CN1676575A - Delayed coking method for increasing coke strength - Google Patents
Delayed coking method for increasing coke strength Download PDFInfo
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- CN1676575A CN1676575A CN 200410029874 CN200410029874A CN1676575A CN 1676575 A CN1676575 A CN 1676575A CN 200410029874 CN200410029874 CN 200410029874 CN 200410029874 A CN200410029874 A CN 200410029874A CN 1676575 A CN1676575 A CN 1676575A
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- coke
- coking
- oil
- recycle ratio
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- 239000000571 coke Substances 0.000 title claims abstract description 86
- 238000004939 coking Methods 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims abstract description 33
- 230000003111 delayed effect Effects 0.000 title claims description 16
- 238000010438 heat treatment Methods 0.000 claims abstract description 4
- 239000002994 raw material Substances 0.000 claims description 22
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 230000001698 pyrogenic effect Effects 0.000 claims description 8
- 230000008859 change Effects 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 230000009466 transformation Effects 0.000 claims description 4
- 238000004231 fluid catalytic cracking Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 2
- 239000005977 Ethylene Substances 0.000 claims description 2
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 2
- 238000010411 cooking Methods 0.000 claims description 2
- 239000004519 grease Substances 0.000 claims description 2
- 238000004230 steam cracking Methods 0.000 claims description 2
- 238000004227 thermal cracking Methods 0.000 claims description 2
- 239000000843 powder Substances 0.000 abstract description 5
- 239000002283 diesel fuel Substances 0.000 abstract description 2
- 230000001351 cycling effect Effects 0.000 abstract 1
- 239000011331 needle coke Substances 0.000 description 19
- 239000002010 green coke Substances 0.000 description 9
- 239000000463 material Substances 0.000 description 6
- 239000007789 gas Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 238000002474 experimental method Methods 0.000 description 4
- 239000003208 petroleum Substances 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 238000001354 calcination Methods 0.000 description 3
- 239000010439 graphite Substances 0.000 description 3
- 229910002804 graphite Inorganic materials 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002006 petroleum coke Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000010426 asphalt Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000005235 decoking Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000009866 aluminium metallurgy Methods 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000004377 microelectronic Methods 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
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- Coke Industry (AREA)
Abstract
This invention is delay coking method of improving coke intensity. The coking raw oil goes into the coke tower after being heated by coking heating furnace, and react under the condition of temperature changing, pressure changing and cycling ratio changing and the coke produced is left in the tower, and the coking oil is separated into coked gas, coked oil, coked diesel oil and coked wax oil. This method produces acerate coke with relatively high intensity in order to decrease the powder coke contents in the coke, and meanwhile lowers the heat expansion coefficient of coke and improves the quality of acerate coke.
Description
Technical field
The invention belongs to a kind of under the situation that does not have hydrogen the thermal non-catalytic cracking method of hydrocarbon ils, more particularly, be a kind of delayed coking method that improves coke strenth.
Background technology
Delayed coking is a kind of heat processing technique that petroleum is converted into gas, gasoline fraction, diesel oil distillate, wax oil cut and refinery coke, it is cheap that it has investment, turndown ratio is big, and the economic value added advantages of higher plays an important role in refining of petroleum.Refinery coke is generally as the byproduct of delay coking process process, less expensive.But selection aromaticity content height, the raw material that sulphur content is low, asphalt content is low can be produced high-quality petroleum coke, i.e. acicular petroleum coke by the suitable adjustment of operating procedure.Petroleum needle coke is a kind of high-quality of sixties exploitation, the refinery coke product with special purpose.The graphite product made from petroleum needle coke has characteristics such as high-density, high purity, high-crystallinity, high conductivity, low ablative, low modulus, low thermal coefficient of expansion, in national defence, metallurgical industry, be widely used, and develop to high-tech sectors such as medical treatment, laser, high energy equipment, microelectronics gradually.In metallurgical industry, the ultra-high power graphite electrode made from needle coke can obviously improve smelting efficient, increases output, cuts down the consumption of energy and raw materials consumption, reduces and pollutes, and improves environment.
The ordinary method of producing needle coke is to take to operate under the constant condition of alternating temperature, constant voltage, recycle ratio.Adopt traditional needle coke production technique to produce easily a large amount of coke powders, and the needle coke that contains a large amount of coke powders is unsuitable for as producing ultra-high power graphite electrode.Compare with bulk or macrobead needle coke, the needle coke price that contains a large amount of coke breezes is wanted considerably cheaper.Therefore reduce coke breeze content, the needle coke quality is significant for improving.The general coke that goes out from delayed coker produces, the intensity that is green coke is lower than the intensity of ripe Jiao after calcining, therefore with regard to the easier interference that is subjected to external force and fragmentation, as in delayed coking unit water conservancy decoking process and in green coke loading and unloading, transportation and calcination processing process, being easy to be subjected to outside destroy formation coke breeze.Therefore the intensity that improves the green coke that delayed coker produces goes out is to reduce coke breeze output, improves the effective measure of needle coke quality.
