CN1276963C - High-yield chemical light oil delayed coking method - Google Patents
High-yield chemical light oil delayed coking method Download PDFInfo
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- CN1276963C CN1276963C CN 03149945 CN03149945A CN1276963C CN 1276963 C CN1276963 C CN 1276963C CN 03149945 CN03149945 CN 03149945 CN 03149945 A CN03149945 A CN 03149945A CN 1276963 C CN1276963 C CN 1276963C
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Abstract
The present invention relates to a high-yield chemical light oil delayed coking method. Raw oil and circulation oil enter a heating furnace, are heated to a coking temperature and enter a coking tower. Oil gas generated in a cracking reaction enters a fractionating tower for fractionating gas, gasoline, diesel oil, wax oil and circulation oil, wherein the circulation oil and the raw oil enter the heating furnace, coke generated by condensation is gathered in the coke tower, and the coke is characterized in that the gauge pressure on the coking tower top is 0.2 to 2.0MPa. The method makes use of vacuum residue, etc. as raw materials so as to produce chemical industry light oil, and the method has higher yield of the chemical industry light oil than conventional coking. Compared with major cycle ratio coking, the method has equivalent chemical industry light oil yield, the processing capability of coking devices is relatively increased by more than 40%, and the unit energy consumption of the raw materials is reduced by more than 10%.
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 of more producing chemical industry light oil.
Background technology
Because the crude oil in China cut is laid particular stress on, the lighting end proportion is less, and virgin naphtha and solar oil yield are about about 30m%, and the raw material major part that offers ethylene unit is solar oil and petroleum naphtha, and lighter hydrocarbons seldom.Simultaneously, the refinery of China is for the production that guarantees aromatic hydrocarbon product and stop bracket gasoline and the production of high-grade derv fuel oil, satisfy the market requirement of the light-weight fuel oil that constantly enlarges, must consume a large amount of straight run lightweight oils, like this, formed the situation that steam cracking and oil refining complete processing are striven the straight run lightweight oil altogether.
The pyrogenic reaction of hydrocarbon compound belongs to free radical reaction, the reaction of isomerization and hydrogen transference seldom, thereby the cracked product is mainly straight-chain paraffin, its gasoline component octane value is very low, seldom as the gasoline blend component.Though coking light ends oil contains a large amount of straight chain hydrocarbon, not good motor spirit, as the raw material of steam pyrolysis production ethene, ethylene yield is but very high, is the high quality raw material of producing ethene.
Residual oil accounts for about 40m% in the crude oil in China, and the source is wide, low price.Delay coking process adopts residual oil as raw material, and the total working ability of delayed coking has surpassed 2000 * 104t/a, will generate the lightweight oil of about 300 * 104t/a like this, provides good source for enlarging the cracking of ethylene raw material.The application delay coking process makes the residual oil lighting produce the cracking of ethylene raw material, will effectively alleviate the situation of ethylene raw anxiety, promotes the development of ethylene industry.
Delayed coking is a kind of sophisticated, heavy oil conversion technology of being widely used.It is the heat processing technique that the residual oil of low value is converted into distillate, gas and the byproduct coke of high value through drastic cracking.The delay coking process process is that stock oil enters separation column after the process furnace heating, the oil gas heat exchange next with coke drum, enter the process furnace radiation section with turning oil again and be heated to coking temperature, thermally splitting and condensation reaction take place after entering coking tower in high-temperature material, the oil gas that cracking reaction produces enters separation column and fractionates out gas, gasoline, diesel oil, wax oil and turning oil, the coke that condensation produces accumulates in the coke drum, when coking tower is full of coke, the pyrogenic reaction material switches to the another one coke drum and continues operation, and coke drum originally cools off the decoking operation.The operational condition of conventional delayed coking is: coking tower top pressure 0.15～0.20MPa, recycle ratio 0.3～0.4,495～505 ℃ of furnace outlet temperature.
In order to improve the coking liquid product yield, US5645712A and CN85103235A propose to adopt the lighter hydrocarbons dilution component of using " non-coking " to improve the temperature of reaction of liquid hydrocarbon in the coking tower, the flow process scope of light hydrocarbon component is generally at 168～454 ℃, be preferably 265～343 ℃ of diesel components, light constituent and material rate are 0～1.0 to be preferably 0.1～0.2, make the interior temperature of coke drum improve 2.8～8.3 ℃ at last, improve liquid product yield, reduce coking yield, this method need increase process furnace and various power-equipment, increase energy consumption.The liquid product that this method increases mainly is the wax oil component, is not suitable for as the raw material of producing ethene.
