CN107880920A - A kind of burnt method and system of batch coking production negative pole - Google Patents
A kind of burnt method and system of batch coking production negative pole Download PDFInfo
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- CN107880920A CN107880920A CN201711200316.5A CN201711200316A CN107880920A CN 107880920 A CN107880920 A CN 107880920A CN 201711200316 A CN201711200316 A CN 201711200316A CN 107880920 A CN107880920 A CN 107880920A
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- coking
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- coke
- oil
- negative pole
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- 238000004939 coking Methods 0.000 title claims abstract description 110
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 239000000571 coke Substances 0.000 claims abstract description 73
- 239000010426 asphalt Substances 0.000 claims abstract description 49
- 239000000203 mixture Substances 0.000 claims abstract description 48
- 239000003245 coal Substances 0.000 claims abstract description 35
- 238000006116 polymerization reaction Methods 0.000 claims abstract description 27
- 238000001035 drying Methods 0.000 claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 22
- 238000005520 cutting process Methods 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000000463 material Substances 0.000 claims abstract description 13
- 238000000746 purification Methods 0.000 claims abstract description 13
- 239000011294 coal tar pitch Substances 0.000 claims abstract description 12
- 238000000605 extraction Methods 0.000 claims abstract description 10
- 238000005235 decoking Methods 0.000 claims abstract description 6
- 238000010438 heat treatment Methods 0.000 claims description 13
- 238000011084 recovery Methods 0.000 claims description 10
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 8
- 239000011271 tar pitch Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 5
- 239000011295 pitch Substances 0.000 claims description 5
- 239000002994 raw material Substances 0.000 claims description 5
- 238000013019 agitation Methods 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- 239000012535 impurity Substances 0.000 claims description 3
- 238000011068 loading method Methods 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 230000013872 defecation Effects 0.000 claims 1
- 239000011269 tar Substances 0.000 abstract description 7
- 239000003921 oil Substances 0.000 description 37
- 239000000047 product Substances 0.000 description 28
- 239000011280 coal tar Substances 0.000 description 10
- 238000012545 processing Methods 0.000 description 7
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 4
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 229910052744 lithium Inorganic materials 0.000 description 4
- 229910001416 lithium ion Inorganic materials 0.000 description 4
- 239000003575 carbonaceous material Substances 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000005553 drilling Methods 0.000 description 2
- 239000002006 petroleum coke Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000009831 deintercalation Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 230000016507 interphase Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000004005 microsphere Substances 0.000 description 1
- 239000011331 needle coke Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000003981 vehicle Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M10/00—Secondary cells; Manufacture thereof
- H01M10/05—Accumulators with non-aqueous electrolyte
- H01M10/052—Li-accumulators
- H01M10/0525—Rocking-chair batteries, i.e. batteries with lithium insertion or intercalation in both electrodes; Lithium-ion batteries
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M4/00—Electrodes
- H01M4/02—Electrodes composed of, or comprising, active material
- H01M4/36—Selection of substances as active materials, active masses, active liquids
- H01M4/58—Selection of substances as active materials, active masses, active liquids of inorganic compounds other than oxides or hydroxides, e.g. sulfides, selenides, tellurides, halogenides or LiCoFy; of polyanionic structures, e.g. phosphates, silicates or borates
- H01M4/583—Carbonaceous material, e.g. graphite-intercalation compounds or CFx
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M4/00—Electrodes
- H01M4/02—Electrodes composed of, or comprising, active material
- H01M4/62—Selection of inactive substances as ingredients for active masses, e.g. binders, fillers
- H01M4/624—Electric conductive fillers
- H01M4/625—Carbon or graphite
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/10—Energy storage using batteries
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Electrochemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Manufacturing & Machinery (AREA)
- Coke Industry (AREA)
Abstract
The present invention relates to the method and system that a kind of batch coking production negative pole is burnt, coal measures is refined after mix asphalt loads preheater preheating and delivers to coking reactor, polymerization, pyrogenetic reaction are successively completed in coking reactor, so with carrying out stripping purification, after stripping purification terminates, cold Jiao is carried out with water, hydraulic decoking is carried out with portable waterpower coke cutting machine；The coke removed falls into wet burnt transporter and is delivered to wet coke bin, is stored in wet coke bin and preliminary hydro-extraction, the coke through preliminary hydro-extraction are dried into drying machine, and the negative pole obtained after drying is burnt to enter finished product coke bin, is transported outward by the entrucking of finished product Jiao's conveyer.The present invention is realized using high temperature coal-tar pitch and middle coalite tar asphalt production negative pole Jiao, and has the advantages that technique is simple, and cost of material is low, good product quality.
