CN106635143B - A kind of method for preparing needle coke - Google Patents
A kind of method for preparing needle coke Download PDFInfo
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- CN106635143B CN106635143B CN201510730040.6A CN201510730040A CN106635143B CN 106635143 B CN106635143 B CN 106635143B CN 201510730040 A CN201510730040 A CN 201510730040A CN 106635143 B CN106635143 B CN 106635143B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
Abstract
The present invention provides a kind of method for preparing needle coke, and the heated stove heat of feedstock oil is to after 465 DEG C ~ 510 DEG C, and into coking tower, the oil gas for reacting generation is discharged from tower top；Gas, gasoline fraction, diesel oil distillate and wax oil cut are obtained after the Oil-gas Separation of generation, wherein, the wax oil cut enters coking tower after being mixed as recycle oil with certain recycle ratio with feedstock oil, when furnace outlet temperature is more than 490 DEG C, it is passed through from the lower charging aperture of coking tower and is not easy coking material, until reaction time terminates, the needle coke of generation is deposited on coking section bottom；The inventive method is effectively eliminated charging and is formed the disturbance brought to wide area interphase by the way of upper feeding and lower feed combinations.
Description
Technical field
The present invention relates to a kind of method for preparing needle coke, and low-heat is prepared using delay coking process more particularly to one kind
The coefficient of expansion（CTE）, low volatile needle coke method.
Background technology
Needle coke has the characteristics that CTE is low, easy graphitization, is the preferred material for producing high power and ultra high power graphite electrode
Material.In the forming process of needle coke, feedstock oil needs to undergo the generation of mesophasespherule, grows up, melts and wait course, develops
For wide area interphase, line style texture structure is then formed in the presence of air-flow again, needle coke is made in final curing.At the beginning of coking
Phase, excessive disturbance is avoided the occurrence of inside system, to ensure that mesophasespherule slowly, is smoothly developed, the hair of interphase
Educate the properties of product that degree direct influence needle coke；In " drawing burnt " stage, system domestic demand constantly will have air-flow at the uniform velocity to escape, will
Wide area interphase pulls into linear structure.
CN103045301 discloses a kind of method that needle coke is prepared using catalytic cracked oil pulp as raw material, works as delayed coking
When unit capacity reaches the 60% ~ 80% of its processing total amount, remaining cut after oil separates out gasoline will be generated and fully enter delay
For coking plant as burnt gas is drawn, obtained needle coke has high microsteping structure.
CN103184057 discloses a kind of method for preparing homogeneous petroleum needle coke.This method in initial reaction stage, raw material with
Lower temperature enter coking tower formed interphase liquid crystal, with the raising of furnace temp, raw material mix successively heavy distillate and
Intermediate oil enters coking tower together, finally make it that temperature reaches 510 DEG C in coking tower.
, it is necessary to provide mitigation, a stable environment for the formation of wide area interphase in needle coke preparation process, avoid
There is excessive disturbance in reaction system.On the contrary, in the pyrogenetic reaction middle and later periods, need constantly there is air-flow at the uniform velocity to escape inside system again
Go out, wide area interphase is pulled into line style texture structure.In addition, whole pyrogenetic reaction system is an alternating temperature operating process, in tower
The heat brought into fresh feed of origin of heat, in order to gradually step up the temperature of reaction system, generally require to improve constantly plus
The temperature of hot stove, prolonged high temperature operation inevitably result in inside heating furnace coking.
The content of the invention
In view of the shortcomings of the prior art, the present invention provides a kind of method for preparing needle coke, and this method is by using raw material
Upper feeding and lower feed combinations mode, in initial reaction stage, charging is effectively eliminated to wide area interphase by upper feeding mode
Form the disturbance brought；In the later stage in the reaction, La Jiao and heat supply can be played dual parts of by lower feeding manner.
The present invention provides a kind of method for preparing needle coke, and methods described includes herein below：
（1）Feedstock oil is after feedstock oil heating furnace is heated to 465 DEG C ~ 510 DEG C, into coking tower, reacts the oil gas of generation
Discharged from tower top；
（2）Step（1）The oil gas of generation enters fractionating system, and gas, gasoline fraction, diesel oil distillate and wax are obtained after separation
Oil distillate, wherein, the wax oil cut is as recycle oil and step（1）In feedstock oil mixing after enter coking tower；
（3）When feedstock oil furnace outlet temperature is more than 490 DEG C, it is passed through from the lower charging aperture of coking tower and is not easy coking material
Matter, until terminating reaction time, the needle coke of generation is deposited on coking section bottom；
Wherein, step（1）Described in heating furnace using one section of constant temperature-three sections of constant temperature of-two sections of heatings temperature programmed work
Mode, wherein, one section of constant temperature is 465 DEG C ~ 490 DEG C 10 ~ 25h of constant temperature, and two sections of heatings rise to 490 with 1 DEG C/h ~ 5 DEG C/h speed
℃~510℃；Three sections of constant temperature are 490 DEG C ~ 510 DEG C 1 ~ 5h of constant temperature, when heating furnace is in one section of constant temperature, feedstock oil and recycle oil
Coking tower is entered by enterprising material mouth；When heating furnace, which terminates one section of constant temperature, starts two sections of heatings, feedstock oil and recycle oil pass through
Lower charging aperture enters coking tower.
Coking tower of the present invention includes cylinder, upper cover and low head, and the cylinder from top to bottom sets gradually coking
Section and packing section, are provided with baffle plate between coking section and packing section, the baffle plate is the baffle plate with sieve aperture, coking section, baffle plate and
Packing section is fixedly connected by flange, and enterprising material mouth is set on the cylinder of the coking section, and the low head sets lower charging aperture,
Lower charging aperture connects with packing section.
In the coking tower, the packing section is highly 1/20~1/2, preferably the 1/20~1/5 of coking tower total height.
In the coking tower, the enterprising material mouth is located at the middle and upper part of the coking section of coking tower, apart from the bottom of towe of coking tower
Highly it is the 3/5 ~ 4/5 of total tower height.
In the coking tower, the baffle plate is the baffle plate with sieve aperture, and the baffle plate sieve aperture is shaped as square, rectangular
Shape, triangle, it is circular in one kind, it is preferably circular；Slot size is 0.1mm~10mm, preferably 1mm~5mm, and sieve aperture edge is kept off
Plate is radially distributed in concentric circles, and total percent opening of baffle plate is 5%~50%, can be uniform pore openings rate or non-homogeneous opens
Porosity, preferably non-uniform perforation, when for non-uniform perforation when, gradually increase from the center of circle along baffle plate radial direction screen-aperture
Big or sieve aperture quantity gradually increases.
In the coking tower, filling heatproof in the packing section, pressure-resistant, corrosion resistant inert filler, the filler can be with
For the one or more in stainless steel, ceramics, inertia silica, its shape can be Raschig ring, Pall ring or non-porous
Granulated filler, the main function of filler is to make to be not easy coking material along tower radial dispersion, avoids being not easy coking Concentration of matter
In tower central shaft area.
In the inventive method, described feedstock oil is the needle-shape coke raw material oil by pretreatment, can remove quinoline not
Coal tar, the coal tar asphalt of molten thing, specially require QI ≯ 0.1% in terms of mass content or pass through desulfurization, de-ash
One or several kinds of mixtures in the ethylene bottom oil of processing, catalytic cracking clarified oil, ardent slugging oil etc., are specially required with matter
Measure content meter S ≯ 0.5%, ash content ≯ 0.1%.
In the inventive method, the operation temperature of the coking tower is 450 DEG C ~ 505 DEG C, operating pressure be 0.5 MPa ~
2MPa, it can be constant voltage operation or become press operation.
In the inventive method, described wax oil cut first passes through be filtered to remove coke powder after mixed again with feedstock oil, recycle ratio
For 0.5 ~ 2, the recycle ratio is the mass ratio of wax oil cut and feedstock oil.
In the inventive method, described coking tower bottom gating location is the position of Conventional delayed coking charging aperture.
In the inventive method, the coking material that is not easy is the material that can carry enough heats, can be vapor, C1
Fractionating column is isolated in the one or more of or present invention in ~ C5 lighter hydrocarbons, light fraction oil gas, gasoline fraction,
One or more in diesel oil distillate.
In the inventive method, step（3）Described in be not easy enter coking after coking material is heated to 480 DEG C ~ 535 DEG C
Tower, the temperature for being not easy coking material are higher than temperature in coking tower 10 DEG C ~ 40 DEG C.
In the inventive method, step（3）Described in the inlet amount for being not easy coking material for coking tower feedstock oil and Jiao
Change wax oil total feed 0.5 ~ 3 times.
Compared with prior art, the method for the present invention for preparing needle coke has the following advantages that：
1st, coking tower is entered using upper feeding mode in pyrogenetic reaction initial stage, feedstock oil mixing circulation oil, avoid due to
The entrance of fresh feed and cause system disturbance excessive, for the generation of mesophasespherule, grow up and melt and provide one it is slow
With, stable developing environment, be advantageous to the formation of large area wide area interphase；In pyrogenetic reaction mid-term, feedstock oil mixing circulation
Oil is changed to enter coking tower from lower charging aperture, on the one hand reduces the viscosity of bottom of towe system, is on the other hand produced using pyrolytic reaction
Raw air-flow promotion system internal structure aligns；In the pyrogenetic reaction later stage, introduced into tower and be largely not easy coking material, by
Coking material is generally lighter than feedstock oil, molecule is small, more volatile in being not easy, therefore the dispersiveness in coking tower is relatively preferable,
Effusion faster, the linear velocity of the system internal gas flow of considerably increasing in axial direction, may advantageously facilitate " drawing for wide area interphase
It is burnt " effect.
2nd, in the pyrogenetic reaction later stage, in order to improve coking tower internal temperature, generally require to improve constantly feedstock oil and circulation
The feeding temperature of oil.And heating furnace is in higher temperature for a long time, tube coking will necessarily be caused serious, be unfavorable for the length of device
Phase operates.In the inventive method, the introducing is not easy coking material and entered with being higher by the temperature of 10 DEG C ~ 40 DEG C of coking tower from bottom of towe
Material, is sufficiently mixed in packing section and feedstock oil and recycle oil, can effectively improve the temperature of feedstock oil and recycle oil.Namely
Say, after the reaction the hot stage of phase, it is not necessary to improve the outlet temperature of heating furnace simply, but coking material is not easy by raising
Temperature bring heat into coking tower, as the main supplying heat source of whole reaction system.
3rd, coking tower packing section and baffle plate play good peptizaiton to bottom feed, to air-flow along tower in the radial direction
It is scattered play facilitation, also cause being uniformly distributed for system temperature improved, greatly improve coke texture structure and
Performance.In the decoking stage, the flange of coking section, baffle plate and packing section junction is dismantled, removes baffle plate and packing section, is then carried out
Normal de-coking operations.For the coke adhered on filler, it can be burnt up in air atmosphere, not interfering with the circulation of filler makes
With.
Figure of description
Fig. 1 is coking tower structural representation of the present invention.
Embodiment
The process and effect of the present invention is further illustrated with reference to embodiment.
Coking tower of the present invention includes cylinder 1, upper cover 2 and low head 3, and the cylinder 1 is from top to bottom set gradually
Coking section 4 and packing section 5, are provided with baffle plate 9 between coking section 4 and packing section 5, the baffle plate 9 is the baffle plate with sieve aperture, coking
Section 4, baffle plate 9 are fixedly connected with packing section 5 by flange 10, enterprising material mouth 8 are set on the cylinder of the coking section 4, under described
End socket 3 sets lower charging aperture 7, and lower charging aperture 7 connects with packing section 5.