In order to improve the chemical industry light oil yield, CN1087665A proposes to be produced by residual oil the method for ethylene raw oil, by wax tailings circulation and cracking again, makes residual oil except that a part is converted into the refinery coke of by-product, and the overwhelming majority all is converted into the stock oil of producing ethene.The shortcoming of this method is the amount that has increased coking recycle oil, and the residual oil working ability that has reduced coker maybe needs newly-increased furnace apparatus to carry out the wax tailings cracking, and the coker energy consumption is improved.
In order to enlarge the raw material sources of producing ethene, solve the under-supply problem of lightweight oil, US6179993B1 proposes a method that is prepared alkene by residual oil raw material, it is characterized in that raw material and mobile solid thermal carriers short-time contact, temperature of reaction is controlled at 760 ℃～790 ℃, the reaction gas phase residence time was less than 0.5 second, and the solid carrier residence time is 5～60 seconds.Flow injecting steam in the reaction zone while with 0.2～0.5 pound of steam per pounds raw material.This invention also comprises the steps such as heating, circulation, gas-oil separation and fractionation of solid carrier.Fluidisation short contact reactor is adopted in this invention, technical sophistication, investment operation cost height, and the processing unit technology is immature, and risk is bigger.
Summary of the invention
One of purpose of the present invention provides the delayed coking method that a kind of more producing chemical industry light oil is an ethylene raw, to overcome the deficiencies in the prior art.
Another object of the present invention is to reduce process furnace radiation section inlet amount, reduces the thermal load of stove, and corresponding raising process furnace and radiation fresh feed pump are handled the ability of coking raw material.
The present invention also aims to reduce the internal circulating load of device, reduce process furnace fuel consumption and fresh feed pump flow, to cut down the consumption of energy.
Method provided by the invention comprises:
Stock oil enters with turning oil and enters coking tower after process furnace is heated to coking temperature, coking cat head gauge pressure is 0.2～2.0MPa, the oil gas that cracking reaction produces enters separation column and fractionates out gas, gasoline, diesel oil, wax oil and turning oil, wherein turning oil enters process furnace with stock oil, and the coke that condensation produces accumulates in the coke drum.
This method is utilized raw material production chemical industry light oils such as vacuum residuum, compares with conventional coking, improves the chemical industry light oil yield; Compare than coking with systemic circulation, the chemical industry light oil yield is suitable, but improves the coker processing power relatively more than 40%, makes the raw material unit consumption of energy reduce more than 10%.
Embodiment
Technical scheme provided by the invention is so concrete enforcement:
Coking raw material is delivered to the heating of coking heater convection zone through feedstock pump, the convection zone temperature out is controlled at about 320～380 ℃, advance separation column and the heat exchange of coking cat head oil gas counter current contact then, advance the process furnace radiation section with turning oil at the bottom of the tower, be heated to 485～510 ℃ of coking temperatures, advance coking tower and carry out cracking and condensation reaction, according to property of raw material and coke chemicals distribution requirement, it is that 0.2～2.0MPa is preferably 0.3～1.5MPa that coking cat head gauge pressure is controlled at.Because coking tower pressure improves, the heavy constituent that cracking produces are difficult to volatilization, rest on and proceed secondary cracking in the coking tower, have improved coking raw material at coking dwell time in the tower and cracking level.Coking cat head oil gas composition is compared with conventional delayed coking and is lightened, and the light constituent ratio improves in coke chemicals.Because system pressure improves, hydrocarbon density improves relatively, and the oil gas volume is diminished relatively, has reduced the oil gas linear speed, has improved the device processing power.
Coking cat head oil gas enters separation column and cuts into gas, gasoline (being chemical industry light oil), diesel oil, wax oil, the low wax slop different fractions such as (being turning oil) of tower, and it is that 0.2～2.0MPa is preferably 0.3～1.5MPa that fractionation cat head gauge pressure is controlled at.Because heavy constituent reduce in the coking oil gas, the circulation oil mass is reduced, when keeping identical wax oil yield, the circulation oil mass reduces, and causes the radiation inlet amount to reduce, and has improved the treatment capacity of device relatively.
Because system pressure improves, cooking gas density is improved, the gas compressor inlet pressure improves, and has improved the actual treatment ability of compressor, reduces the energy consumption of compressor unit's gas volume.
Above-described coking raw material comprises long residuum, vacuum residuum, visbreaking residue, fluid catalytic cracking decant oil, hydrocracking tail oil, ethylene bottom oil, lubricating oil extraction oil, deasphalted oil, de-oiled asphalt and two or more the mixing oil of heavy crude and any crude oil.Because the used coking raw material of the present invention is heavy oil, therefore, there is not and produces the problem of motor spirit contention raw material.
The invention has the advantages that and utilize vacuum residuum to produce chemical industry light oil, compare, improve the chemical industry light oil yield with conventional coking; Compare than coking with systemic circulation, the chemical industry light oil yield is suitable, but improves the coker processing power relatively more than 40%, makes the raw material unit consumption of energy reduce more than 10%.
The following examples will give further instruction to present method, but therefore not limit present method.
Comparative Examples 1
It is raw material that this Comparative Examples adopts heavy crude, carries out the coking test under the conventional pressure, and the coking tower top pressure is 0.17MPa, and the coking recycle ratio is that the regular circulation ratio is 0.4.Processing condition and product yield are listed in table 1, and as can be seen from Table 1, the coker gasoline yield only is 13.23 heavy %.
Comparative Examples 2
The raw material of this Comparative Examples is identical with Comparative Examples 1, also carries out the coking test under the conventional pressure, and coking cat head gauge pressure is 0.17MPa, and the coking recycle ratio is that systemic circulation is than 0.92.Processing condition and product yield are listed in table 1, and as can be seen from Table 1, the coker gasoline yield is 16.67 heavy %.
Embodiment 1
The raw material of present embodiment is identical with Comparative Examples 1, and coking cat head gauge pressure is 0.3MPa, and the coking recycle ratio is 0.3.Processing condition and product yield are listed in table 1, and as can be seen from Table 1, the coker gasoline yield is 15.17 heavy %.Compare with Comparative Examples 1, improve the coking tower top pressure, recycle ratio is lower than the regular circulation ratio, and the coker gasoline yield has improved 14.6%.
Embodiment 2
The raw material of present embodiment is identical with embodiment's 1, and coking cat head gauge pressure is 0.7MPa, and the coking recycle ratio still is 0.3.Processing condition and product yield are listed in table 2, and as can be seen from Table 2, the coker gasoline yield is 17.41 heavy %.Compare with Comparative Examples 1, improve the coking tower top pressure, the coker gasoline yield has improved 31.6%; Compare with Comparative Examples 2, the coker gasoline yield is suitable, and than 0.92, the device processing power improves 47% to recycle ratio far below systemic circulation.
Embodiment 3
The raw material of present embodiment is identical with embodiment's 1, and coking cat head gauge pressure is 1.0MPa, and the coking recycle ratio still is 0.3.Processing condition and product yield are listed in table 2, and as can be seen from Table 2, the coker gasoline yield is up to 18.63 heavy %.Compare with Comparative Examples 1, improve the coking tower top pressure, the coker gasoline yield has improved 37.8%; Compare with Comparative Examples 2, the coker gasoline yield is suitable, and than 0.92, the device processing power improves 47% to recycle ratio far below systemic circulation.
Embodiment 4
The raw material of present embodiment is a vacuum residuum, and coking cat head gauge pressure is 1.5MPa, and the coking recycle ratio still is 0.3.Processing condition and product yield are listed in table 3, and as can be seen from Table 3, the coker gasoline yield is up to 19.46 heavy %.
Embodiment 5
The raw material of present embodiment is deasphalted oil, and coking cat head gauge pressure is 2.0MPa, and the coking recycle ratio still is 0.3.Processing condition and product yield are listed in table 3, and as can be seen from Table 3, the coker gasoline yield is up to 21.36 heavy %.
Table 1
| Comparative Examples 1 | Comparative Examples 2 | Embodiment 1 | |
| Raw material | Heavy crude | Heavy crude | Heavy crude |
| Processing condition | |||
| Tower top pressure (table), MPa | 0.17 | 0.17 | 0.3 |
| The furnace outlet temperature, ℃ | 500 | 500 | 500 |
| Recycle ratio | 0.4 | 0.92 | 0.3 |
| Product yield, heavy % | |||
| Gas | 7.51 | 9.43 | 8.54 |
| Gasoline | 13.23 | 16.67 | 15.17 |
| Diesel oil | 35.28 | 43.26 | 37.92 |
| Wax oil | 19.08 | 3.82 | 12.61 |
| Coke | 24.90 | 26.82 | 25.76 |
Table 2
| Embodiment 2 | Embodiment 3 | |
| Raw material | