CN1115375C - Improved coking process with two-channel feed system - Google Patents
Improved coking process with two-channel feed system Download PDFInfo
- Publication number
- CN1115375C CN1115375C CN 98117810 CN98117810A CN1115375C CN 1115375 C CN1115375 C CN 1115375C CN 98117810 CN98117810 CN 98117810 CN 98117810 A CN98117810 A CN 98117810A CN 1115375 C CN1115375 C CN 1115375C
- Authority
- CN
- China
- Prior art keywords
- feed system
- main
- coke
- separation column
- enters
- 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.)
- Expired - Lifetime
Links
- 238000004939 coking Methods 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000000571 coke Substances 0.000 claims abstract description 57
- 239000002994 raw material Substances 0.000 claims abstract description 21
- 238000000926 separation method Methods 0.000 claims description 11
- 230000005855 radiation Effects 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 238000005516 engineering process Methods 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 230000026676 system process Effects 0.000 claims 3
- 229920006395 saturated elastomer Polymers 0.000 claims 2
- 238000005194 fractionation Methods 0.000 abstract description 37
- 238000010438 heat treatment Methods 0.000 abstract description 37
- 239000002006 petroleum coke Substances 0.000 abstract description 5
- 238000006243 chemical reaction Methods 0.000 description 12
- 230000003111 delayed effect Effects 0.000 description 10
- 239000002283 diesel fuel Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000004227 thermal cracking Methods 0.000 description 3
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 238000006482 condensation reaction Methods 0.000 description 2
- 238000005235 decoking Methods 0.000 description 2
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011331 needle coke Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Coke Industry (AREA)
Abstract
一种改进的具有两路进料系统的焦化工艺，是采用主进料、副进料两个系统，共用一个分馏塔，当副进料系统加热炉炉管结焦后，主进料的一部分进入共用分馏塔以维持正常操作；当主进料系统的原料饱和份大于40重%时，分馏塔的重馏分油循环一部分至主进料中而加以调节。用本发明提供的工艺可以同时生产两种不同级别的石油焦：普通焦和优质焦。An improved coking process with a two-way feed system, which uses two systems of main feed and auxiliary feed, sharing a fractionation tower. When the heating furnace tube of the auxiliary feed system is coked, a part of the main feed enters The fractionation tower is shared to maintain normal operation; when the raw material saturation of the main feed system is greater than 40% by weight, a part of the heavy distillate oil in the fractionation tower is circulated to the main feed for adjustment. The process provided by the invention can simultaneously produce two different grades of petroleum coke: ordinary coke and high-quality coke.
Description
本发明属于一种改进的延迟焦化工艺，更具体地说，是一种具有两路进料系统的焦化工艺。The invention belongs to an improved delayed coking process, more specifically, a coking process with a two-way feeding system.
延迟焦化是渣油深度加工较理想的工艺，它具有投资省、流程简单、技术成熟、渣油转化率高等特点，它不但能大幅度提高炼厂轻质油收率，它的副产品石油焦还是炼铝、生产石墨电极以及其他碳素制品的重要原料，在国外50％以上的渣油都是通过延迟焦化转化的。Delayed coking is an ideal process for deep processing of residual oil. It has the characteristics of low investment, simple process, mature technology, and high conversion rate of residual oil. It can not only greatly increase the yield of light oil in refineries, but its by-product petroleum coke is also An important raw material for aluminum smelting, production of graphite electrodes and other carbon products, more than 50% of residual oil in foreign countries is converted by delayed coking.
为了更好地发挥延迟焦化的作用以提高炼厂的经济效益，CN101416B公开了一种具有两路进料系统的渣油延迟焦化工艺，该发明是共用一个分馏塔的两套常规延迟焦化装置，一套延迟焦化装置的原料为普通的减压渣油即主进料系统，原料经换热后直接进入一个加热炉加热，然后进入生产普通焦的焦炭塔进行焦化反应，反应后的焦化油气由焦炭塔顶进入共用的分馏塔。另一套延迟焦化装置的目的产物为优质石油针状焦(简称优质焦)，即副进料系统，其原料为选自热裂化渣油、催化裂化澄清油、乙烯焦油和糠醛抽出油中的一种或一种以上的混合物，原料经换热后进入共用的分馏塔下部，与分馏塔中的重馏分油混合换热后进入另一加热炉的辐射段加热，再进入生产优质焦的焦炭塔，反应生成的焦化油气进入与主进料系统共用的分馏塔，因此主进料系统无重馏分油循环，而主、副进料系统反应物的重馏分油都在副进料系统中循环。In order to better play the role of delayed coking to improve the economic benefits of the refinery, CN101416B discloses a residue delayed coking process with a two-way feed system. This invention is two sets of conventional delayed coking devices sharing a fractionation tower. The raw material of a set of delayed coking unit is ordinary vacuum residue, which is the main feed system. After heat exchange, the raw material directly enters a heating furnace for heating, and then enters the coke tower for the production of ordinary coke for coking reaction. The coked oil gas after the reaction is produced by The top of the coke column enters the shared fractionation column. The target product of another delayed coking unit is high-quality petroleum needle coke (referred to as high-quality coke), that is, the auxiliary feed system, and its raw material is selected from thermal cracking residue, catalytic cracking clarified oil, ethylene tar and furfural extracted oil. One or more than one mixture, the raw material enters the lower part of the shared fractionation tower after heat exchange, mixes with the heavy distillate oil in the fractionation tower for heat exchange, then enters the radiation section of another heating furnace for heating, and then enters the coke for producing high-quality coke Tower, the coke oil gas generated by the reaction enters the fractionation tower shared with the main feed system, so there is no heavy distillate oil circulation in the main feed system, while the heavy distillate oil of the reactants of the main and auxiliary feed systems are circulated in the auxiliary feed system .
CN101416B的流程见附图1，其优点是：The flow process of CN101416B is shown in accompanying drawing 1, and its advantage is:
1、由于主、副进料系统反应物的重馏分油都进入副进料系统，因此可扩大生产优质石油焦的原料来源；1. Since the heavy distillates of the reactants of the main and auxiliary feed systems all enter the auxiliary feed system, the source of raw materials for the production of high-quality petroleum coke can be expanded;
2、当副进料系统缺少原料时，副进料系统也可用普通的减压渣油做原料，此时由于只有副进料系统有重馏分油循环，而主进料系统没有重馏分油循环，整个装置的循环比将降低，有利于提高装置的液体产品收率。2. When the auxiliary feed system lacks raw materials, the auxiliary feed system can also use ordinary vacuum residue as raw material. At this time, only the auxiliary feed system has heavy distillate oil circulation, while the main feed system does not have heavy distillate oil circulation. , the circulation ratio of the whole device will be reduced, which is beneficial to improve the liquid product yield of the device.
