CN115433601A - Co-production process and device for preparing multipurpose high-performance needle coke - Google Patents
Co-production process and device for preparing multipurpose high-performance needle coke Download PDFInfo
- Publication number
- CN115433601A CN115433601A CN202211055632.9A CN202211055632A CN115433601A CN 115433601 A CN115433601 A CN 115433601A CN 202211055632 A CN202211055632 A CN 202211055632A CN 115433601 A CN115433601 A CN 115433601A
- Authority
- CN
- China
- Prior art keywords
- tank
- asphalt
- needle coke
- raw material
- coking
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000011331 needle coke Substances 0.000 title claims abstract description 71
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 42
- 239000010426 asphalt Substances 0.000 claims abstract description 97
- 238000004939 coking Methods 0.000 claims abstract description 65
- 239000002994 raw material Substances 0.000 claims abstract description 65
- 239000007788 liquid Substances 0.000 claims abstract description 51
- 238000001354 calcination Methods 0.000 claims abstract description 28
- 239000012046 mixed solvent Substances 0.000 claims abstract description 24
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000000034 method Methods 0.000 claims abstract description 19
- 238000002156 mixing Methods 0.000 claims abstract description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000010439 graphite Substances 0.000 claims abstract description 13
- 229910002804 graphite Inorganic materials 0.000 claims abstract description 13
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 claims abstract description 7
- 229910001416 lithium ion Inorganic materials 0.000 claims abstract description 7
- 239000010406 cathode material Substances 0.000 claims abstract description 5
- 238000005189 flocculation Methods 0.000 claims description 61
- 230000016615 flocculation Effects 0.000 claims description 59
- 239000000571 coke Substances 0.000 claims description 33
- 230000003111 delayed effect Effects 0.000 claims description 27
- 230000003068 static effect Effects 0.000 claims description 23
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 18
- 238000004821 distillation Methods 0.000 claims description 16
- 239000007789 gas Substances 0.000 claims description 16
- 239000000047 product Substances 0.000 claims description 15
- 239000003638 chemical reducing agent Substances 0.000 claims description 14
- 238000006243 chemical reaction Methods 0.000 claims description 13
- 238000004062 sedimentation Methods 0.000 claims description 13
- 239000008394 flocculating agent Substances 0.000 claims description 11
- 239000002904 solvent Substances 0.000 claims description 11
- 239000006227 byproduct Substances 0.000 claims description 10
- 239000011300 coal pitch Substances 0.000 claims description 9
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 8
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 5
- 238000000462 isostatic pressing Methods 0.000 claims description 5
- 238000009628 steelmaking Methods 0.000 claims description 5
- 229910052786 argon Inorganic materials 0.000 claims description 4
- 150000004945 aromatic hydrocarbons Chemical group 0.000 claims description 4
- 239000001307 helium Substances 0.000 claims description 4
- 229910052734 helium Inorganic materials 0.000 claims description 4
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 3
- 239000002283 diesel fuel Substances 0.000 claims description 3
- 239000003502 gasoline Substances 0.000 claims description 3
- 239000003350 kerosene Substances 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 239000001993 wax Substances 0.000 claims description 3
- 230000003311 flocculating effect Effects 0.000 claims description 2
- 239000000126 substance Substances 0.000 abstract description 4
- 239000003245 coal Substances 0.000 abstract description 2
- 238000000151 deposition Methods 0.000 abstract 1
- 239000011295 pitch Substances 0.000 description 9
- 239000000428 dust Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- 238000005119 centrifugation Methods 0.000 description 6
- 230000009286 beneficial effect Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000005086 pumping Methods 0.000 description 4
- 239000011311 coal-based needle coke Substances 0.000 description 3
- 238000005235 decoking Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000002010 green coke Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000004806 packaging method and process Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 1
- 229910052796 boron Inorganic materials 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000007770 graphite material Substances 0.000 description 1
- 125000005842 heteroatom Chemical group 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000007773 negative electrode material Substances 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 238000012643 polycondensation polymerization Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
Images
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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Coke Industry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
A process for preparing multi-purpose high-performance needle coke includes such steps as mixing coal asphalt with mixed solvent, depositing, collecting all the liquid or upper and lower liquid, coking and calcining to obtain needle coke products of 3 specifications. In the invention, only quinoline insoluble substances which affect the performance of the needle coke are removed in the centrifugal process, and all effective components in the asphalt are remained in the raw material asphalt, so that the yield of refined asphalt can be improved, and the production cost can be greatly reduced. The invention realizes the production of needle coke with three specifications by a whole set of production process, greatly improves the production efficiency and reduces the time and space cost. The invention can effectively and stably produce needle coke products with 3 specifications. Are respectively used in the fields of high-end graphite, high-temperature graphite electrodes and lithium ion battery cathode materials. The invention realizes the full coverage of the production lines of needle coke with different specifications.