Description
Technical field
The present invention relates to negative pole Jiao's production technical field, more particularly to a kind of burnt method of batch coking production negative pole and
System.
Background technology
China's coke output is about 4.5 hundred million tons, accounts for the 68% of world's coke total output, while the substantial amounts of high-temperature coal of by-product
Tar, and the country that high temperature coal-tar processing capacity is maximum.To the end of the year 2016, China's high temperature coal-tar working ability will exceed
25000000 tons, high temperature coal-tar process technology develops rapidly, and coal tar distillation list covering device ability has reached 500,000 tons/year.With
This simultaneously, coal tar down-stream product applications are constantly widened, people increasingly pay attention to high temperature coal-tar processing technical progress
Situation and developing direction.Bituminous production accounts for more than the 50% of tar production amount in high temperature coal-tar distillage, coal tar pitch
Processing and utilization to coal tar processing industry tool be of great significance.
In addition, coal is still main body in China's energy-consuming, and as environmental requirement is more and more stricter, the clean utilization of coal
Technology be have developed rapidly, and particularly coal gasification technology is widely applied.Semi-coke yield increased quickly in recent years, was coal in
The specialty industries of carbonization generation semi-coke, coal gas and middle coalite tar, realize coal to solid-state, liquid under cryogenic conditions
The Efficient Conversion of state, gaseous energy form, be country encourage the classification of coal sub-prime, one of the pattern that utilizes of green high-efficient.This
Coalite tars during sample is a large amount of with regard to by-product, it is pitch that the processing and utilization of middle coalite tar, which has 30% or so, low in this part
Warm coal tar asphalt is not well processed utilization, and the overwhelming majority is configured among fuel oil and supplying high-temperature coking coal, made
Into the wasting of resources.
Lithium ion battery is portable chemical power supply a kind of than energy highest at present, it have voltage it is high, it is bigger than energy,
Discharging voltage balance, low temperature performance well, security performance be excellent and storage and the advantages that long working life.With current electronic equipment
Miniaturization and the rapid development of miniaturization, and country encourage the policy of development energy saving vehicle and new-energy automobile, small lithium ion
The research of battery and dynamic lithium battery is also increasingly paid attention to application.
At present, it is to find a kind of special negative material to carry out substituted metal to develop one of main task of lithium ion battery
Lithium, it should have alap operating potential, while have sufficiently high lithium embedded quantity and good lithium deintercalation invertibity again,
To ensure high voltage, Large Copacity and the requirement having extended cycle life.In numerous negative materials, carbon material application the most into
Work(.Compared with other insert materials, Carbon Materials possess high faraday's capacity, high circulation efficiency, and low electrode current potential and length are followed
The ring life-span.But up to the present also mainly there is interphase without special negative pole carbon material, lithium ion battery negative material
Carbon microspheres, native graphite, petroleum coke and needle coke, and these materials are in the equal Shortcomings of cost and properties of product etc., because
It is burnt significant that this develops a kind of charcoal negative pole specialty.
The content of the invention
The invention provides the method and system that a kind of batch coking production negative pole is burnt, realize and utilize high temperature coal-tar
Pitch and middle coalite tar asphalt production negative pole are burnt, and have the advantages that technique is simple, and cost of material is low, good product quality.
In order to achieve the above object, the present invention is realized using following technical scheme：
A kind of burnt method of batch coking production negative pole, comprises the following steps：
1) coal measures that will be gone after the removal of impurity refines mix asphalt loading preheater, extremely has good flowing with heating medium for heating
Property, it is delivered in coking reactor and is heated by asphalt delivery pump, coal measures refines mix asphalt and successively completed in coking reactor
Polymerisation and pyrogenetic reaction；Volatile matter caused by polymerization and pyrogenetic reaction process is after the condensation cooling of coking oil condensate cooler
Into coking oil groove；
2) coke that polymerization and pyrogenetic reaction generate after terminating in coking reactor, stripping purification is carried out with water vapour, is steamed
Vapour together enters oil and gas mixture condensate cooler with the oil and gas mixture being stripped off, and devil liquor recovery is entered after condensed cooling
Groove；After stripping purification terminates, cold Jiao is carried out with water, hydraulic decoking is carried out with portable waterpower coke cutting machine；
3) coke removed through hydraulic coke-cutting falls into wet burnt conveyer and is delivered to wet coke bin, is stored up in wet coke bin
Deposit and preliminary hydro-extraction, the coke through preliminary hydro-extraction are dried into drying machine, the negative pole obtained after drying is burnt to enter finished product Jiao
Storehouse, transported outward by the entrucking of finished product Jiao's conveyer.
The softening point that the coal measures refines mix asphalt is 70~150 DEG C, and coking value 30%~50%, quinoline insolubles contains
Measure ＜ 0.1%.
It is that high temperature coal-tar pitch is mixed and passed through in proportion with middle coalite tar pitch that the coal measures, which refines mix asphalt,
The product crossed after purified treatment, the weight of wherein high temperature coal-tar pitch account for coal measures refine mix asphalt gross weight 10%~
90%.
The heating agent that the preheater uses refines mix asphalt for conduction oil or fused salt, by coal measures and is heated to 200~380
℃。
The temperature during polymerisation is 420~460 DEG C, 0.6~1.0MPa of polymerization pressure, and polymerization time is 4~6 small
When；Mechanical agitation is carried out to material in polymerization process, mixing speed is 200~300r/min.
The temperature during pyrogenetic reaction is 480~800 DEG C, 0~0.6MPa of coking pressure, scorch time 6~12 hours.
The stripping purification process time is 1~2 hour.
The hydraulic pressure of the portable waterpower coke cutting machine is 30~80MPa；Drying machine uses rotary dryer, drying temperature
150~300 DEG C, the burnt moisture of finished product negative pole is 1%~3%.
A kind of system for being used to realize that the batch coking production negative pole of claim 1 methods described is burnt, it is characterised in that
Including preheater, coking reactor, wet burnt conveyer, wet coke bin, drying machine and the finished product coke bin being sequentially connected, in addition to coking
Oily condensate cooler, coking oil groove, oil and gas mixture condensate cooler and devil liquor recovery groove；Raw material is set at the top of the preheater
Pitch entrance, bottom set the pitch entrance that asphalt outlet connects coking reactor by asphalt delivery pipeline, asphalt delivery pipeline
On set asphalt delivery pump；Coking reactor is furnished with portable waterpower coke cutting machine；The top of coking reactor set steam entry and
Coke cooling water entrance, bottom set coke outlet, set wet burnt conveyer below coke outlet, the delivery end of wet burnt conveyer is located at wet coke bin top
The wet burnt entrance top in portion, the wet burnt entrance of the wet burnt outlet connection drying machine of wet coke bin bottom, the dry burnt outlet of drying machine connects
Product coke bin is connected into, the burnt outlet lower section of finished product of finished product coke bin bottom is set as product Jiao's conveyer；Jiao at the top of the coking reactor
Carburetion outlet connects the coking oil-in of coking oil condensate cooler, the condensation of coking oil condensate cooler by coking oil-piping
Liquid outlet connection coking oil groove；Oil and gas mixture outlet at the top of coking reactor connects oil and gas by oil and gas mixture conduit and mixed
Compound condensate cooler, the condensate outlet connection devil liquor recovery groove of oil and gas mixture condensate cooler.
The coking reactor is vertical response kettle, inside sets electric heater.
Compared with prior art, the beneficial effects of the invention are as follows：
1) use high temperature coal-tar pitch and middle coalite tar pitch to produce negative pole Jiao for raw material, open high temperature coal tar
The new way of oil asphalt and middle coalite tar pitch processing and utilization；
2) polymerization and pyrogenetic reaction that coal measures refines mix asphalt are successively completed in coking reactor, utilizes reaction temperature
The burnt tap density of the parameter adjustment such as degree, reaction time, reaction pressure, coking temperature, coking pressure negative pole, specific surface area, wave
The indexs such as part are sent out, effectively improve the burnt product quality of negative pole；
3) coal measures refines mix asphalt and enters coking reactor after first preheated device is preheated by heating agent, in coking reactor
Polymerization, pyrogenetic reaction are completed using electrical heating, its is easy to operate, good energy-conserving effect；
4) coking reactor is equipped with stripping purifier and portable waterpower coke cutting machine, coke cleaning efficiency high, is advantageous to improve
Coke quality；
5) integrated artistic is simple, and cost of material is low, small investment, and floor space is small.
Brief description of the drawings
Fig. 1 is a kind of process chart of the burnt method of batch coking production negative pole of the present invention.