The method that the present invention prepares needle coke is one section of perseverance that feedstock oil is heated to 465 DEG C ~ 490 DEG C through feedstock oil heating furnace
During thermophase, enter coking tower from enterprising material mouth 8；When heating furnace enters two sections of temperature rise periods, feedstock oil and recycle oil are changed to
Enter coking tower from lower charging aperture 7；When furnace outlet temperature is more than 490 DEG C, starts to be passed through from lower charging aperture 7 and be not easy coking
Material, it is not easy coking material and enters coking section 4 by packing section 5 and baffle plate 9 respectively, until reaction time terminates, wherein being not easy
Coking material is previously heated to 480 DEG C ~ 535 DEG C；The needle coke of generation is deposited on the bottom of coking section 4.In the decoking stage, dismantle
Flange 10 and the junction of baffle plate 9, are devoked；Filler in packing section 5, which can be poured out, to carry out burning cleaning.
Feedstock oil used in following examples and comparative example is to be shown in Table by the catalytic cracked oil pulp of pretreatment, specific nature
1；Recycle oil used is the wax oil cut that fractionating column is isolated（350 DEG C of ＞）；Used is not easy coking material as fractionating column point
The diesel oil distillate separated out（220~350℃）.
The fundamental property of the catalytic cracked oil pulp of table 1
Embodiment 1
The method that needle coke is prepared using coking tower of the present invention, feedstock oil and recycle oil are entered using upper and lower two-way
Material mode, it is not easy coking material and uses lower feeding manner, carries out delayed coking reaction.Wherein enterprising material mouth is highly apart from bottom of towe
The 4/5 of total tower height, the height of bottom of towe packing section are the 1/10 of total tower height.
Feedstock oil mixing circulation oil enters coking tower after feedstock oil heats stove heat, and recycle ratio 0.8, feedstock oil adds
Hot stove is controlled using alternating temperature, 470 DEG C of holding 15h of initial temperature, is then warming up to 500 DEG C of holding 3h with 4 DEG C/h speed.Work as original
When to expect oily furnace outlet temperature be 470 DEG C of constant temperature, feedstock oil and recycle oil enter coking tower from enterprising material mouth；When feedstock oil plus
When hot stove is in the temperature programming stage, feedstock oil and recycle oil enter coking tower from lower charging aperture；When feedstock oil heating furnace reaches
At 500 DEG C, it is not easy coking material and also enters coking tower from lower charging aperture together after heating in advance.It is not easy adding for coking material
Hot stove is also controlled using alternating temperature, and initial temperature is 500 DEG C, is then warming up to 525 DEG C with 10 DEG C/h speed and keeps constant temperature, directly
Terminate to reaction.The inlet amount for being not easy coking material is 1.1 times of feedstock oil and recycle oil inlet amount.In whole course of reaction
In, temperature range is 454 DEG C ~ 493 DEG C in coking tower, and constant pressure is 1.5MPa.The needle coke volatile matter content prepared
0.68%wt, the thermal coefficient of expansion of sample is 1.42 × 10 after graphitization-6/℃(100℃~600℃)。
Embodiment 2
Embodiment prepares needle coke using the inventive method.Different from embodiment 1, coking tower has pressure release in coking
Journey.
Feedstock oil mixing circulation oil enters coking tower after feedstock oil heats stove heat, and recycle ratio 1.2, feedstock oil adds
Hot stove is controlled using alternating temperature, 480 DEG C of holding 15h of initial temperature, is then warming up to 505 DEG C of holding 3h with 3 DEG C/h speed.Work as original
When to expect oily furnace outlet temperature be 480 DEG C of constant temperature, feedstock oil and recycle oil enter coking tower from enterprising material mouth；When feedstock oil plus
When hot stove is in two sections of temperature rise periods, feedstock oil and recycle oil enter coking tower from lower charging aperture；When feedstock oil heating furnace reaches
At 505 DEG C, it is not easy coking material and also enters coking tower from lower charging aperture together after heating in advance.It is not easy adding for coking material
Thermal process is also controlled using alternating temperature, and initial temperature is 505 DEG C, is then warming up to 530 DEG C with 10 DEG C/h speed and keeps constant temperature,
Until reaction terminates.The inlet amount for being not easy coking material is the 0.9 of feedstock oil and recycle oil inlet amount.In whole course of reaction
In, temperature range is 461 DEG C ~ 496 DEG C in coking tower；Initial pressure is 1.5MPa, when feedstock oil furnace outlet temperature reaches
At 505 DEG C, first introduce after being not easy coking material, then system pressure is down to 0.5MPa in 20min.The needle coke prepared is waved
Send out and divide content 0.46%wt, the thermal coefficient of expansion of sample is 1.29 × 10 after graphitization-6/℃(100℃~600℃)。
Comparative example 1
Comparative example prepares needle coke using traditional coking method, and feedstock oil and recycle oil are carried out using lower feeding manner all the time
Delayed coking reaction, and the coking tower does not have packing section, introducing is not easy coking material.