Description
Technical Field
The invention belongs to the technical field of coal-based needle coke preparation, and particularly relates to a co-production process and a co-production device for preparing multi-purpose high-performance needle coke.
Background
The needle coke is a high-quality carbon material, has the advantages of low Coefficient of Thermal Expansion (CTE), good electric conductivity, heat conductivity and the like, and is mainly used for producing high-power (HP) or ultra-high power (UHP) graphite electrodes for electric furnace steelmaking, lithium ion battery cathode materials, high-end graphite materials and other fields.
Coal pitch is a raw material for producing coal-based needle coke, is a co-dissolved mixture of various organic compounds, has extremely complex composition and structure, has composition related to the properties of raw coal used for coking, a coking process and coal tar processing conditions, has different composition properties of coal pitch from different sources, and can be used for producing needle coke only through specific pretreatment. The raw material of the needle coke needs the requirements of high aromatic hydrocarbon content, low heteroatom content, low metal content, low ash content and the like, the pretreatment of the raw material is the core technology of coal-based needle coke industrialization, the continuous innovation is the key for improving the quality of needle coke products and reducing the production cost, the pretreatment effect is ensured, the yield of the treated asphalt is improved, and the influence of the raw material source is eliminated. The main purpose of raw material pretreatment is to remove harmful impurities such as Quinoline Insoluble (QI) in raw material asphalt and keep beneficial components in the asphalt to prepare refined asphalt with proper composition. The needle coke pretreatment technology at home and abroad mainly comprises a distillation method, a centrifugal method, a flash condensation polymerization method and a solvent method, while the production method for really realizing industrialization in the production of needle coke at home is the solvent method, but with the development of graphite electrodes and lithium ion battery technologies, higher requirements are put on the performance and cost of the needle coke, the needle coke is required to have more stable performance and lower production cost, and the needle coke prepared by the existing solvent method is mature but greatly influenced by the change of coal pitch raw material sources. And because the purposes of the needle coke are different, the parameters of the required needle coke are different, and the requirement of multiple purposes cannot be met by maintaining one parameter to produce the needle coke, so that the development of a new needle coke raw material pretreatment technology and the production of a multi-purpose needle coke product have important significance.
Disclosure of Invention
The invention provides a co-production process and a co-production device for preparing multi-purpose high-performance needle coke, and the used co-production process method can effectively and stably produce needle coke products with 3 specifications.
In order to achieve the purpose, the invention adopts the following technical scheme:
a coproduction process for preparing multi-purpose high-performance needle coke takes coal pitch as a raw material, the coal pitch and a mixed solvent are mixed and settled, all settled liquid is taken, or upper-layer liquid and lower-layer liquid are respectively taken as raw materials, and after coking and calcination, needle coke products with 3 specifications can be produced, and the coproduction process specifically comprises the following steps:
1) Statically mixing raw material asphalt with a viscosity reducer and a flocculating agent, then entering a flocculation tank for flocculation and sedimentation, then entering centrifugal equipment for centrifugal operation, sending a centrifuged light phase into a flash tower for distillation operation, condensing evaporated gas, then entering a distilled light phase tank, and entering residual liquid into a coking raw material tank as a pre-coking raw material, wherein the raw material asphalt is named as asphalt A and is used for preparing isostatic pressing graphite;
2) Statically mixing raw material asphalt with a viscosity reducer and a flocculating agent, then entering a flocculation tank for flocculation and sedimentation, pumping out upper-layer liquid of the flocculation and sedimentation tank, sending the upper-layer liquid into a flash tower for distillation operation, condensing evaporated gas, then entering a distillation light phase tank, and entering residual liquid into a coking raw material tank to be used as a raw material before coking, wherein the raw material asphalt is named as asphalt B and is used for preparing graphite electrodes for steelmaking;
3) Pumping out the lower layer liquid of the flocculation tank in the step 2), then statically mixing the lower layer liquid with a mixed solvent of a viscosity reducer and a flocculating agent again, then performing flocculation sedimentation again, performing centrifugal operation on the settled mixed liquid, then sending the centrifuged light phase into a flash tower for distillation operation, condensing the evaporated gas, then entering a distillation light phase tank, and enabling the residual liquid to enter a coking raw material tank as a raw material before coking, wherein the raw material asphalt is named as asphalt C and is used for preparing a lithium ion battery cathode material
4) The coking reaction process comprises the following steps: respectively feeding the asphalt A, the asphalt B and the asphalt C into a heating furnace for preheating, then feeding the asphalt A, the asphalt B and the asphalt C into a coking tower for delayed coking, feeding light component steam into a light component condenser, condensing the light component steam, then feeding the condensed light component steam into a light component oil storage tank, and packaging and selling the light component oil;
5) Product and subsequent treatment: after the coking reaction is completed, cutting coke by using water vapor, then sending the coke into a product dryer through a conveyor belt, sending the dried coke into a calcining furnace, sending the prepared gas into a tail gas treatment device, sending the obtained coke into a dust removal blower for dust removal treatment, and packaging and selling the three types of the coke after dust removal.
The static mixing lasts for 1-2 hours, and the flocculation settling time lasts for 3-5 hours.
The flocculant is a saturated alkane solvent and is one or more of gasoline, diesel oil, kerosene and wax oil; the viscosity reducer is an aromatic hydrocarbon solvent and is one or more of anthracene oil, wash oil, toluene and quinoline.
The by-products centrifugally separated in the step 1) or the step 3) comprise toluene and quinoline insoluble substances.
The mass ratio of the flocculating agent to the viscosity reducer is 1-3.
The pumping amount of the upper layer liquid is 50 to 80 percent of the mass of the whole mixed liquid in the flocculation tank.
The temperature of the flash tower is 200-300 ℃.
The temperature of the heating furnace is 300-500 ℃, the coking final temperature of the coking tower is 450-500 ℃, and the reaction pressure is 0-5 MPa.
The drying time of the step 5) is 3 to 5 hours; the reaction temperature of the calcining furnace is 800-1500 ℃, and the gas in the calcining furnace is one of nitrogen, argon and helium.
In the coke preparation process, three needle coke products with different purposes are obtained by controlling the conditions of raw material pretreatment flocculation centrifugation and thermal reaction pressure and temperature.
A device used in a co-production process for preparing multi-purpose high-performance needle coke comprises a mixed solvent tank, a raw material asphalt tank, a static mixer I, a flocculation tank I, a centrifugal device I, a static mixer II, a flocculation tank II, a centrifugal device II, a light phase tank A, a light phase tank B, a light phase tank C, a flash tower I, a flash tower II, a refined asphalt tank A, a refined asphalt tank B, a refined asphalt tank C, a pre-heating furnace, a delayed coking tower, a coke dryer and a calcining furnace, wherein one outlet of the mixed solvent tank and the outlet of the raw material asphalt tank are respectively connected with the inlet of the static mixer I, the outlet of the static mixer I is connected with the flocculation tank I, the outlet at the bottom of the flocculation tank I is divided into two paths, one path is connected with the centrifugal device I, the other path is connected with the static mixer II, the other outlet of the mixed solvent tank is also connected with the static mixer II, the centrifugal device I is connected with the light phase tank A, the upper outlet of the flocculation tank I is connected with the light phase tank B, the outlet of the flocculation tank II is connected with the flocculation tank II, and the centrifugal device II is connected with the centrifugal tank II; the light phase tank A and the light phase tank B are respectively connected with a flash tower I, the light phase tank C is connected with a flash tower II, the outlet of the flash tower I is respectively connected with a refined asphalt tank A and a refined asphalt tank B, and the outlet of the flash tower II is connected with a refined asphalt tank C; the refined asphalt tank A, the refined asphalt tank B and the refined asphalt tank C are respectively connected with a preheating furnace, the preheating furnace is connected with a delayed coking tower, the delayed coking tower is connected with a coke dryer, and the coke dryer is connected with a calcining furnace.
Compared with the prior art, the invention has the beneficial effects that:
1) In the existing solvent method pretreatment process, part of components which are beneficial to the growth of the intermediate phase and generated by the needle coke are separated along with impurity components, so that the loss of beneficial components is caused, namely, the components suitable for the generation of the needle coke in the raw materials are not fully utilized, and the production economic benefit needs to be further improved. In the invention, only quinoline insoluble substances influencing the performance of the needle coke are removed in the centrifugal process, and all effective components in the asphalt are remained in the raw material asphalt, so that the yield of refined asphalt can be improved, and the production cost is greatly reduced.
2) The existing needle coke production device can only produce a needle coke product with one purpose, if the final product is changed, the production parameters need to be frequently adjusted, and the change of the types of raw materials can consume a large amount of manpower and material resources, so that the production efficiency is greatly reduced. The invention realizes the production of needle coke with three specifications by a whole set of production process, greatly improves the production efficiency and reduces the time and space cost.
3) The invention can produce coke with three specifications, namely needle coke A: the method is used in the field of isostatic pressing graphite, the needle coke B is used in the field of high-temperature graphite electrodes for steelmaking, and the needle coke C is applied in the field of lithium ion battery cathode materials. The invention realizes the full coverage of production lines of needle coke with different specifications.
Drawings
Figure 1 is a process scheme of the present invention.