In order to reduce powder coke content, improve the needle coke quality, US4,521,278 and US5,007,987 green coke that proposes delayed coker produces is gone out is before advancing the calcining petroleum coke device, improve coke strenth to 24 hours internal heating to 875-1200 °F (about 468-649 ℃) last 10 minute at special device, reduced powder coke content.But this method can't avoid delayed coking unit in the water conservancy decoking process and green coke stores and transportation in green coke intensity hang down the tendency that is subjected to outside destroy and generates coke breeze.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of delayed coking method that improves coke strenth, the needle coke that this method production intensity is higher relatively.
Method provided by the invention comprises: coking raw material oil enters coke drum after the coking heater heating, under the condition of alternating temperature, transformation and/or change recycle ratio, react, the coke that generates is stayed in the coke drum, and coking oil gas obtains cooking gas, coker gasoline, coker gas oil, wax tailings through separation.
This method is produced the higher needle coke of intensity, thereby reduces the content of coke breeze in the coke, reduces the thermal expansivity of coke simultaneously, improves the quality of needle coke.
Embodiment
The present invention improves the delayed coking method of coke strenth, is the working method that adopts alternating temperature, transformation and/or become recycle ratio, improves the temperature of reaction of coke drum internal reaction material, thereby reduces coke volatile component, improves the intensity of coke.
Its implementation method is to begin to improve furnace outlet temperature and coke tower top pressure in the 1/4-3/4 time in each coke drum operational cycle, or raising furnace outlet temperature and recycle ratio, or improve furnace outlet temperature, coke tower top pressure and recycle ratio simultaneously, and then improve material temperature in the coke drum.Specifically, the Outlet Temperature in Delayed Coking Furnace variation range is 400-540 ℃, and coke tower top pressure variation range is 0.1-1.5MPa, and the recycle ratio variation range of pyrogenic reaction is 0-∞.
The described operational cycle is that the coking time of each coke drum is 20-50 hour, the coking time is meant that this coke drum switches to another coke drum used time to switching four-way valve with raw material from advancing coking raw material, and the coking time has been reflected the length of coking raw material in the coke drum internal reaction time.
The pyrogenic reaction recycle ratio is meant the weight and the weight ratio of advancing the stock oil of coking radiating furnace tube of the turning oil that at a time advances the coking radiating furnace tube, recycle ratio is 0 to mean and do not contain turning oil in the coking raw material that recycle ratio is that ∞ means that coking raw material all is a turning oil.Less in the initial stage in operational cycle recycle ratio, can be 0-1.0, behind the 1/4-3/4 in operational cycle, recycle ratio is 0.2-∞.General coking radiation feeding manner can be independent coking raw material oil, coking raw material oil and the mixture of turning oil, independent coking recycle oil and optional wax tailings, and wherein wax tailings also can be used as a kind of turning oil.Coking raw material grease separation is from the mixture of the tar of long residuum, vacuum residuum, visbreaking residue, thermal cracking residue, fluid catalytic cracking decant oil, lubex, preparing ethylene by steam cracking, hydrocracking tail oil, straight-run gas oil, wax tailings or above any two or plurality of raw materials.
Improve the furnace outlet temperature, can improve the temperature of reaction of material in the coke drum; Improve the coke tower top pressure a part of coking recycle oil and wax tailings are kept in the coke drum, their high potential temperature heat energy is retained in the coke drum, thereby has improved the temperature of reaction of material in the coke drum; Improving recycle ratio can bring more heat into coke drum, has also just improved the temperature of reaction of material in the coke drum.Therefore by alternating temperature, transformation and/or the operation of change recycle ratio, can control in a coke drum operational cycle temperature of reaction of material in the differential responses time coke drum, thereby reach the purpose of controlling the coke drum temperature and pressure according to required optimal reaction temperature of differential responses time and pressure.
Advantage of the present invention is to produce the higher needle coke of intensity on delayed coking unit, thereby reduces the content of coke breeze in the coke, reduces the thermal expansivity of coke simultaneously, improves the quality of needle coke.Method of the present invention also is applicable to production aluminium metallurgy coke product.
The intensity of coke adopts ASTM D5003 refinery coke Ha Shi can grind index (HardgroveGrindability Index is HGI), and numerical value is more little, and the intensity of expression coke is high more.
The following examples will give further instruction to present method, but therefore not limit present method.
Comparative Examples 1
The employing fluid catalytic cracking decant oil is a raw material, carries out the delayed coking experiment, and feedstock property sees Table 1.The pyrogenic reaction condition is 460 ℃ of furnace outlet temperature initial stages, raises gradually then, and in 510 ℃ of latter stages, the coke tower top pressure is constant in 0.3MPa, and recycle ratio is 0.5: 1, and gained needle coke character sees Table 2 after the pyrogenic reaction.