Feedstock oil mixing circulation oil enters coking tower, recycle ratio 0.8 after feedstock oil heats stove heat.Feedstock oil adds
Hot stove is controlled using alternating temperature, 470 DEG C of holding 15h of initial temperature, and then 4 DEG C/h speed is warming up to 505 DEG C of holding 3h.Whole
In course of reaction, temperature range is 454 DEG C ~ 487 DEG C in coking tower, and constant pressure is 1.5MPa.The needle coke volatilization prepared
Point content 0.87%wt, the thermal coefficient of expansion of sample is 1.54 × 10 after graphitization-6/℃(100℃~600℃)。
Comparative example 2
It is identical with comparative example 1, it is a difference in that in coking that coking tower has pressure leak process.
Feedstock oil mixing circulation oil enters coking tower, recycle ratio 1.3 after feedstock oil heats stove heat.Feedstock oil adds
Hot stove is controlled using alternating temperature, 480 DEG C of holding 15h of initial temperature, and then 3 DEG C/h speed is warming up to 505 DEG C of holding 3h.Whole
In course of reaction, temperature range is 462 DEG C ~ 488 DEG C in coking tower；Initial pressure is 1.5MPa, when feedstock oil furnace outlet
When temperature reaches 490 DEG C, system pressure is down to 0.5MPa in 20min.The needle coke volatile matter content 0.56% prepared
Wt, the thermal coefficient of expansion of sample is 1.41 × 10 after graphitization-6/℃(100℃~600℃)。
Comparative example 3
Comparative example prepares needle coke using traditional coking method.Bottom of towe is equipped with filler, and packing section is highly the 1/ of total tower height
10.Different from comparative example 2, the coking later stage introduces from lower charging aperture to coking tower and is not easy coking material, and is not easy coking material
A heating stove heat is shared with feedstock oil and recycle oil.
Feedstock oil mixing circulation oil enters coking tower, recycle ratio 1.3 after feedstock oil heats stove heat.Feedstock oil adds
Hot stove is controlled using alternating temperature, 470 DEG C of holding 15h of initial temperature, and then 4 DEG C/h speed is warming up to 505 DEG C of holding 3h.Whole
In course of reaction, temperature range is 453 DEG C ~ 489 DEG C in coking tower；Initial pressure is 1.5MPa, when feedstock oil furnace outlet
When temperature reaches 505 DEG C, system pressure is down to 0.5MPa in 20min.Before pressure release, it will first be not easy to make friends with material process
Also controlled after heating stove heat from lower charging aperture introducing coking tower, this heating furnace using alternating temperature, initial temperature is 505 DEG C, then
530 DEG C are warming up to 10 DEG C/h speed and keeps constant temperature, until reaction terminates.In addition, the inlet amount for being not easy coking material is
The 0.9 of feedstock oil and recycle oil inlet amount.The needle coke volatile matter content 0.53%wt prepared, sample is hot swollen after graphitization
Swollen coefficient is 1.38 × 10-6/℃(100℃~600℃)。
Claims (18)
1. a kind of method for preparing needle coke, methods described includes herein below：
（1）Feedstock oil is after feedstock oil heating furnace is heated to 465 DEG C ~ 510 DEG C, into coking tower, reacts the oil gas of generation from tower
Top row goes out；
（2）Step（1）The oil gas of generation enters fractionating system, and gas, gasoline fraction, diesel oil distillate and wax oil are obtained after separation and is evaporated
Point, wherein, the wax oil cut is as recycle oil and step（1）In feedstock oil mixing after enter coking tower；
（3）When feedstock oil furnace outlet temperature is more than 490 DEG C, it is passed through from the lower charging aperture of coking tower and is not easy coking material,
Until reaction time terminates, the needle coke of generation is deposited on coking section bottom, and the coking material that is not easy is vapor, C1 ~ C5
One or more in the gas that lighter hydrocarbons, light fraction are oily, the fractionating system is isolated；
Wherein, step（1）Described in heating furnace using one section of constant temperature-three sections of constant temperature of-two sections of heatings temperature programmed work mode,
Wherein, one section of constant temperature is 465 DEG C ~ 485 DEG C 10 ~ 25h of constant temperature, and two sections of heatings rise to 490 DEG C ~ 510 with 1 DEG C/h ~ 5 DEG C/h speed
℃；Three sections of constant temperature are 490 DEG C ~ 510 DEG C 1 ~ 5h of constant temperature, and when heating furnace is in one section of constant temperature, feedstock oil and recycle oil pass through upper
Charging aperture enters coking tower；When heating furnace, which terminates one section of constant temperature, starts two sections of heatings, feedstock oil and recycle oil pass through lower charging
Mouth enters coking tower.
2. in accordance with the method for claim 1, it is characterised in that：The coking tower includes cylinder, upper cover and low head, institute
State cylinder and from top to bottom set gradually coking section and packing section, baffle plate is provided between coking section and packing section, the baffle plate is band
There is the baffle plate of sieve aperture, coking section, baffle plate and packing section are fixedly connected by flange, and upper feeding is set on the cylinder of the coking section
Mouthful, the low head sets lower charging aperture, and lower charging aperture connects with packing section.
3. in accordance with the method for claim 2, it is characterised in that：The packing section highly for coking tower total height 1/20~
1/2。
4. in accordance with the method for claim 2, it is characterised in that：The packing section highly for coking tower total height 1/20~
1/5。
5. in accordance with the method for claim 2, it is characterised in that：On the enterprising material mouth is located in the coking section of coking tower
Portion, the bottom of towe apart from coking tower are highly the 3/5 ~ 4/5 of total tower height.
6. in accordance with the method for claim 2, it is characterised in that：The baffle plate is the baffle plate with sieve aperture, the baffle plate sieve
Hole is shaped as square, rectangle, one kind in triangle or circle.
7. in accordance with the method for claim 6, it is characterised in that：The baffle plate sieve aperture is shaped as circle.
8. in accordance with the method for claim 5, it is characterised in that：The slot size is 0.1mm~10mm.
9. in accordance with the method for claim 8, it is characterised in that：The slot size is 1mm~5mm.
10. in accordance with the method for claim 6, it is characterised in that：The sieve aperture is radially distributed along baffle plate in concentric circles, baffle plate
Total percent opening be 5%~50%.
11. in accordance with the method for claim 10, it is characterised in that：The baffle plate uses uniform pore openings rate or non-homogeneous perforate
Rate, when for non-uniform perforation when, from the center of circle along baffle plate radial direction screen-aperture gradually increase or sieve aperture quantity it is gradual
Increase.
12. in accordance with the method for claim 2, it is characterised in that：It is filling heatproof in the packing section, pressure-resistant, corrosion resistant
Inert filler, the filler are the one or more in stainless steel, ceramics, inertia silica, and its shape is Raschig ring, Bauer
Ring.