但该发明也有以下的缺点：But this invention also has following shortcoming:
1、副进料系统生产优质石油焦时，从加热炉出来的焦化原料温度不是恒定的，而是在430～510℃间变化，这样变温操作使得焦炭塔和分馏塔的温度和热量随之变化，因此常有焦粉带入分馏塔并与重馏分油一起进入副进料系统加热炉而使副进料加热炉容易结焦，当副进料加热炉结焦后，副进料不能进入分馏塔，分馏塔中相当一部分热量不能通过副进料而带出分馏塔，分馏塔的热平衡无法维持，因而主进料系统也无法操作；1. When the auxiliary feed system produces high-quality petroleum coke, the temperature of the coking raw material coming out of the heating furnace is not constant, but changes between 430 and 510°C. Such variable temperature operation makes the temperature and heat of the coke tower and fractionation tower change accordingly , so coke powder is often brought into the fractionation tower and enters the auxiliary feed system heating furnace together with the heavy distillate oil, which makes the auxiliary feed heating furnace easy to coke. When the auxiliary feed heating furnace is coked, the auxiliary feed cannot enter the fractionation tower. A considerable part of the heat in the fractionation tower cannot be taken out of the fractionation tower through the auxiliary feed, and the heat balance of the fractionation tower cannot be maintained, so the main feed system cannot be operated;
2、在延迟焦化中，反应主要在焦炭塔中进行，在焦炭塔中进行的反应大致可分为烃类的热裂化反应及芳烃的热缩合反应，而芳烃的缩合反应为放热反应。当延迟焦化处理某些芳烃含量低的原料时，在焦炭塔中进行的反应以烃类的热裂化反应为主，由于反应需吸收大量热量，因此焦炭塔很难保持在要求的温度下操作，当焦炭塔温度低于要求温度，焦化反应不能完全进行，此时会产生软焦，不但使除焦操作难于进行，而且也影响焦炭质量。2. In delayed coking, the reaction is mainly carried out in the coke tower. The reaction in the coke tower can be roughly divided into thermal cracking reaction of hydrocarbons and thermal condensation reaction of aromatic hydrocarbons, and the condensation reaction of aromatic hydrocarbons is an exothermic reaction. When delayed coking is used to treat some raw materials with low aromatic content, the reaction in the coke tower is mainly the thermal cracking reaction of hydrocarbons. Since the reaction needs to absorb a large amount of heat, it is difficult to maintain the coke tower at the required temperature. When the temperature of the coke tower is lower than the required temperature, the coking reaction cannot be carried out completely, and soft coke will be produced at this time, which not only makes the decoking operation difficult, but also affects the coke quality.
本发明的目的是在现有技术的基础上提供一种改进的具有两路进料系统的焦化工艺，即在副进料系统的加热炉结焦后，共用分馏塔的热平衡不致受到破坏，主进料系统仍能维持正常操作；当主进料系统的原料饱和份大于40重％时，除焦操作及焦炭质量仍不会受到影响。The purpose of the present invention is to provide an improved coking process with a two-way feed system on the basis of the prior art, that is, after the heating furnace of the auxiliary feed system is coked, the heat balance of the shared fractionation tower will not be damaged, and the main feed system will not be damaged. The feed system can still maintain normal operation; when the raw material saturation of the main feed system is greater than 40% by weight, the decoking operation and coke quality will not be affected.
本发明提供的工艺包括主进料、副进料两路进料系统、四个焦炭塔和一个共用分馏塔，当副进料系统的加热炉发生炉管结焦时，主进料的一部分进入分馏塔下部，分馏塔底的重馏分油进入缓冲罐与其余的主进料一起经主进料系统加热炉的辐射段预热后，在焦炭塔中生产普通焦；当主进料系统的原料饱和份大于40重％时，分馏塔底重馏分油的一部分进入缓冲罐与其余的主进料一起经主进料系统加热炉的辐射段预热后，在焦炭塔中生产普通焦，副进料系统仍生产优质焦；在副进料系统的加热炉发生炉管结焦，同时主进料系统的原料饱和份大于40重％的情况下，主进料的一部分进入分馏塔，分馏塔底的重馏分油进入缓冲罐与其余的主进料一起经主进料系统加热炉的辐射段预热后，在焦炭塔中生产普通焦。The process provided by the invention includes a two-way feed system for main feed and auxiliary feed, four coke towers and a shared fractionation tower. When coking of the furnace tube occurs in the heating furnace of the auxiliary feed system, a part of the main feed enters the fractionation In the lower part of the tower, the heavy distillate oil at the bottom of the fractionating tower enters the buffer tank together with the rest of the main feed and is preheated by the radiant section of the heating furnace of the main feed system to produce ordinary coke in the coke tower; when the raw material saturation of the main feed system When it is greater than 40% by weight, a part of the heavy distillate at the bottom of the fractionation tower enters the buffer tank and the rest of the main feed is preheated by the radiation section of the heating furnace of the main feed system, and then ordinary coke is produced in the coke tower, and the auxiliary feed system High-quality coke is still produced; when furnace tube coking occurs in the heating furnace of the auxiliary feed system, and the raw material saturation content of the main feed system is greater than 40% by weight, a part of the main feed enters the fractionation tower, and the heavy fraction at the bottom of the fractionation tower After the oil enters the buffer tank and the rest of the main feed is preheated by the radiation section of the main feed system heating furnace, ordinary coke is produced in the coke tower.
