；The raw material cabin outlet is consolidated with the heat exchanger
Body material inlet is connected；The solid matter outlet of the heat exchanger and the CaC2The carbide raw material entrance of reactor is connected
Connect；The gas access of the heat exchanger is connected with the high temperature raw coke oven gas outlet of the down-flow fluidized bed using ECT pyrolysis oven；The heat exchanger
Gas outlet is connected with the gas access of the sack cleaner.
The CaC2Reactor includes carbide raw material entrance and the outlet of carbide material, for smelting synthesis carbide product；It is described
Carbide raw material entrance high-temperature semi-coke and Calx outlet, the lower sieve of the Calx fragmentation cell respectively with the down-flow fluidized bed using ECT pyrolysis oven
Material outlet is connected.
In order to recycle the oil gas product that pyrolysis is produced, system may also include oil-water separation unit, and which includes that low temperature is waste
The outlet of gas entry, pyrolysis gas outlet and profit；The low temperature of the low temperature raw coke oven gas entrance and the moving bed heat exchanger unit
Raw coke oven gas outlet is connected.
Coal after pyrolysis sends into CaC with sieve material under sieve material on Calx and Calx2Before reactor, in order to realize after pyrolysis
The sensible heat utilization of solid material, needs mix several materials, thus above-mentioned system may also include blending bunker, and which is located at
The CaC2Before reactor, including sieve material entrance, high-temperature semi-coke and lime inlet and mixed material outlet under Calx；The stone
The lower sieve material entrance of ash is connected with the lower sieve material outlet of the Calx fragmentation cell, the high-temperature semi-coke and lime inlet with it is described under
The high-temperature semi-coke of row bed pyrolysis oven is connected with Calx outlet, and the mixed material is exported and the CaC2The carbide raw material of reactor
Entrance is connected.
The concrete operation step of the production method of the carbide of the high temperature raw coke oven gas heat recovery that the present invention is provided is as follows：
Feed coal is crushed to ＜ 3mm into fast pyrogenation stove, and fast pyrogenation reaction occurs at 800-900 DEG C, high temperature is generated
The high-temperature semi-coke of raw coke oven gas and more than 800 DEG C.High temperature raw coke oven gas is produced by the middle part of fast pyrogenation stove, into moving bed heat exchanger,
The lime block of the 1mm-3mm produced with Calx fragmentation cell is exchanged heat, and the low temperature raw gas temperature after heat exchange is controlled in 110-
140 DEG C, oil-water separation unit is entered back into afterwards further lowered the temperature and separate and collect with oil, gas and water.
Calx Jing after Calx fragmentation cell crushing and screening, the powdered lime of ＜ 1mm and fast pyrogenation furnace bottom height out
Warm solid semicoke and Calx enter CaC in the lump2Reactor.The block Calx of 1mm-3mm enters moving bed heat exchanger unit.It is block
The high temperature raw coke oven gas heat exchange of Calx and more than 800 DEG C, reclaims 800 DEG C and is down to 110-140 DEG C of high temperature crude-gas sensible heat.
Due to Calx main component be CaO, the effect with catalytic tar second pyrolysises, Calx with high temperature raw coke oven gas
Absorption while heat exchange is down to the 110-140 DEG C of tar for condensing by 800 DEG C, and carries out part quadric catalysis cracking, cracks
Remainder tar is entered in stove from fast pyrogenation stove lower sides after being adsorbed by Calx, carries out secondary high-temperature catalytic pyrolysiss.
The high-temperature semi-coke and Calx discharged from fast pyrogenation furnace bottom enters CaC after mixing with the cold Calx of ＜ 1mm2Reaction
, there is chemical reaction more than 1800 DEG C and generate CaC in device2With the calcium carbide stove exhaust based on CO.
The production system and method for the carbide provided from such scheme, the present invention, it is waste by block Calx and high temperature
Coal gas-gas heat exchange, can reclaim high temperature crude-gas sensible heat, and the raw coke oven gas produced in solving traditional carbide smelting process does not have remaining
Recuperation of heat, but direct water-cooling oil gas collection, heat loss are big, and efficiency is low.