13. in accordance with the method for claim 1, it is characterised in that：Described feedstock oil is the coal tar for removing quinoline insolubles
Oil, coal tar asphalt, QI ≯ 0.1% in terms of mass content, or split by desulfurization, the ethylene bottom oil of de-ash processing, catalysis
Change one or several kinds of mixtures in clarified oil, ardent slugging oil, S ≯ 0.5%, ash content ≯ 0.1% in terms of mass content.
14. in accordance with the method for claim 1, it is characterised in that：The operation temperature of the coking tower is 450 DEG C ~ 505 DEG C,
Operating pressure is 0.5 MPa ~ 2MPa.
15. in accordance with the method for claim 1, it is characterised in that：Described wax oil cut first passes through be filtered to remove coke powder after
Mixed again with feedstock oil, recycle ratio is 0.5 ~ 2.
16. in accordance with the method for claim 1, it is characterised in that：Step（3）Described in the coking material that is not easy be heated to
Enter coking tower after 480 DEG C ~ 535 DEG C.
17. in accordance with the method for claim 1, it is characterised in that：Step（3）Described in the temperature for being not easy coking material ratio
In coking tower temperature it is high 10 DEG C ~ 40 DEG C.
18. in accordance with the method for claim 1, it is characterised in that：Step（3）Described in the inlet amount for being not easy coking material
0.5 ~ 3 times of feedstock oil and wax tailings total feed for coking tower.
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| CN108130119A (en) * | 2018-02-05 | 2018-06-08 | 曹式黎 | A kind of drawing of needle coke industrialized production is burnt, drying means |
| CN114479906B (en) * | 2020-10-27 | 2023-08-08 | 中国石油化工股份有限公司 | Method for preparing high-quality petroleum coke |
| CN114479921B (en) * | 2020-10-27 | 2023-08-08 | 中国石油化工股份有限公司 | Method for preparing needle coke |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1769373A (en) * | 2004-11-04 | 2006-05-10 | 戴惠筠 | Method for producing high quality needle-type coke by improving coking process |
| CN101302434A (en) * | 2008-06-20 | 2008-11-12 | 中国石油大学(华东) | Process for preparing needle coke |
| CN101597518A (en) * | 2009-06-25 | 2009-12-09 | 中国石油化工集团公司 | A kind of improved delay coking process |
| 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 |
| CN102295943A (en) * | 2011-08-12 | 2011-12-28 | 中石油东北炼化工程有限公司葫芦岛设计院 | Method for coking needle coke by large recycle ratio oil system |
| CN103215062A (en) * | 2013-05-07 | 2013-07-24 | 山东东明石化集团有限公司 | Delay coking processing method of inferior residual oil |
| CN104164253A (en) * | 2013-05-15 | 2014-11-26 | 中石化洛阳工程有限公司 | Heavy oil processing method |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102011122322A1 (en) * | 2011-12-23 | 2013-06-27 | Mann + Hummel Gmbh | Centrifugal separator and filter arrangement |
-
2015
- 2015-11-02 CN CN201510730040.6A patent/CN106635143B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1769373A (en) * | 2004-11-04 | 2006-05-10 | 戴惠筠 | Method for producing high quality needle-type coke by improving coking process |
| CN101302434A (en) * | 2008-06-20 | 2008-11-12 | 中国石油大学(华东) | Process for preparing needle coke |
| CN101597518A (en) * | 2009-06-25 | 2009-12-09 | 中国石油化工集团公司 | A kind of improved delay coking process |
| 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 |
| CN102295943A (en) * | 2011-08-12 | 2011-12-28 | 中石油东北炼化工程有限公司葫芦岛设计院 | Method for coking needle coke by large recycle ratio oil system |
| CN103215062A (en) * | 2013-05-07 | 2013-07-24 | 山东东明石化集团有限公司 | Delay coking processing method of inferior residual oil |
| CN104164253A (en) * | 2013-05-15 | 2014-11-26 | 中石化洛阳工程有限公司 | Heavy oil processing method |
Non-Patent Citations (1)
| Title |
|---|
| 提高液体收率的上进料延迟焦化新工艺;王宝石等;《石油学报（石油加工）》;20120831;第28卷(第4期);第544-549页 * |
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