本发明提供的工艺是这样具体实施的：Technology provided by the invention is implemented like this:
主进料系统：Main feed system:
主进料进入该系统的加热炉对流段加热后通过缓冲罐进入加热炉的辐射段，加热至495～505℃进入该系统的焦炭塔以生产普通焦，同时焦化油气进入分馏塔分离得到焦化气、焦化汽油、焦化柴油、焦化蜡油。The main feed enters the convection section of the heating furnace of the system to be heated and then enters the radiation section of the heating furnace through the buffer tank, and is heated to 495-505°C and enters the coke tower of the system to produce ordinary coke. , Coker gasoline, coker diesel oil, coker wax oil.
当主进料系统的原料饱和份大于40重％时，分馏塔底部的一部分焦化重馏分油进入缓冲罐与主进料混合，主进料系统的循环比可根据需要加以调节。When the raw material saturation of the main feed system is greater than 40% by weight, a part of the coked heavy distillate at the bottom of the fractionation tower enters the buffer tank to be mixed with the main feed, and the circulation ratio of the main feed system can be adjusted as required.
副进料系统：Vice feed system:
副进料进入该系统的加热炉对流段加热后进入分馏塔，与分馏塔底部的部分焦化重馏分油混合后，进入加热炉的辐射段，加热后进入该系统的焦炭塔以生产优质焦，同时焦化油气进入分馏塔分离得到焦化气、焦化汽油、焦化柴油、焦化蜡油。The auxiliary feed enters the convection section of the heating furnace of the system and enters the fractionation tower after being heated. After being mixed with part of the coking heavy distillate oil at the bottom of the fractionation tower, it enters the radiation section of the heating furnace. After heating, it enters the coke tower of the system to produce high-quality coke. At the same time, the coked oil gas enters the fractionating tower to be separated to obtain coked gas, coked gasoline, coked diesel oil and coked wax oil.
当副进料系统的加热炉发生炉管结焦时，主进料总量的1/5～1/4在温度为100～120℃时进入分馏塔，与焦化油气换热至370～390℃，进入缓冲罐与其余的主进料混合后，送入主进料系统加热炉的辐射段，加热至495～505℃进入主进料系统焦炭塔，以生产普通焦，焦化油气则进入分馏塔分离产品。When coking occurs in the furnace tube of the heating furnace of the auxiliary feed system, 1/5~1/4 of the total amount of main feed enters the fractionation tower at a temperature of 100~120°C, and exchanges heat with coking oil and gas to 370~390°C. After entering the buffer tank and mixing with the rest of the main feed, it is sent to the radiant section of the heating furnace of the main feed system, heated to 495-505°C, and enters the coke tower of the main feed system to produce ordinary coke, and the coke oil gas enters the fractionation tower for separation product.
在副进料系统的加热炉发生炉管结焦，同时主进料系统的原料饱和份大于40重％的情况下，主进料总量的1/5～1/4在温度为100～120℃时进入分馏塔，与焦化油气换热至370～390℃进入缓冲罐，与其余的主进料混合后，送入主进料系统的加热炉辐射段。加热至495～505℃进入焦炭塔以生产普通焦，焦化油气则进入分馏塔分离产品。When the furnace tube coking occurs in the heating furnace of the auxiliary feed system, and the raw material saturation of the main feed system is greater than 40% by weight, 1/5-1/4 of the total amount of the main feed is at a temperature of 100-120°C When it enters the fractionation tower, it exchanges heat with coke oil and gas to 370-390°C and enters the buffer tank. After mixing with the rest of the main feed, it is sent to the radiant section of the heating furnace of the main feed system. It is heated to 495-505°C and enters the coke tower to produce ordinary coke, and the coke oil gas enters the fractionation tower to separate products.
本发明的优点在于：当两路进料系统中的副进料系统加热炉炉管结焦后，主进料的一部分可进入共用分馏塔，使分馏塔的热平衡能维持正常，使主进料系统仍能平稳操作；而当主进料系统的原料饱和份大于40重％时，共用分馏塔的重馏分油可循环一部分至主进料中而加以调节。用本发明提供的工艺可以同时生产两种不同级别的石油焦：普通焦和优质焦。The advantage of the present invention is that: when the heating furnace tube of the auxiliary feed system in the two-way feed system is coked, a part of the main feed can enter the shared fractionation tower, so that the heat balance of the fractionation tower can be maintained normally, and the main feed system It can still operate smoothly; and when the raw material saturation of the main feed system is greater than 40% by weight, a part of the heavy distillate oil in the common fractionation tower can be circulated to the main feed for adjustment. The process provided by the invention can simultaneously produce two different grades of petroleum coke: ordinary coke and high-quality coke.
附图1是现有技术CN101416B的具有两路进料系统的焦化工艺流程示意图。Accompanying drawing 1 is the schematic flow chart of the coking process with two-way feed system of the prior art CN101416B.
附图2是本发明提供的改进的具有两路进料系统的焦化工艺流程示意图。Accompanying drawing 2 is the schematic flow chart of the improved coking process with a two-way feed system provided by the present invention.
附图中各编号说明如下：The descriptions of each number in the accompanying drawings are as follows:
1、2、3、4均代表焦炭塔，5为分馏塔，6为缓冲罐，7、8为加热炉，9、10、11、12、13、14、15、16、17、18均代表管线。1, 2, 3, 4 all represent coke towers, 5 is fractionating tower, 6 is buffer tank, 7, 8 is heating furnace, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18 all represent pipeline.
下面结合附图2来描述本发明所提供的工艺的具体实施方式。The specific implementation of the process provided by the present invention will be described below in conjunction with FIG. 2 .
主进料系统：Main feed system:
来自管线12的主进料进入加热炉8的对流段，加热后进入缓冲罐6，经管线16进入加热炉8的辐射段，加热至495～505℃进入焦炭塔1或2以生产普通焦，同时焦化油气经管线17进入分馏塔5，分离得到焦化气、焦化汽油、焦化柴油、焦化蜡油。The main feed from the
当主进料系统的原料饱和份大于40重％时，分馏塔5底部的一部分焦化重馏分油依次经管线9、10进入缓冲罐6而与主进料混合，主进料系统的循环比可根据需要加以调节。When the raw material saturation of the main feed system was greater than 40% by weight, a part of the coked heavy distillate oil at the bottom of the
副进料系统：Vice feed system:
来自管线11的副进料经管线14进入加热炉7的对流段，加热后经管线18进入分馏塔5，与分馏塔5底部的部分焦化重馏分油混合后，经管线9进入加热炉7的辐射段，加热后进入焦炭塔3或4以生产优质焦，同时焦化油气经管线17进入分馏塔5，分离得到焦化气、焦化汽油、焦化柴油、焦化蜡油。The auxiliary feed from the pipeline 11 enters the convection section of the
当副进料系统加热炉7的炉管结焦时，主进料总量的1/5～1/4在温度为100～120℃时依次经管线13、14、15进入分馏塔5，与焦化油气换热至370～390℃，依次经管线9、10进入缓冲罐6，与其余的主进料混合后，送入主进料加热炉8的辐射段。加热至495～505℃进入焦炭塔1或2生产普通焦，焦化油气则经管线17进入分馏塔5。When the furnace tube of the
在副进料系统的加热炉7发生炉管结焦，同时主进料系统的原料饱和份大于40重％的情况下，主进料总量的1/5～1/4在温度为100～120℃时依次经管线13、14、15进入分馏塔5，与焦化油气换热至370～390℃，依次经管线9、10进入缓冲罐6，与其余的主进料混合后，送入主进料加热炉8的辐射段。加热至495～505℃进入焦炭塔1或2生产普通焦，焦化油气则经管线17进入分馏塔5。In the
Claims (5)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 98117810 CN1115375C (en) | 1998-08-27 | 1998-08-27 | Improved coking process with two-channel feed system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 98117810 CN1115375C (en) | 1998-08-27 | 1998-08-27 | Improved coking process with two-channel feed system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1246513A CN1246513A (en) | 2000-03-08 |
| CN1115375C true CN1115375C (en) | 2003-07-23 |
Family
ID=5225724
