CN1461793A - Method of removing fine coke from coking oil gas - Google Patents
Method of removing fine coke from coking oil gas Download PDFInfo
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- CN1461793A CN1461793A CN 02120778 CN02120778A CN1461793A CN 1461793 A CN1461793 A CN 1461793A CN 02120778 CN02120778 CN 02120778 CN 02120778 A CN02120778 A CN 02120778A CN 1461793 A CN1461793 A CN 1461793A
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- oil
- coking
- coke powder
- pyrogenic reaction
- gas
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A process for removing coke powder from the coking oil gas features that the raw coking oil is introduced to the lower part of evaporting segment in coking fractional tower via two ways, after it is mixed with the coking oil vapour containing coke powder the mixture comes in upper segment for separating the coke powder, and the separated coke powder along with raw oil and circulating oil is delivered to heater and coking tower. A nozzle is used for atomizing part of the raw material. Its advantage is high effect up to 75-99.9%.
Description
Technical field
The present invention relates to a kind of method that removes coke powder in the coker, more particularly, is a kind of coke powder method that coking oil gas carries that removes.
Background technology
Delayed coking is effective economical means of the heavy poor residuum of a kind of refinery's processing, is subjected to people and generally payes attention to.At present, domestic coker obtains aspect such as optimum economic benefit and generally faces the problem of improving technical level in device maximization, long period, Optimizing operation.The technology that relates to has low circulation or ultralow recycle ratio coking technology, shortens coking tower operational cycle technology, online coke cleaning technology etc., and coker removes the integral part that the coke powder technology is low recycle ratio technology.Reduction along with the operation cycle ratio, separation column evaporator section gas volume increases, the linear speed height, the liquid phase load reduces simultaneously, cause washing coke powder deleterious, generally run into coker gas oil even coker gasoline, the diesel oil overhead product carries the coke powder phenomenon, the expansion of the existing coker of the serious restriction of this problem can be operated.
Existing coker adopts the method for washing to remove coke powder, promptly establish 2～5 wash plate at evaporator section, float valve or solid tongue are housed on the plate, have 15%～17% valve opening on the plate, contain that valve opening passes fast with 3.5～4.0m/s gas speed on the oil gas slave plate of 0.01%～0.1% coke powder, have 50～80mm liquid level to keep fluid-tight on the plate, carrying out liquid phase is that external phase, gas phase are the vapour-liquid heat and mass transfer process of disperse phase.In low recycle ratio even single-pass operation process, liquid-vapour ratio is very little, can not form effective fluid-tight layer on the plate, because gas via hole speed is big, cause forming air pocket, reduced the abundant touch opportunity of vapour-liquid, influenced its heat and mass effect at the valve opening place, make the part coke powder be carried to tower top, overhead product band coke powder phenomenon occurs.The coking overhead product carries coke powder, has a strong impact on the course of processing thereafter, as influencing vapour, diesel oil hydrofining device operational cycle and tooling cost, influences catalytic cracking unit operation operating mode and liquid and receives, and reduces economic benefit.
USP4,549,934 relate to a kind of coking, in the evaporating area of separation column, light coker gas oil or heavy coker gas oil are sprayed by nozzle, directly contact with the high-temperature-coked oil gas that rises, establish packing section in the evaporating area, advance process furnace with raw material being used as turning oil under the heavy coker gas oil condensation in the high-temperature-coked oil gas.But there is following practical problems in this patent: device allows as the light coker gas oil or the heavy coker gas oil of coke powder washing oil very limitedly in low circulation or ultralow cyclical operation, and specific liquid rate is little, generally 0.5～5.0m only
3/ hm
2, washing effect is undesirable; Be to improve specific liquid rate, certainly will extract the heavy coker gas oil of a certain amount of band coke powder out, the heavy coker gas oil following process that contains a large amount of coke powders is very difficult, its most reliable processing means or coking, so this process too big actual value of nothing that becomes; For improving specific liquid rate, also can adopt the washing oil circulation, but the washing oil boiling range after the balance is generally 450 ℃～650 ℃ even heavier, and carry a large amount of coke powders, under evaporating area high temperature (410 ℃～425 ℃), the easy coking and blocking of pipeline and filler, circulating oil pump operation operating mode is very abominable, can't realize the long period operation.
USP5,645,711 relate to a kind of coking, coke powder in light coker gas oil that separation column is extracted out or the heavy coker gas oil filtering and removing oil product, but must filter coking distillate by the independent filtration unit of a newly-built cover, just can carry out following process.
Summary of the invention
The purpose of this invention is to provide a kind of coke powder method that coking oil gas carries that in coker, removes.
Technical scheme of the present invention is: the raw material oil content enters coking fractional distillation column evaporator section bottom for two strands, one inlet is below pyrogenic reaction oil gas advances the separation column inlet, another strand injects on the pyrogenic reaction gas pipeline, with enter after the coking oil gas that contains coke powder mixes separation column evaporator section top from, the coke powder of deviating from comes along process furnace, coke drum with stock oil, turning oil.