The present invention makes pyrolysis unit and CaC2Generator carries out energy coupling, except above-mentioned high temperature crude-gas sensible heat is reclaimed
Outward, after being also capable of achieving to be pyrolyzed, the sensible heat utilization of solid material, reduces CaC2The energy consumption of synthetic reaction, improves the efficiency of system,
Break in traditional carbide smelting process, pyrolysis unit and carbide smelting unit are relatively independent, and two units do not have energy coupling
Technique framework, solve the problems, such as that system energy consumption is big.
Meanwhile, the system can carry out the production of carbide using powder material, overcome traditional carbide production technology to raw material
The shortcomings of requiring harshness, highly energy-consuming, high pollution, poor benefit.
Technical scheme is illustrated with reference to specific embodiment.
In following embodiments, institute's taking technique condition value is exemplary, and its desirable numerical range is as indicated above in book
It is shown.
Embodiment 1
The system includes feed coal fragmentation cell, down-flow fluidized bed using ECT pyrolysis oven, CaC2Reactor, Calx fragmentation cell, moving bed
Heat exchanger unit and oil-water separation unit.Feed coal crushing system, down-flow fluidized bed using ECT pyrolysis oven, CaC2Reactor is sequentially connected；Calx
Fragmentation cell, moving bed heat exchanger unit, down-flow fluidized bed using ECT pyrolysis oven bottom are sequentially connected；In the middle part of down-flow fluidized bed using ECT pyrolysis oven, moving bed changes
Hot device, oil-water separation unit are sequentially connected.
Feed coal is crushed to into ＜ 3mm and sends into fast pyrogenation stove, fast pyrogenation reaction occurs at 820 DEG C or so, generated high
The high-temperature semi-coke of warm raw coke oven gas and more than 800 DEG C.High temperature raw coke oven gas is produced by the middle part of fast pyrogenation stove, is exchanged heat into moving bed
Device, the 1mm-3mm Calx produced with Calx fragmentation cell are exchanged heat, and the low temperature raw gas temperature after heat exchange is controlled at 110 DEG C
Left and right, is further lowered the temperature into oil-water separation unit afterwards and separate and collect with oil, gas and water.
Jing after Calx fragmentation cell crushing and screening, the block Calx of 1mm-3mm enters moving bed heat exchanger unit to Calx, with
More than 800 DEG C of high temperature raw coke oven gas heat exchange, reclaims 800 DEG C of near 110 DEG C of crude-gas sensible heats.The powdered lime of ＜ 1mm with it is quick
Pyrolysis furnace bottom high-temp solid semicoke out and Calx enter CaC in the lump2Reactor.
Due to Calx main component be CaO, the effect with catalytic tar second pyrolysises, Calx with high temperature raw coke oven gas
Absorption while heat exchange is down to 110 DEG C of tar for condensing by 800 DEG C, and carries out part quadric catalysis cracking, and cracking is remaining
Part tar is entered in stove from fast pyrogenation stove lower sides after being adsorbed by Calx, carries out secondary high-temperature catalytic pyrolysiss.
The high-temperature semi-coke and Calx discharged from fast pyrogenation furnace bottom enters CaC after mixing with the cold Calx of ＜ 1mm2Reaction
, there is chemical reaction more than 1800 DEG C and generate CaC in device2With the calcium carbide stove exhaust based on CO.
Embodiment 2
The system includes feed coal fragmentation cell, down-flow fluidized bed using ECT pyrolysis oven, CaC2Reactor, Calx fragmentation cell, moving bed
Heat exchanger unit and oil-water separation unit.Feed coal crushing system, down-flow fluidized bed using ECT pyrolysis oven, CaC2Reactor is sequentially connected；Calx
Fragmentation cell, moving bed heat exchanger unit, down-flow fluidized bed using ECT pyrolysis oven bottom are sequentially connected；In the middle part of down-flow fluidized bed using ECT pyrolysis oven, moving bed changes
Hot device, oil-water separation unit are sequentially connected.