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 98117810 Expired - Lifetime CN1115375C (en) | 1998-08-27 | 1998-08-27 | Improved coking process with two-channel feed system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1115375C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015016804A1 (en) * | 2012-11-01 | 2015-02-05 | Fluor Technologies Corporation | Multiple drum coking system |
| US9852389B2 (en) | 2012-11-01 | 2017-12-26 | Fluor Technologies Corporation | Systems for improving cost effectiveness of coking systems |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115873631B (en) * | 2021-08-27 | 2024-12-06 | 中国石油化工股份有限公司 | Delayed coking method and device |
-
1998
- 1998-08-27 CN CN 98117810 patent/CN1115375C/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015016804A1 (en) * | 2012-11-01 | 2015-02-05 | Fluor Technologies Corporation | Multiple drum coking system |
| US9852389B2 (en) | 2012-11-01 | 2017-12-26 | Fluor Technologies Corporation | Systems for improving cost effectiveness of coking systems |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1246513A (en) | 2000-03-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR101712238B1 (en) | Process for delayed coking of whole crude oil | |
| US5350503A (en) | Method of producing consistent high quality coke | |
| CN102482586A (en) | An Effective Method to Improve the Quality of Coking Gas Oil | |
| RU2686152C1 (en) | Method of producing oil needle coke | |
| KR20000064658A (en) | How to increase the liquid product yield in delayed coke manufacturing process | |
| KR101811676B1 (en) | Purification device for naphtha and purification method for naphtha using the same | |
| JP6357202B2 (en) | Delayed coking process using pre-cracking reactor | |
| CN102234531A (en) | A kind of device and application of heavy oil zone catalytic cracking | |
| CN1115375C (en) | Improved coking process with two-channel feed system | |
| US3878088A (en) | Integrated production of olefins and coke | |
| CN113755211B (en) | Method for producing needle coke by using raw material containing optimized ethylene tar | |
| US20210171835A1 (en) | Coking system and coking process | |
| RU2314333C1 (en) | Method of speeded down carbonization | |
| CN106147879A (en) | A kind of rapid pyrolysis oil gas processing system and method | |
| RU2729191C1 (en) | Method for producing oil needle coke | |
| US2294126A (en) | Method of treating a plurality of hydrocarbon oils for subsequent cracking | |
| RU2689634C1 (en) | Method of two-stage thermal cracking with multi-stage separation system | |
| GB2083492A (en) | Production of pitch from petroleum fractions | |
| RU2717815C1 (en) | Method of producing oil needle coke | |
| NO138150B (en) | PROCEDURE FOR PREPARING COKE WITH ELECTRODE QUALITY | |
| CN87102308A (en) | Residual Oil Coking Process with Two-way Feed System | |
| RU2825280C1 (en) | Method of producing highly structured petroleum coke | |
| RU2639795C2 (en) | Method of producing low-sulfur petroleum coke | |
| RU2786846C1 (en) | Method for producing petroleum needle coke | |
| RU2744637C1 (en) | Delayed coking process for oil residues |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20030723 |
|
| CX01 | Expiry of patent term |