The present invention adopts nozzle that washing lotion is atomized into small-particle, improves the vapour-liquid contact area, has also strengthened the vapour-liquid heat and mass transfer process, improves the coke powder washing effect.The present invention can remove in the pyrogenic reaction oil gas 75～99.9% coke powder.
Description of drawings
Accompanying drawing is the method synoptic diagram that removes coke powder in the coking oil gas provided by the invention.
Embodiment
Technical scheme of the present invention is: the coking raw material oil content enters coking fractional distillation column evaporator section bottom for two strands, one inlet is below pyrogenic reaction oil gas advances the separation column inlet, another strand injects on the pyrogenic reaction gas pipeline, with enter after the coking oil gas that contains coke powder mixes separation column evaporator section top from, the coke powder of deviating from comes along process furnace, coke drum with stock oil, turning oil.
Coking raw material oil on the injection pyrogenic reaction gas pipeline accounts for 5～60 weight % that account for the coker combined feed total feed of device combined feed total feed.
The present invention adopts 1～8 nozzle that stock oil is sprayed in the pyrogenic reaction gas pipeline, and nozzle is uniform distribution on reaction oil gas pipeline outer circumference.Stock oil adopts 0～50% water vapour to atomize in nozzle sprays into pyrogenic reaction oil gas pipe, when not having water vapour, is the power atomizing.The pressure that stock oil enters nozzle is 0.30～2.0MPa, and the stock oil in the pipe after the atomizing is fan-shaped or conical and contacts with pyrogenic reaction oil gas vapour-liquid, and the atomizing particle granularity is 40～120 μ m.
Stock oil injects on the pyrogenic reaction gas pipeline, mix after gas pipeline advances the tower inlet below washing section with pyrogenic reaction oil gas, it is that vertical direction enters or tangential direction enters that the pyrogenic reaction gas pipeline advances tower, and stock oil decanting point to pyrogenic reaction gas pipeline advances tower inlet distance 0～80 times for pyrogenic reaction gas pipeline external diameter.
At present, the stock oil of industrial coker also is that two strands of branches enter coking fractional distillation column evaporator section bottom, wherein one inlet is also below pyrogenic reaction oil gas advances the separation column inlet, but another strand is above pyrogenic reaction oil gas advances the separation column inlet, rather than inject on the pyrogenic reaction gas pipeline, coke powder does not have any help in coking oil gas to removing for this.
The present invention adopts nozzle that washing lotion is atomized into small-particle, improves the vapour-liquid contact area, has also strengthened the vapour-liquid heat and mass transfer process, improves the coke powder washing effect.The present invention can remove in the pyrogenic reaction oil gas 75～99.9% coke powder.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.
Accompanying drawing is the method synoptic diagram that removes coke powder in the coking oil gas provided by the present invention.
Coking raw material oil content from pipeline 1 is a two-way, wherein one the tunnel enter the evaporator section bottom of coking fractional distillation column 6 through pipeline 2, another road contacts with pyrogenic reaction oil gas from pipeline 4 through pipeline 3, after nozzle atomization, be fan-shaped or conical at this place's stock oil, the granularity of atomizing particle is 40～120 μ m, the stock oil atomizing particle mixes with pyrogenic reaction oil gas after pipeline 5 enters the evaporator section bottom of coking fractional distillation column 6, this inlet at stock oil above pipeline 2 is gone into the separation column place, the coking oil gas that removes coke powder enter separation column evaporator section top from, the coke powder of deviating from is with stock oil, turning oil removes process furnace through pipeline 7 together, coke drum.
Method advantage provided by the invention is: the present invention adopts nozzle that washing lotion is atomized into small-particle, improves the vapour-liquid contact area, has also strengthened the vapour-liquid heat and mass transfer process, improves the coke powder washing effect.The present invention can remove in the pyrogenic reaction oil gas 75～99.9% coke powder.
The following examples will give further instruction to present method, but therefore not limit present method.
Decoking powder simulation test used medium is: the coke of solid dielectric for pulverizing, and granularity is 20～150 μ m; It is pressurized air that coke powder carries medium, and liquid medium is a fresh water, and test temperature is a normal temperature, and test pressure is approximate normal pressure.Experiment is the analoging industrial device operating conditions.Adopt the conventional valve disc washing in the tower, wherein the conventional valve disc washing column adopts Φ 80*600 synthetic glass king-post, and king-post is established one deck sieve aperture tower tray, opens 4 Φ 10 holes, and Ta Bishang has overflow port, and tower tray is held the above liquid level of 50mm when keeping operational stage.Thereby calculate the coke powder extrusion rate by remaining coke powder amount in the gas after the quantitative assay washing, test-results sees Table 1.
Comparative Examples
Fresh moisture two-way enters the washing king-post in the above and below that the pressurized air that contains coke powder is gone into the tower place respectively.Outside tower, do not atomize as the fresh water of washing liq, do not contact with the pressurized air that contains coke powder yet; In tower, adopt the conventional valve disc washing.
Embodiment
Fresh moisture two-way, wherein 50 weight % directly enter the washing king-post, remain 50 weight % different with Comparative Examples be, contact with the pressurized air that contains coke powder after under 0.3MPa, being atomized into the particle of 40～120 μ m, enter the washing king-post again.In tower, also adopt the conventional valve disc washing.
As can be seen from Table 1, the coke powder extrusion rate is 67.27% only in the Comparative Examples, and the coke powder extrusion rate is then up to 99.55% in the present embodiment.
Table 1
| Comparative Examples | Embodiment | |
| The void tower linear speed, m/s | ????0.5 | ????0.5 |
| The via hole linear speed, m/s | ????7.5 | |
| Kinetic energy factor, m/s (g/cm 3) 0.5 | ????8.5 | |
| Washing water account for gas volume, weight % | ????35 | ????35 |
| Coke powder inlet content, g/m 3 | ????0.11 | ????0.11 |
| Coke powder outlet content, g/m 3 | ????0.036 | ????0.005 |
| The coke powder extrusion rate, % | ????67.27 | ????99.55 |
Claims (5)
1, a kind of method that removes coke powder in the coking oil gas, it is characterized in that two strands of coking raw material oil contents enter coking fractional distillation column evaporator section bottom, one inlet is below pyrogenic reaction oil gas advances the separation column inlet, another strand injects on the pyrogenic reaction gas pipeline, with enter after the coking oil gas that contains coke powder mixes separation column evaporator section top from, the coke powder of deviating from comes along process furnace, coke drum with stock oil, turning oil.
2,, it is characterized in that injecting 5～60 weight % that account for the coker combined feed total feed that coking raw material oil on the pyrogenic reaction gas pipeline accounts for the device combined feed total feed according to the method for claim 1.
3,, it is characterized in that stock oil adopts 0～50% water vapour to atomize in nozzle sprays into pyrogenic reaction oil gas pipe according to the method for claim 1.
4, according to the method for claim 1, it is characterized in that the pressure that stock oil enters nozzle is 0.30～2.0MPa, the stock oil in the pipe after the atomizing is fan-shaped or conical and contacts with pyrogenic reaction oil gas vapour-liquid, and the atomizing particle granularity is 40～120 μ m.
5, according to the method for claim 4, its feature is advanced tower inlet distance 0～80 times for pyrogenic reaction gas pipeline external diameter at stock oil decanting point to pyrogenic reaction gas pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02120778 CN1208427C (en) | 2002-05-31 | 2002-05-31 | Method of removing fine coke from coking oil gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02120778 CN1208427C (en) | 2002-05-31 | 2002-05-31 | Method of removing fine coke from coking oil gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1461793A true CN1461793A (en) | 2003-12-17 |
| CN1208427C CN1208427C (en) | 2005-06-29 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02120778 Expired - Lifetime CN1208427C (en) | 2002-05-31 | 2002-05-31 | Method of removing fine coke from coking oil gas |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101892065A (en) * | 2010-01-10 | 2010-11-24 | 何巨堂 | Coal tar processing method |
| CN101987961A (en) * | 2009-07-30 | 2011-03-23 | 中国石油化工股份有限公司石油化工科学研究院 | Coking delaying method |
| WO2012167513A1 (en) * | 2011-06-10 | 2012-12-13 | 济南世纪华泰科技有限公司 | A dedusting process and device for oil-air mixture |
| CN103224808A (en) * | 2013-01-10 | 2013-07-31 | 上海河图工程股份有限公司 | Inferior heavy oil fluidization conversion technology |
-
2002
- 2002-05-31 CN CN 02120778 patent/CN1208427C/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101987961A (en) * | 2009-07-30 | 2011-03-23 | 中国石油化工股份有限公司石油化工科学研究院 | Coking delaying method |
| CN101892065A (en) * | 2010-01-10 | 2010-11-24 | 何巨堂 | Coal tar processing method |
| CN101892065B (en) * | 2010-01-10 | 2013-08-28 | 何巨堂 | Coal tar processing method |
| WO2012167513A1 (en) * | 2011-06-10 | 2012-12-13 | 济南世纪华泰科技有限公司 | A dedusting process and device for oil-air mixture |
| CN103224808A (en) * | 2013-01-10 | 2013-07-31 | 上海河图工程股份有限公司 | Inferior heavy oil fluidization conversion technology |
| CN103224808B (en) * | 2013-01-10 | 2015-04-22 | 上海河图工程股份有限公司 | Inferior heavy oil fluidization conversion technology |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1208427C (en) | 2005-06-29 |
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