Feed coal is crushed to into ＜ 3mm and sends into fast pyrogenation stove, fast pyrogenation reaction occurs at 850 DEG C or so, generated high
The high-temperature semi-coke of warm raw coke oven gas and more than 800 DEG C.High temperature raw coke oven gas is produced by the middle part of fast pyrogenation stove, is exchanged heat into moving bed
Device, the 1mm-3mm Calx produced with Calx fragmentation cell are exchanged heat, and the raw gas temperature after heat exchange is controlled at 125 DEG C or so,
Further lowered the temperature and oil-water separation and collection into oil-water separation unit afterwards.
Jing after Calx fragmentation cell crushing and screening, the block Calx of 1mm-3mm enters moving bed heat exchanger unit to Calx, with
More than 800 DEG C of high temperature raw coke oven gas heat exchange, reclaims 800 DEG C of near 125 DEG C of crude-gas sensible heats.The powdered lime of ＜ 1mm with it is quick
Pyrolysis furnace bottom high-temp solid semicoke out and Calx enter CaC in the lump2Reactor.
Due to Calx main component be CaO, the effect with catalytic tar second pyrolysises, Calx with high temperature raw coke oven gas
Absorption while heat exchange is down to 125 DEG C of tar for condensing by 800 DEG C, and carries out part quadric catalysis cracking, and cracking is remaining
Part tar is entered in stove from fast pyrogenation stove lower sides after being adsorbed by Calx, carries out secondary high-temperature catalytic pyrolysiss.
The high-temperature semi-coke and Calx discharged from fast pyrogenation furnace bottom enters CaC after mixing with the cold Calx of ＜ 1mm2Reaction
, there is chemical reaction more than 1800 DEG C and generate CaC in device2With the calcium carbide stove exhaust based on CO.
Embodiment 3
The system includes feed coal fragmentation cell, down-flow fluidized bed using ECT pyrolysis oven, CaC2Reactor, Calx fragmentation cell, moving bed
Heat exchanger unit and oil-water separation unit.Feed coal crushing system, down-flow fluidized bed using ECT pyrolysis oven, CaC2Reactor is sequentially connected；Calx
Fragmentation cell, moving bed heat exchanger unit, down-flow fluidized bed using ECT pyrolysis oven bottom are sequentially connected；In the middle part of down-flow fluidized bed using ECT pyrolysis oven, moving bed changes
Hot device, oil-water separation unit are sequentially connected.
Feed coal is crushed to into ＜ 3mm and sends into fast pyrogenation stove, fast pyrogenation reaction occurs at 900 DEG C or so, generated high
The high-temperature semi-coke of warm raw coke oven gas and more than 800 DEG C.High temperature raw coke oven gas is produced by the middle part of fast pyrogenation stove, is exchanged heat into moving bed
Device, the 1mm-3mm Calx produced with Calx fragmentation cell are exchanged heat, and the raw gas temperature after heat exchange is controlled at 140 DEG C or so,
Further lowered the temperature and oil-water separation and collection into oil-water separation unit afterwards.
Jing after Calx fragmentation cell crushing and screening, the block Calx of 1mm-3mm enters moving bed heat exchanger unit to Calx, with
More than 800 DEG C of high temperature raw coke oven gas heat exchange, reclaims 800 DEG C and is down to 140 DEG C of crude-gas sensible heats.The powdered lime of ＜ 1mm with it is quick
Pyrolysis furnace bottom high-temp solid semicoke out and Calx enter CaC in the lump2Reactor.
Due to Calx main component be CaO, the effect with catalytic tar second pyrolysises, Calx with high temperature raw coke oven gas
Absorption while heat exchange is down to 140 DEG C of tar for condensing by 800 DEG C, and carries out part quadric catalysis cracking, and cracking is remaining
Part tar is entered in stove from fast pyrogenation stove lower sides after being adsorbed by Calx, carries out secondary high-temperature catalytic pyrolysiss.
The high-temperature semi-coke and Calx discharged from fast pyrogenation furnace bottom enters CaC after mixing with the cold Calx of ＜ 1mm2Reaction
, there is chemical reaction more than 1800 DEG C and generate CaC in device2With the calcium carbide stove exhaust based on CO.
As seen from the above-described embodiment, technical scheme energy effectively utilizes are pyrolyzed the calorific value of high-temp solid, effectively profit
High temperature crude-gas sensible heat is used, carbide can be produced using powder material, be developed towards the maximized direction of resource and energy utilization, it is right
Whole carbide production industry suffers from positive effect with social environment.
Finally it should be noted that：Obviously, above-described embodiment is only intended to clearly illustrate example of the present invention, and and
The non-restriction to embodiment.For those of ordinary skill in the field, can also do on the basis of the above description
Go out the change or variation of other multi-forms.There is no need to be exhaustive to all of embodiment.And thus drawn
Obvious change that Shen goes out or among changing still in protection scope of the present invention.
Claims (9)
1. a kind of production system of the carbide of high temperature raw coke oven gas heat recovery, the system include feed coal crushing system,
Down-flow fluidized bed using ECT pyrolysis oven, Calx fragmentation cell, CaC2Reactor and moving bed heat exchanger unit, wherein,
The feed coal crushing system includes feed coal entrance and coal export, for the broken of feed coal；
Coal entrance that the down-flow fluidized bed using ECT pyrolysis oven includes portion disposed thereon, the high temperature raw coke oven gas being located therein outlet, positioned at which
On the heating Calx of bottom, sieve material entrance and the high-temperature semi-coke positioned at its bottom are exported with Calx, for the pyrolysis of coal；The coal
Entrance is connected with the coal export of the feed coal crushing system；
The Calx fragmentation cell includes lime inlet, the outlet of upper sieve material and lower sieve material outlet, for the broken and screening of Calx；
The moving bed heat exchanger unit includes that sieve material entrance, high temperature raw coke oven gas entrance, low temperature raw coke oven gas are exported and added on Calx
Sieve material outlet on hot Calx, expects the heat exchange with pyrolysis oven high temperature raw coke oven gas for sieve on Calx；On the Calx sieve material entrance with
The upper sieve material outlet of the Calx fragmentation cell is connected, and the high temperature raw coke oven gas entrance is waste with the high temperature of the down-flow fluidized bed using ECT pyrolysis oven
Gas exit is connected；The outlet of sieve material and sieve material entrance phase on the heating Calx of the down-flow fluidized bed using ECT pyrolysis oven on the heating Calx
Even；
The CaC2Reactor includes carbide raw material entrance and the outlet of carbide material, for smelting synthesis carbide product；The carbide is former
Lower sieve material of the material entrance respectively with the high-temperature semi-coke of the down-flow fluidized bed using ECT pyrolysis oven with Calx outlet, the Calx fragmentation cell is exported
It is connected.
2. system according to claim 1, it is characterised in that the moving bed heat exchanger unit includes raw material cabin, heat exchange
Device, sack cleaner；The raw material cabin entrance is connected with the upper sieve material outlet of the Calx fragmentation cell；The raw material cabin goes out
Mouth is connected with the solid material inlet of the heat exchanger；The solid matter outlet of the heat exchanger and the CaC2Reactor
Carbide raw material entrance is connected；The gas access of the heat exchanger is connected with the high temperature raw coke oven gas outlet of the down-flow fluidized bed using ECT pyrolysis oven
Connect；The gas outlet of the heat exchanger is connected with the gas access of the sack cleaner.
3. system according to claim 1, it is characterised in that the system also includes oil-water separation unit, and which includes low
The outlet of warm raw coke oven gas entrance, pyrolysis gas outlet and profit；The low temperature raw coke oven gas entrance and the moving bed heat exchanger unit
The outlet of low temperature raw coke oven gas is connected.
4. system according to claim 1, it is characterised in that the system also includes blending bunker, and which is located at the CaC2Instead
Before answering device, including sieve material entrance, high-temperature semi-coke and lime inlet and mixed material outlet under Calx；Under the Calx sieve expect into
Mouthful be connected with the lower sieve material outlet of the Calx fragmentation cell, the high-temperature semi-coke and lime inlet and the down-flow fluidized bed using ECT pyrolysis oven
The outlet of high-temperature semi-coke and Calx be connected, the mixed material is exported and the CaC2The carbide raw material entrance of reactor is connected.
5. system described in a kind of any one of utilization claim 1 to 4 carries out the production method of carbide, comprises the following steps：
The down-flow fluidized bed using ECT pyrolysis oven is sent into after feed coal is crushed by the feed coal crushing system to be pyrolyzed, high temperature is obtained
Semicoke；
After by Calx Calx fragmentation cell crushing and screening described in, sieve material and lower sieve material are obtained；
The upper sieve material is passed through after the moving bed heat exchanger unit is exchanged heat and obtains sieve material on high-temperature lime；
Sieve material on the high-temperature lime is passed through into the bottom of the down-flow fluidized bed using ECT pyrolysis oven；
The high-temperature semi-coke that the lower sieve material and the down-flow fluidized bed using ECT pyrolysis oven are discharged sends into the CaC with sieve material on high-temperature lime2Instead
Answer device to be smelted, obtain carbide；
The raw coke oven gas of the down-flow fluidized bed using ECT pyrolysis oven is sent into into the moving bed heat exchanger unit.
6. method according to claim 5, it is characterised in that the temperature of the high temperature raw coke oven gas that the down-flow fluidized bed using ECT pyrolysis oven is produced
Spend for more than 800 DEG C.
7. method according to claim 5, it is characterised in that the temperature of the low temperature raw coke oven gas after heat exchange is 110-
140℃。
8. method according to claim 5, it is characterised in that the particle diameter ＜ 1mm of the lower sieve material, the grain of the upper sieve material
Footpath is 1mm-3mm, particle diameter ＜ 3mm after the feed coal is broken.
9. method according to claim 5, it is characterised in that methods described also includes step：The moving bed is exchanged heat
The low temperature raw coke oven gas that device unit is discharged is separated by oil-water separation unit, obtains pyrolysis gas and tar.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611128349.9A CN106517205A (en) | 2016-12-09 | 2016-12-09 | Calcium carbide production system capable of recovering and utilizing high-temperature raw coke oven gas waste heat, and calcium carbide production method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611128349.9A CN106517205A (en) | 2016-12-09 | 2016-12-09 | Calcium carbide production system capable of recovering and utilizing high-temperature raw coke oven gas waste heat, and calcium carbide production method |
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| CN106517205A true CN106517205A (en) | 2017-03-22 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108913880A (en) * | 2018-08-27 | 2018-11-30 | 攀钢集团攀枝花钢铁研究院有限公司 | Using the molding method of raw coke oven gas supplies and for the material of smelting iron and steel |
| CN109055735A (en) * | 2018-08-27 | 2018-12-21 | 攀钢集团攀枝花钢铁研究院有限公司 | Using the molding method of raw coke oven gas supplies and for the material of smelting iron and steel |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105858660A (en) * | 2016-03-30 | 2016-08-17 | 神雾环保技术股份有限公司 | System and method for preparing calcium carbide |
| CN206266231U (en) * | 2016-12-09 | 2017-06-20 | 神雾环保技术股份有限公司 | A kind of production system of the calcium carbide of high temperature raw coke oven gas heat recovery |
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2016
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105858660A (en) * | 2016-03-30 | 2016-08-17 | 神雾环保技术股份有限公司 | System and method for preparing calcium carbide |
| CN206266231U (en) * | 2016-12-09 | 2017-06-20 | 神雾环保技术股份有限公司 | A kind of production system of the calcium carbide of high temperature raw coke oven gas heat recovery |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108913880A (en) * | 2018-08-27 | 2018-11-30 | 攀钢集团攀枝花钢铁研究院有限公司 | Using the molding method of raw coke oven gas supplies and for the material of smelting iron and steel |
| CN109055735A (en) * | 2018-08-27 | 2018-12-21 | 攀钢集团攀枝花钢铁研究院有限公司 | Using the molding method of raw coke oven gas supplies and for the material of smelting iron and steel |
| CN109055735B (en) * | 2018-08-27 | 2019-11-12 | 攀钢集团攀枝花钢铁研究院有限公司 | Using the molding method of raw coke oven gas supplies and for the material of smelting iron and steel |
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