In FIG. 1: 1-mixed solvent tank, 2-raw material asphalt tank, 3-static mixer I, 4-flocculation tank I, 5-centrifugal device I, 6-static mixer II, 7-flocculation tank II, 8-centrifugal device II, 9-light phase tank A, 10-light phase tank B, 11-light phase tank C, 12-flash tower I, 13-flash tower II, 14-refined asphalt tank A, 15-refined asphalt tank B, 16-refined asphalt tank C, 17-distillation light phase tank, 18-preheating furnace I, 19-preheating furnace II, 20-delayed coking tower I, 21-delayed coking tower II, 22-coke dryer A, 23-coke dryer B, 24-coke dryer C, 25-light oil storage tank I, 26-light oil storage tank II, 27-light oil blower, 28-dust removal furnace I, 29-tail gas processing device.
Detailed Description
The following examples are included to further illustrate embodiments of the invention:
as shown in figure 1, the co-production process can effectively and stably produce needle coke products with 3 specifications, and the first needle coke in the method takes coal pitch as a raw material, the coal pitch is uniformly mixed with a viscosity reducer and a flocculating agent, and is subjected to flocculation and then centrifugation treatment to obtain refined pitch with low quinoline insoluble substances, and the refined pitch is coked and calcined to obtain the needle coke which is isostatic pressing graphite raw material coke; the second is carried out by taking the first flocculation sedimentation upper layer liquid as a raw material to obtain graphite electrode raw material coke for steelmaking; and thirdly, mixing the flocculated and settled lower-layer liquid of the first raw material with a viscosity reducer and a flocculating agent again, and performing flocculation and centrifugation treatment to obtain the raw material coke of the lithium ion negative electrode material. The invention realizes the full coverage of the production lines of needle coke with different specifications.
A device used in a co-production process for preparing multi-purpose high-performance needle coke comprises a mixed solvent tank 1, a raw material pitch tank 2, a static mixer I3, a flocculation tank I4, a centrifugal device I5, a static mixer II 6, a flocculation tank II 7, a centrifugal device II 8, a light phase tank A9, a light phase tank B10, a light phase tank C11, a flash tower I13, a flash tower II 12, a refined pitch tank A14, a refined pitch tank B15, a refined pitch tank C16, a preheating furnace, a delayed coking tower, a coke dryer and a calcining furnace 27, wherein one outlet of the mixed solvent tank 1 and the outlet of the raw material pitch tank 2 are respectively connected with an inlet of the static mixer I3, an outlet of the static mixer I3 is connected with the other flocculation tank I4, an outlet at the bottom of the flocculation tank I4 is connected with the centrifugal device I5, one way is connected with the static mixer II 6, the other outlet of the mixed solvent tank 1 is also connected with the static mixer 6, the centrifugal device 5 is connected with the light phase A9, an outlet of the light phase tank I4 is connected with the centrifugal tank II 6, an outlet of the light phase tank II 10 is connected with the flocculation tank II 6, and a flocculation tank II 7 is connected with the centrifugal device II 8, and a light phase tank II 8; the light phase tank A9 and the light phase tank B10 are respectively connected with a flash tower I13, the light phase tank C11 is connected with a flash tower II 12, the outlet of the flash tower I13 is respectively connected with a refined asphalt tank A14 and a refined asphalt tank B15, and the outlet of the flash tower II 12 is connected with a refined asphalt tank C16; the refined asphalt tank A, the refined asphalt tank B and the refined asphalt tank C are respectively connected with a preheating furnace, the preheating furnace is connected with a delayed coking tower, the delayed coking tower is connected with a coke dryer, and the coke dryer is connected with a calcining furnace. The asphalt A and the asphalt B jointly use a flash tower I and a delayed coking tower I, and the asphalt C uses a flash tower II and a delayed coking tower II.
The specific process steps of the invention are as follows:
performing flocculation sedimentation on the coal-series asphalt and a mixed solvent in a flocculation tank I4, wherein the upper layer part is a raw material of refined asphalt B, the lower layer part is a raw material of refined asphalt C, and the whole is used as a raw material of refined asphalt A;
all the liquid after flocculation and sedimentation enters centrifugal equipment I5 for centrifugal treatment, the obtained by-product is sold, and the rest part enters a light phase tank A9;
statically mixing the lower layer liquid of the flocculation sedimentation with a mixed solvent, and finally entering a flocculation tank II 7 for flocculation sedimentation;
after flocculation is carried out in the flocculation tank II 7, all liquid enters centrifugal equipment II 8 for centrifugal treatment, the byproducts and the byproducts in the centrifugal equipment I5 are packed and sold together, and the rest liquid enters a light phase tank C11;
the upper layer liquid in the flocculation tank I4 directly enters a light phase tank B10;
the liquid in the light phase tank A9 enters a flash tower I13 for flash evaporation, the light components enter a distillation light phase tank 17, and the residual asphalt enters a refined asphalt tank A14; the light phase tank B10 and the light phase tank A9 share a flash tower I13;
the light phase tank C11 enters a flash tower II 12 for flash evaporation, the light components enter a distillation light phase tank 17, and the residual asphalt enters a refined asphalt tank C16;
the refined asphalt A enters a heating furnace I18 for preheating, and then enters a delayed coking tower I20 for delayed coking, and the refined asphalt B and the refined asphalt A share the delayed coking tower I20;
the refined asphalt C enters a heating furnace II 19 for preheating, and then enters a coking tower II 21 for delayed coking;
after coking is finished, decoking treatment is carried out, and then drying is carried out through a blast drier to finally obtain three kinds of needle coke green coke;
and respectively feeding the three types of cokes into a calcining device for calcining treatment, and finally obtaining needle coke calcined cokes with three specifications.
In the mixed solvent, the mass ratio of the flocculating agent to the viscosity reducer is 1-3.
The flocculating agent is a saturated alkane solvent and is one or more of gasoline, diesel oil, kerosene and wax oil.
The viscosity reducer is aromatic hydrocarbon solvent, and is one or more of anthracene oil, wash oil, toluene, and quinoline.
The static mixing time is 1-2 hours; the flocculation settling time is 3 to 5 hours.
The by-product of the centrifugation is toluene, quinoline insoluble or other elemental compounds.
The extracted upper layer liquid accounts for 50-80% of the total liquid.
The temperature of the flash tower I13 is 200-300 ℃.
The temperature of the flash tower II 12 is 200-300 ℃.
The temperature of the preheating furnace I18 is 300-500 ℃.
The coking final temperature of the delayed coking tower I20 is 450-500 ℃.
The reaction pressure in the delayed coking tower I20 is 0-5 MPa.
The temperature of the preheating furnace II 19 is 300-500 ℃.
The coking final temperature of the delayed coking tower II 21 is 450-500 ℃.
The reaction pressure in the delayed coking tower II 21 is 0-5 MPa.
The decoking method is water vapor decoking.
The drying time of the dryer is 3 to 5 hours.
The reaction temperature of the calcining furnace is between 800 and 1500 ℃.
The gas in the calcining furnace is one of nitrogen, argon and helium.
Example 1:
and (3) statically mixing the preheated and melted raw material asphalt with the mixed solvent for 1-2 hours, and then feeding the mixture into a flocculation tank I4. Flocculating for 3-5 hours in a flocculation tank I4, and then integrally pumping into a centrifugal device I5, wherein the part is raw material mixed liquid of needle coke A; and then statically mixing the preheated raw material asphalt with the mixed solvent for 1-2 hours, and then feeding the mixture into a flocculation tank I4. After flocculation is carried out for 3-5 hours in the flocculation tank I4, the upper layer is pumped into a light phase tank B10 which is the raw material mixed liquid of the needle coke B, and the lower layer and the solvent in the mixed solvent tank are pumped into a static device II 6 which is the raw material mixed liquid of the needle coke C.
After the raw material mixed liquid A enters a centrifugal device I5 for centrifugation, a byproduct is packaged and sold as a byproduct, and the rest liquid enters a light phase tank A9; the raw material mixed liquid C and the mixed solvent enter a static mixing device II 6 together to be mixed for 1-2 hours and then are pumped into a flocculation tank II 7, after flocculation and sedimentation are carried out in the flocculation tank II 7 for 3-5 hours, all the raw material mixed liquid C and the mixed solvent enter a centrifugal device II 8, byproducts after centrifugation are packed and sold as the byproducts in the centrifugal device I5, and the rest raw material mixed liquid C and the mixed solvent enter a light phase tank C11.
The liquids in the light phase tank A9 and the light phase tank B10 share one set of follow-up device, and the liquid in the light phase tank C11 uses one set of follow-up device separately. The liquid in the light phase tank A9 enters a flash tower I13, the light phase enters a distillation light phase tank 17, the rest part enters a refined asphalt tank A14, and the liquid in the light phase tank B10 finally enters a refined asphalt tank B15 in the same way; the liquid in the light phase tank C11 enters a flash tower II 12, the light phase enters a distillation light phase tank 17, and the rest enters a refined asphalt tank C16. To this end, all of the three needle coke refined pitch feedstocks are in their respective refined pitch tanks.
1. Preparing needle coke A: and (3) feeding the treated refined asphalt A into an asphalt preheater at 400 ℃, carrying out delayed coking under the conditions that the parameter of a delayed coking tower I20 is 2MPa and the coking final temperature is 480 ℃, feeding the obtained raw coke into a calcining furnace 27, and controlling the temperature of the calcining furnace 27 to be 1200 ℃, thus finally obtaining the calcined needle coke A.
2. Preparing needle coke B: and (3) feeding the treated refined asphalt B into an asphalt preheater at 400 ℃, carrying out delayed coking under the conditions that the parameter of a delayed coking tower I20 is 2MPa and the coking final temperature is 480 ℃, feeding the obtained raw coke into a calcining furnace 27, and finally obtaining calcined needle coke B, wherein the temperature of the calcining furnace is 1200 ℃.
3. Preparing needle coke C: and (3) feeding the treated refined asphalt C into an asphalt preheater at 400 ℃, performing delayed coking under the conditions that the parameters of a coking tower II 21 are 2MPa and the coking final temperature is 480 ℃, feeding the obtained green coke into a calcining furnace 27, and the temperature of the calcining furnace is 1200 ℃, thus finally obtaining the calcined needle coke C.
After the coking reaction is completed, the coke is cut by using water vapor and then is sent into a product dryer through a conveyor belt, and the dried coke enters a calcining furnace. The high-temperature calcining furnace carries out high-temperature calcining under the condition of one of protective gas of nitrogen, argon and helium, the generated gas enters a tail gas treatment device, the obtained coke enters a dust removal blower for dust removal treatment, and three needle coke products after dust removal can be packaged and sold.
The three cokes obtained in example 1 are shown in Table 1 for their performance in terms of their use:
table 1 example 1 three cokes perform in each field
The parameters of the needle coke A meet the requirements of isostatic pressing graphite on raw materials, namely, the thermal expansion coefficient, ash content and boron content are all lower than the parameters of normal needle coke.
The invention can prepare the needle coke with three specifications by the delayed coking device, can obtain a finished product with a certain yield value, and can adjust the yield value and the product performance by adjusting parameters such as temperature, pressure and the like.
The foregoing is merely exemplary of the present invention and is not intended to limit the invention in any way, which is equivalent to the above-described modifications or variations that may be made by persons skilled in the art using the teachings disclosed herein. However, any simple modification, equivalent change and modification made to the above embodiments according to the technical essence of the present invention still belong to the protection scope of the technical solution of the present invention.
Claims (10)
1. A coproduction process for preparing multi-purpose high-performance needle coke is characterized in that coal pitch is used as a raw material, the coal pitch and a mixed solvent are mixed and settled, all settled liquids are taken, or an upper layer liquid and a lower layer liquid are respectively taken as the raw materials, and then coking and calcining are carried out, so that needle coke products with 3 specifications can be produced, and the coproduction process specifically comprises the following steps:
1) Statically mixing raw material asphalt with a viscosity reducer and a flocculating agent, then entering a flocculation tank for flocculation and sedimentation, then entering centrifugal equipment for centrifugal operation, sending a centrifuged light phase into a flash tower for distillation operation, condensing evaporated gas, then entering a distilled light phase tank, and entering residual liquid into a coking raw material tank as a pre-coking raw material, wherein the raw material asphalt is named as asphalt A and is used for preparing isostatic pressing graphite;
2) Statically mixing raw material asphalt, a viscosity reducer and a flocculating agent, then entering a flocculation tank for flocculation and sedimentation, extracting upper liquid of the flocculation and sedimentation tank, sending the upper liquid into a flash tower for distillation operation, condensing evaporated gas, then entering a distillation light phase tank, and entering residual liquid into a coking raw material tank as a raw material before coking, wherein the raw material asphalt is named as asphalt B and is used for preparing graphite electrodes for steelmaking;
3) Extracting the lower layer liquid of the flocculation tank in the step 2), then statically mixing the lower layer liquid with a mixed solvent of a viscosity reducer and a flocculating agent again, then flocculating and settling again, carrying out centrifugal operation on the settled mixed liquid, then sending the centrifuged light phase into a flash tower for distillation operation, condensing the evaporated gas, then feeding the condensed gas into a distillation light phase tank, feeding the residual liquid into a coking raw material tank as a raw material before coking, and naming the raw material asphalt as asphalt C for preparing a lithium ion battery cathode material;
4) The coking reaction process comprises the following steps: respectively feeding the asphalt A, the asphalt B and the asphalt C into a heating furnace for preheating, then feeding the asphalt A, the asphalt B and the asphalt C into a coking tower for delayed coking, and feeding light component steam into a light component condenser;
5) Product and subsequent treatment: and after the coking reaction is completed, drying, and feeding the dried coke into a calcining furnace to prepare three kinds of coke.
2. The co-production process for preparing multi-purpose high-performance needle coke according to claim 1, wherein the static mixing is performed for 1-2 hours, and the flocculation settling time is 3-5 hours.
3. The co-production process for preparing the multipurpose high-performance needle coke according to claim 1, wherein the flocculant is a saturated alkane solvent which is one or more of gasoline, diesel oil, kerosene and wax oil; the viscosity reducer is an aromatic hydrocarbon solvent and is one or more of anthracene oil, wash oil, toluene and quinoline.
4. The co-production process for preparing multi-purpose high-performance needle coke according to claim 1, wherein the by-products centrifugally separated in the step 1) or 3) comprise toluene and quinoline insolubles.
5. The co-production process for preparing the multipurpose high-performance needle coke according to claim 1, wherein the mass ratio of the flocculant to the viscosity reducer is 1-3.