In figure：1. 2. asphalt delivery pump of preheater, 3. coking reactor, the 4. wet burnt wet drying machine 7. of coke bin 6. of conveyer 5. into
The oil and gas mixture condensate cooler 12. of 8. finished product Jiao conveyer of product coke bin, 9. 10. coking oil groove of coking oil condensate cooler 11. is useless
Liquid accumulator tank
Embodiment
The embodiment of the present invention is described further below in conjunction with the accompanying drawings：
As shown in figure 1, the method that a kind of batch coking production negative pole of the present invention is burnt, comprises the following steps：
1) coal measures that will be gone after the removal of impurity refines mix asphalt loading preheater 1, extremely has good stream with heating medium for heating
Dynamic property, is delivered in coking reactor 3 by asphalt delivery pump 2 and heated, and it is interior successively in coking reactor 3 that coal measures refines mix asphalt
Complete polymerisation and pyrogenetic reaction；Volatile matter caused by polymerization and pyrogenetic reaction process condenses through coking oil condensate cooler 9
Enter coking oil groove 10 after cooling；
2) coke that polymerization and pyrogenetic reaction generate after terminating in coking reactor 3, stripping purification is carried out with water vapour, is steamed
Vapour together enters oil and gas mixture condensate cooler 11 with the oil and gas mixture being stripped off, and devil liquor recovery is entered after condensed cooling
Groove 12；After stripping purification terminates, cold Jiao is carried out with water, hydraulic decoking is carried out with portable waterpower coke cutting machine；
3) coke removed through hydraulic coke-cutting falls into wet burnt conveyer 4 and is delivered to wet coke bin 5, enters in wet coke bin 5
Row storage and preliminary hydro-extraction, the coke through preliminary hydro-extraction are dried into drying machine 6, after drying obtained negative pole it is burnt into
Product coke bin 7, transported outward by the entrucking of finished product Jiao conveyer 8.
The softening point that the coal measures refines mix asphalt is 70~150 DEG C, and coking value 30%~50%, quinoline insolubles contains
Measure ＜ 0.1%.
It is that high temperature coal-tar pitch is mixed and passed through in proportion with middle coalite tar pitch that the coal measures, which refines mix asphalt,
The product crossed after purified treatment, the weight of wherein high temperature coal-tar pitch account for coal measures refine mix asphalt gross weight 10%~
90%.
The heating agent that the preheater 1 uses refines mix asphalt for conduction oil or fused salt, by coal measures and is heated to 200~380
℃。
The temperature during polymerisation is 420~460 DEG C, 0.6~1.0MPa of polymerization pressure, and polymerization time is 4~6 small
When；Mechanical agitation is carried out to material in polymerization process, mixing speed is 200~300r/min.
The temperature during pyrogenetic reaction is 480~800 DEG C, 0~0.6MPa of coking pressure, scorch time 6~12 hours.
The stripping purification process time is 1~2 hour.
The hydraulic pressure of the portable waterpower coke cutting machine is 30~80MPa；Drying machine 6 uses rotary dryer, dries temperature
150~300 DEG C of degree, the burnt moisture of finished product negative pole are 1%~3%.
A kind of system for being used to realize that the batch coking production negative pole of claim 1 methods described is burnt, it is characterised in that
Including the preheater 1, coking reactor 3, wet burnt conveyer 4, wet coke bin 5, drying machine 6 and finished product coke bin 7 being sequentially connected, also wrap
Include coking oil condensate cooler 9, coking oil groove 10, oil and gas mixture condensate cooler 11 and devil liquor recovery groove 12；The preheating
The top of device 1 sets material asphalt entrance, and bottom sets asphalt outlet and entered by the pitch of asphalt delivery pipeline connection coking reactor 3
Mouthful, set asphalt delivery pump 2 on asphalt delivery pipeline；Coking reactor 3 is furnished with portable waterpower coke cutting machine；Coking reactor 3
Top sets steam entry and coke cooling water entrance, and bottom sets coke outlet, wet burnt conveyer 4, wet burnt conveyer 4 are set below coke outlet
Delivery end positioned at the wet burnt entrance top at the top of wet coke bin 5, wet Jiao of the wet burnt outlet connection drying machine 6 of the wet bottom of coke bin 5
Entrance, the dry burnt outlet connection finished product coke bin 7 of drying machine 6, the burnt outlet lower section of finished product of the bottom of finished product coke bin 7 is set as the burnt conveying of product
Machine 8；The coking oil export at the top of coking reactor 3 connects the coking of coking oil condensate cooler 9 by coking oil-piping
Oil-in, the condensate outlet connection coking oil groove 10 of coking oil condensate cooler 9；The oil and gas mixing at the top of coking reactor 3
Thing outlet connects oil and gas mixture condensate cooler 11 by oil and gas mixture conduit, oil and gas mixture condensate cooler 11 it is cold
Condensate outlet connection devil liquor recovery groove 12.
The coking reactor 3 is vertical response kettle, inside sets electric heater.
Following examples are implemented under premised on technical solution of the present invention, give detailed embodiment and tool
The operating process of body, but protection scope of the present invention is not limited to following embodiments.Method therefor is such as without spy in following embodiments
It is conventional method not mentionlet alone bright.
【Embodiment】
In the present embodiment, the burnt production process of negative pole is as follows：
1) prepared by raw material；High temperature coal-tar pitch is mixed in proportion with middle coalite tar pitch, after purified processing
Obtain coal measures and refine mix asphalt, the weight of wherein high temperature coal-tar pitch accounts for coal measures refines mix asphalt gross weight 60%.
The softening point that coal measures refines mix asphalt is 110 DEG C, coking value 35%, quinoline insolubles (QI) ＜ 0.1% (mass percent).
2) raw material preheating；Coal measures is refined into mix asphalt and loads preheater 1, volume filling rate is 85%, uses heating medium for heating
To 300 DEG C.
3) polymerization and coking；Coal measures is refined into mix asphalt by asphalt delivery pump 2 to be delivered in coking reactor 3, held
Product filling rate is 90%.Heated in coking reactor 3 using electric heater, coal measures refines mix asphalt in pyrogenetic reaction
Polymerization and pyrogenetic reaction are successively completed in device 3.Wherein：
Mechanical agitation, mixing speed 250r/min, control are carried out to material with mechanical agitator in polymerization process
420 DEG C of polymerization temperature, polymerization pressure 0.8MPa, polymerization time are 4 hours；
600 DEG C of pyrogenetic reaction controlling reaction temperature, coking pressure 0.3MPa, scorch time 8 hours；
Volatile matter caused by polymerization and coking enters coking oil groove after the condensation cooling of coking oil condensate cooler 9
10；
4) purification decoking；After coking terminates, water vapour is passed through coking reactor 3, stripping purification steam consumption is 600 public
Jin/ton is burnt；Stripping purification 1.5 hours, steam and the gas mixture being stripped off enter oil and gas mixture condensate cooler 11, cold
Enter devil liquor recovery groove 12 after solidifying cooling.
After stripping purification terminates, water is passed through in coking reactor 3 and carries out cold Jiao, enters water-filling with portable waterpower coke cutting machine
Power devokes；During decoking, by the water under high pressure of high-pressure hydraulic pump conveying, by rotary hose, the nozzle of drilling rod to hydraulic coke-cutting machine, from waterpower
The water under high pressure that the nozzle of coke cutting machine sprays forms high-pressure water jet, is cut petroleum coke using the strong impact power of high-pressure water jet
Get off, constantly lift and rotate by drilling rod, untill the coke in coking reactor is all cleared.
5) dry；The coke removed through hydraulic coke-cutting falls into wet burnt transporter 4 and is delivered to wet coke bin 5, in wet Jiao
Storehouse 5 is stored and preliminary hydro-extraction, and the coke through preliminary hydro-extraction is dried into rotary dryer, 300 DEG C of drying temperature；
Dried negative pole Jiao moisture content of finished products is 1.5%, is sent into finished product coke bin 7, and transported outward by the entrucking of finished product Jiao conveyer 8.
The foregoing is only a preferred embodiment of the present invention, but protection scope of the present invention be not limited thereto,
Any one skilled in the art the invention discloses technical scope in, technique according to the invention scheme and its
Inventive concept is subject to equivalent substitution or change, should all be included within the scope of the present invention.
Claims (10)
1. a kind of burnt method of batch coking production negative pole, it is characterised in that comprise the following steps：
1) coal measures that will be gone after the removal of impurity refines mix asphalt loading preheater, extremely has good mobility with heating medium for heating,
It is delivered in coking reactor and is heated by asphalt delivery pump, coal measures refines mix asphalt and polymerization is successively completed in coking reactor
Reaction and pyrogenetic reaction；Volatile matter caused by polymerization and pyrogenetic reaction process enters after the condensation cooling of coking oil condensate cooler
Coking oil groove；
2) coke that polymerization and pyrogenetic reaction generate after terminating in coking reactor, stripping purification is carried out with water vapour, steam with
The oil and gas mixture being stripped off together enters oil and gas mixture condensate cooler, and devil liquor recovery groove is entered after condensed cooling；Vapour
After defecation terminates, cold Jiao is carried out with water, hydraulic decoking is carried out with portable waterpower coke cutting machine；
3) coke removed through hydraulic coke-cutting falls into wet burnt conveyer and is delivered to wet coke bin, wet coke bin carry out storage and
Preliminary hydro-extraction, the coke through preliminary hydro-extraction are dried into drying machine, and the negative pole obtained after drying is burnt to enter finished product coke bin, by
The entrucking of finished product Jiao's conveyer is transported outward.
A kind of 2. burnt method of batch coking production negative pole according to claim 1, it is characterised in that the coal measures essence
The softening point of mix asphalt processed is 70~150 DEG C, coking value 30%~50%, quinoline insolubles content ＜ 0.1%.
A kind of 3. burnt method of batch coking production negative pole according to claim 1, it is characterised in that the coal measures essence
Mix asphalt processed is that high temperature coal-tar pitch mixes and the product after purified treatment in proportion with middle coalite tar pitch,
The weight of wherein high temperature coal-tar pitch accounts for 10%~90% that coal measures refines mix asphalt gross weight.
A kind of 4. burnt method of batch coking production negative pole according to claim 1, it is characterised in that the preheater
The heating agent used refines mix asphalt for conduction oil or fused salt, by coal measures and is heated to 200~380 DEG C.
5. the burnt method of a kind of batch coking production negative pole according to claim 1, it is characterised in that the polymerization is anti-
Seasonable temperature is 420~460 DEG C, 0.6~1.0MPa of polymerization pressure, and polymerization time is 4~6 hours；In polymerization process
Mechanical agitation is carried out to material, mixing speed is 200~300r/min.
6. the burnt method of a kind of batch coking production negative pole according to claim 1, it is characterised in that the coking is anti-
Seasonable temperature is 480~800 DEG C, 0~0.6MPa of coking pressure, scorch time 6~12 hours.
7. the burnt method of a kind of batch coking production negative pole according to claim 1, it is characterised in that the stripping is net
It is 1~2 hour to change process time.
A kind of 8. burnt method of batch coking production negative pole according to claim 1, it is characterised in that the movable type
The hydraulic pressure of hydraulic coke-cutting machine is 30~80MPa；Drying machine uses rotary dryer, and 150~300 DEG C of drying temperature, finished product is born
Extremely burnt moisture is 1%~3%.
A kind of 9. system for being used to realize that the batch coking production negative pole of claim 1 methods described is burnt, it is characterised in that bag
Include the preheater being sequentially connected, coking reactor, wet burnt conveyer, wet coke bin, drying machine and finished product coke bin, in addition to coking oil
Condensate cooler, coking oil groove, oil and gas mixture condensate cooler and devil liquor recovery groove；Raw material drip is set at the top of the preheater
Blue or green entrance, bottom sets the pitch entrance that asphalt outlet connects coking reactor by asphalt delivery pipeline, on asphalt delivery pipeline
If asphalt delivery pump；Coking reactor is furnished with portable waterpower coke cutting machine；The top of coking reactor sets steam entry and cold
Burnt water inlet, bottom set coke outlet, and wet burnt conveyer is set below coke outlet, and the delivery end of wet burnt conveyer is located at the top of wet coke bin
Wet burnt entrance top, the wet burnt entrance of the wet burnt outlet connection drying machine of wet coke bin bottom, the dry burnt outlet connection of drying machine
Finished product coke bin, the burnt outlet lower section of finished product of finished product coke bin bottom are set as product Jiao's conveyer；Coking at the top of the coking reactor
Oil export connects the coking oil-in of coking oil condensate cooler, the condensate liquid of coking oil condensate cooler by coking oil-piping
Outlet connection coking oil groove；Oil and gas mixture outlet at the top of coking reactor connects oil and gas by oil and gas mixture conduit and mixed
Thing condensate cooler, the condensate outlet connection devil liquor recovery groove of oil and gas mixture condensate cooler.
A kind of 10. burnt system of batch coking production negative pole according to claim 9, it is characterised in that the coking
Reactor is vertical response kettle, inside sets electric heater.
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| CN110734779A (en) * | 2019-10-15 | 2020-01-31 | 湖南中科星城石墨有限公司 | isotropic cokes suitable for lithium ion battery cathode raw materials and preparation method thereof |
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