Comparative Examples 2
Adopt above-mentioned raw materials to carry out the coking experiment, the coke drum charging of coking initial stage is independent coking raw material oil, the furnace outlet temperature maintenance is at 455 ℃, the coke drum charging changes independent coking recycle oil and wax tailings circulation into after 1.67/4 time in coking operation cycle, heater outlet temperature remains unchanged after being elevated to 510 ℃, the coke tower top pressure is constant in 0.5MPa in the cycle in entire operation, and coke property is listed in table 2 after the pyrogenic reaction.
Embodiment 1
Adopt above-mentioned raw materials to carry out the coking experiment, the coke drum charging of coking initial stage is independent coking raw material oil, the furnace outlet temperature maintenance is at 455 ℃, the coke tower top pressure initial stage maintains 0.2MPa, after 1.67/4 time in coking operation cycle, the coke drum charging changes independent coking recycle oil and wax tailings circulation into, and heater outlet temperature remains unchanged after being elevated to 510 ℃, the coke tower top pressure is elevated to 1.0MPa and remains unchanged, and coke property is listed in table 2 after the pyrogenic reaction.
As can be seen from Table 2, adopt coke strenth of the present invention obviously to improve, the volatile matter that shows as green coke reduces, wear-resistant index reduces.The present invention can improve the true density of coke simultaneously, reduces the thermal expansivity of coke, has improved the needle coke quality.
Embodiment 2
Still adopt above-mentioned raw materials to carry out the coking experiment, coking initial stage furnace outlet temperature is 450 ℃, elevated temperature after 1/2 time in coking operation cycle, and latter stage, temperature reached 515 ℃; Coke tower top pressure initial stage 0.2MPa, the pressure that raises after 1/2 time in coking operation cycle reaches 1.0MPa latter stage; The recycle ratio initial stage is 0.1, improves recycle ratio after 1/2 time in coking operation cycle, and reach 10: 1 latter stage, and coke property is listed in table 2 after the pyrogenic reaction.
As can be seen from Table 2, adopt coke strenth of the present invention obviously to improve, the volatile matter that shows as green coke reduces, wear-resistant index reduces.The present invention can improve the true density of coke simultaneously, reduces the thermal expansivity of coke, has improved the needle coke quality.
Table 1
| Density (20 ℃), g/cm 3Kinematic viscosity (100 ℃), mm 2/ s carbon residue, the wt% ash content, the wt% ultimate analysis, wt% C H S N metal analysis, mg/kg Ni V compositional analysis, the saturated part aromatic hydrocarbons gum asphalt of wt% vacuum distillation range, ℃ initial boiling point 10% 50% 70% | ????1.0635 ????63.28 ????13.8 ????0.015 ? ????89.31 ????9.24 ????0.36 ????0.51 ? ????22.5 ????＜0.1 ? ????32.6 ????53.3 ????13.2 ????1.1 ? ????302 ????384 ????451 ????490 |
Table 2
| Comparative Examples 1 | Comparative Examples 2 | Embodiment 1 | Embodiment 2 | |
| Green coke: wear-resistant index (HGI) volatile matter, wt% S, the wt% ash content, ripe Jiao of wt%: true density, g/cm 3Volatile matter, wt% S, the wt% ash content, wt% CTE, * 10 -6/ ℃ (1000 ℃ are burnt till, room temperature～600 ℃) | ? ????135 ????7.4 ????0.32 ????0.055 ? ????2.122 ????0.7 ????0.33 ????0.081 ????2.46 ? | ? ????121 ????6.5 ????0.32 ????0.053 ? ????2.122 ????0.6 ????0.33 ????0.079 ????2.40 | ? ????102 ????4.5 ????0.32 ????0.051 ? ????2.126 ????0.6 ????0.34 ????0.079 ????2.31 | ? ????108 ????4.2 ????0.31 ????0.050 ? ????2.125 ????0.6 ????0.33 ????0.077 ????2.35 |
Claims (8)
1, a kind of delayed coking method that improves coke strenth, coking raw material oil enters coke drum after the coking heater heating, under the condition of alternating temperature, react, the coke that generates is stayed in the coke drum, coking oil gas obtains cooking gas, coker gasoline, coker gas oil, wax tailings through separation, it is characterized in that coking raw material oil reacts under the condition of transformation and/or change recycle ratio.
2,, it is characterized in that the mixture of described coking raw material grease separation from the tar of long residuum, vacuum residuum, visbreaking residue, thermal cracking residue, fluid catalytic cracking decant oil, lubex, preparing ethylene by steam cracking, hydrocracking tail oil, straight-run gas oil, wax tailings or above any two or plurality of raw materials according to the method for claim 1.
3,, it is characterized in that beginning to change temperature, pressure and recycle ratio in the 1/4-3/4 time in each coke drum operational cycle according to the method for claim 1.
4,, it is characterized in that the described operational cycle is 20-50 hour according to the method for claim 3.
5, according to claim 1,3 or 4 method, it is characterized in that the Outlet Temperature in Delayed Coking Furnace variation range is 400-540 ℃.
6, according to claim 1,3 or 4 method, it is characterized in that coke tower top pressure variation range is 0.1-1.5MPa.
7, according to claim 1,3 or 4 method, the recycle ratio variation range that it is characterized in that pyrogenic reaction is 0-∞.
8, according to the method for claim 7, it is characterized in that recycle ratio is 0-1.0 at the initial stage in operational cycle, be 0.2-∞ in the middle and later periods.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100298746A CN1323131C (en) | 2004-03-31 | 2004-03-31 | Delayed coking method for increasing coke strength |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100298746A CN1323131C (en) | 2004-03-31 | 2004-03-31 | Delayed coking method for increasing coke strength |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1676575A true CN1676575A (en) | 2005-10-05 |
| CN1323131C CN1323131C (en) | 2007-06-27 |
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| CNB2004100298746A Expired - Lifetime CN1323131C (en) | 2004-03-31 | 2004-03-31 | Delayed coking method for increasing coke strength |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101302434B (en) * | 2008-06-20 | 2012-09-26 | 中国石油大学(华东) | Process for preparing needle coke |
| CN103184057A (en) * | 2011-12-29 | 2013-07-03 | 中国石油化工股份有限公司 | Production method of homogeneous petroleum needle coke |
| CN106675632A (en) * | 2015-11-09 | 2017-05-17 | 中国石油化工股份有限公司 | Delayed coking method |
| CN109439353A (en) * | 2018-11-19 | 2019-03-08 | 山西中科化美科技有限责任公司 | A kind of coking calcining integration system of refined bitumen is for needle coke technique |
| CN109943354A (en) * | 2019-03-29 | 2019-06-28 | 山东益大新材料有限公司 | A kind of Co carbonization technique of aromatic naphtha and refined bitumen mixed raw material |
| CN113355117A (en) * | 2017-11-14 | 2021-09-07 | 中国石油化工股份有限公司 | Coking system and coking method |
| CN113698956A (en) * | 2021-08-31 | 2021-11-26 | 山东亿维新材料有限责任公司 | Production process for improving compressive strength of needle coke |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5007987A (en) * | 1983-04-27 | 1991-04-16 | Union Oil Company Of California | Method for producing needle coke |
| CN1063213C (en) * | 1996-07-25 | 2001-03-14 | 沿海化工(鞍山)有限公司 | Process for producing improved coal system needle coke |
| CN1417294A (en) * | 2001-11-06 | 2003-05-14 | 中国石化集团长岭炼油化工有限责任公司 | Delayed coking process capable of flexibly regulating circulation ratio |
-
2004
- 2004-03-31 CN CNB2004100298746A patent/CN1323131C/en not_active Expired - Lifetime
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101302434B (en) * | 2008-06-20 | 2012-09-26 | 中国石油大学(华东) | Process for preparing needle coke |
| CN103184057A (en) * | 2011-12-29 | 2013-07-03 | 中国石油化工股份有限公司 | Production method of homogeneous petroleum needle coke |
| CN103184057B (en) * | 2011-12-29 | 2014-12-31 | 中国石油化工股份有限公司 | Production method of homogeneous petroleum needle coke |
| CN106675632A (en) * | 2015-11-09 | 2017-05-17 | 中国石油化工股份有限公司 | Delayed coking method |
| CN106675632B (en) * | 2015-11-09 | 2020-02-14 | 中国石油化工股份有限公司 | Delayed coking method |
| CN113355117A (en) * | 2017-11-14 | 2021-09-07 | 中国石油化工股份有限公司 | Coking system and coking method |
| CN109439353A (en) * | 2018-11-19 | 2019-03-08 | 山西中科化美科技有限责任公司 | A kind of coking calcining integration system of refined bitumen is for needle coke technique |
| CN109943354A (en) * | 2019-03-29 | 2019-06-28 | 山东益大新材料有限公司 | A kind of Co carbonization technique of aromatic naphtha and refined bitumen mixed raw material |
| CN113698956A (en) * | 2021-08-31 | 2021-11-26 | 山东亿维新材料有限责任公司 | Production process for improving compressive strength of needle coke |
| CN113698956B (en) * | 2021-08-31 | 2022-11-15 | 山东亿维新材料有限责任公司 | Production process for improving compressive strength of needle coke |
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| Publication number | Publication date |
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| CN1323131C (en) | 2007-06-27 |
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