6. The co-production process for preparing multi-purpose high-performance needle coke as claimed in claim 1, wherein the amount of the upper liquid is extracted from the flocculation tank by 50-80% of the total mixed liquid mass.
7. The co-production process for preparing multi-purpose high-performance needle coke according to claim 1, wherein the temperature of the flash tower is 200-300 ℃.
8. The co-production process for preparing the multipurpose high-performance needle coke according to claim 1, wherein the temperature of the heating furnace is 300-500 ℃, the coking final temperature of the coking tower is 450-500 ℃, and the reaction pressure is 0-5 MPa.
9. The co-production process for preparing multipurpose high-performance needle coke according to claim 1, wherein the drying time of the step 5) is 3 to 5 hours; the reaction temperature of the calcining furnace is 800-1500 ℃, and the gas in the calcining furnace is one of nitrogen, argon and helium.
10. The device for the co-production process of the multipurpose high-performance needle coke as claimed in any one of claims 1 to 9, which comprises a mixed solvent tank, a raw material asphalt tank, a static mixer I, a flocculation tank I, a centrifugal device I, a static mixer II, a flocculation tank II, a centrifugal device II, a light phase tank A, a light phase tank B, a light phase tank C, a flash tower I, a flash tower II, a refined asphalt tank A, a refined asphalt tank B, a refined asphalt tank C, a pre-heating furnace, a delayed coking tower, a coke dryer and a calcining furnace, wherein one outlet of the mixed solvent tank and the outlet of the raw material asphalt tank are respectively connected with the inlet of the static mixer I, the outlet of the static mixer I is connected with the flocculation tank I, the outlet of the bottom of the flocculation tank I is divided into two paths, one path is connected with the centrifugal device I, the other path is connected with the static mixer II, the other outlet of the mixed solvent tank is also connected with the static mixer II, the centrifugal device I is connected with the light phase tank A, the upper outlet of the flocculation tank I is connected with the light phase tank II, the outlet of the flocculation tank II is connected with the centrifugal device II, and the centrifugal device II is connected with the flocculation tank II; the light phase tank A and the light phase tank B are respectively connected with a flash tower I, the light phase tank C is connected with a flash tower II, the outlet of the flash tower I is respectively connected with a refined asphalt tank A and a refined asphalt tank B, and the outlet of the flash tower II is connected with a refined asphalt tank C; the refined asphalt tank A, the refined asphalt tank B and the refined asphalt tank C are respectively connected with a preheating furnace, the preheating furnace is connected with a delayed coking tower, the delayed coking tower is connected with a coke dryer, and the coke dryer is connected with a calcining furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211055632.9A CN115433601B (en) | 2022-08-31 | 2022-08-31 | Co-production process and device for preparing multi-purpose high-performance needle coke |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211055632.9A CN115433601B (en) | 2022-08-31 | 2022-08-31 | Co-production process and device for preparing multi-purpose high-performance needle coke |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115433601A true CN115433601A (en) | 2022-12-06 |
| CN115433601B CN115433601B (en) | 2023-12-01 |
Family
ID=84244369
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211055632.9A Active CN115433601B (en) | 2022-08-31 | 2022-08-31 | Co-production process and device for preparing multi-purpose high-performance needle coke |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115433601B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115651689A (en) * | 2022-12-27 | 2023-01-31 | 唐山东日新能源材料有限公司 | Method for producing same-quality coke and needle coke by using soft asphalt |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4518486A (en) * | 1980-12-24 | 1985-05-21 | The Standard Oil Company | Concurrent production of two grades of coke using a single fractionator |
| CN86100675A (en) * | 1986-01-20 | 1987-02-25 | 冶金部鞍山焦化耐火材料设计研究院 | A kind of novel preparation method of coal-based needle coke |
| US20080003167A1 (en) * | 2006-06-29 | 2008-01-03 | Miller Douglas J | Method Of Producing Needle Coke For Low CTE Graphite Electrodes |
| CN102021005A (en) * | 2009-08-20 | 2011-04-20 | 山东金诚重油化工有限公司 | Method for producing needle coke |
| CN102329637A (en) * | 2011-08-29 | 2012-01-25 | 云南昆钢煤焦化有限公司 | Intensive production method of coal tar pitch needle coke |
| CN109868146A (en) * | 2019-03-14 | 2019-06-11 | 山西昭旭科技有限公司 | A kind of medium temperature coal pitch environmental protection and efficiently utilize combined producing process method |
| US20220041935A1 (en) * | 2020-08-05 | 2022-02-10 | Indian Oil Corporation Limited | Process for Production of Graphite Coke from an Admixture of Coal and Petroleum Based Hydrocarbons |
| CN114806620A (en) * | 2021-12-29 | 2022-07-29 | 宁夏百川新材料有限公司 | Pretreatment process for coal-based needle coke preparation raw material |
| US20220267151A1 (en) * | 2019-09-17 | 2022-08-25 | Nippon Steel Chemical & Material Co., Ltd. | Low-cte, low-puffing needle coke |
-
2022
- 2022-08-31 CN CN202211055632.9A patent/CN115433601B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4518486A (en) * | 1980-12-24 | 1985-05-21 | The Standard Oil Company | Concurrent production of two grades of coke using a single fractionator |
| CN86100675A (en) * | 1986-01-20 | 1987-02-25 | 冶金部鞍山焦化耐火材料设计研究院 | A kind of novel preparation method of coal-based needle coke |
| US20080003167A1 (en) * | 2006-06-29 | 2008-01-03 | Miller Douglas J | Method Of Producing Needle Coke For Low CTE Graphite Electrodes |
| CN102021005A (en) * | 2009-08-20 | 2011-04-20 | 山东金诚重油化工有限公司 | Method for producing needle coke |
| CN102329637A (en) * | 2011-08-29 | 2012-01-25 | 云南昆钢煤焦化有限公司 | Intensive production method of coal tar pitch needle coke |
| CN109868146A (en) * | 2019-03-14 | 2019-06-11 | 山西昭旭科技有限公司 | A kind of medium temperature coal pitch environmental protection and efficiently utilize combined producing process method |
| US20220267151A1 (en) * | 2019-09-17 | 2022-08-25 | Nippon Steel Chemical & Material Co., Ltd. | Low-cte, low-puffing needle coke |
| US20220041935A1 (en) * | 2020-08-05 | 2022-02-10 | Indian Oil Corporation Limited | Process for Production of Graphite Coke from an Admixture of Coal and Petroleum Based Hydrocarbons |
| CN114806620A (en) * | 2021-12-29 | 2022-07-29 | 宁夏百川新材料有限公司 | Pretreatment process for coal-based needle coke preparation raw material |
Non-Patent Citations (1)
| Title |
|---|
| 郭少青;张伟;王桂云;赵亮富;: "煤系针状焦原料预处理技术进展", 炭素技术, no. 03, pages 368 - 372 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115651689A (en) * | 2022-12-27 | 2023-01-31 | 唐山东日新能源材料有限公司 | Method for producing same-quality coke and needle coke by using soft asphalt |
| CN115651689B (en) * | 2022-12-27 | 2023-04-28 | 唐山东日新能源材料有限公司 | Method for producing like coke and needle coke by using soft asphalt |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115433601B (en) | 2023-12-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103396820B (en) | Method for preparing bio-oil through biomass pyrolysis | |
| CN109970038B (en) | Method for producing mesocarbon microbeads by using medium-low temperature coal tar as raw material | |
| CN115433601B (en) | Co-production process and device for preparing multi-purpose high-performance needle coke | |
| CN103614153A (en) | Preparation method of polycondensed asphalt, preparation method of needle coke and needle coke | |
| CN115093874B (en) | Preparation method and system of low-quinoline insoluble high-softening-point petroleum-based coated asphalt | |
| CN101724419A (en) | Method for producing needle coke by utilizing delay coking of coal tar | |
| CN112592734A (en) | Continuous production method of lithium ion battery cathode coating material | |
| CN109319758B (en) | Co-production process method of mesocarbon microbeads and negative electrode material coke | |
| CN113337304A (en) | Continuous production method of graphite coating material | |
| CN111453721A (en) | Preparation method and device of wide-area sheet-shaped structure cathode material special for lithium ion battery | |
| CN106635102B (en) | Process for producing negative electrode material coke by using supercritical extraction oil slurry as raw material and application thereof | |
| CN111826187A (en) | Novel high-performance asphalt special for carbon material and preparation method thereof | |
| CN212174460U (en) | Device for preparing wide-area sheet-shaped structure cathode material special for lithium ion battery | |
| CN214654660U (en) | Refined asphalt production device for efficiently separating quinoline insoluble substances from low-temperature asphalt | |
| CN112574770B (en) | Preparation method of high-quality coal-based needle coke | |
| CN110408418B (en) | Preparation method of high-regular-carbon microcrystalline pitch coke | |
| CN116120957A (en) | Method for preparing high-performance coal-based needle coke by thermal cracking | |
| KR101359266B1 (en) | Method for Preparing of Coal Pitch | |
| CN105087033A (en) | Method for preparing isotropic coke | |
| CN111180726B (en) | Production process and device for co-producing isotropic coke by using anode material | |
| CN107880921A (en) | A kind of petroleum Multifunctional asphalt resin and its manufacture method | |
| CN115594826B (en) | Low-energy-consumption synthesis method of carbon negative electrode coating material | |
| CN113716544B (en) | Preparation method of low-cost high-magnification anode material coke | |
| CN114133945B (en) | Asphalt coke and preparation method and application thereof | |
| CN212024783U (en) | Production device of hard carbon negative electrode material |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |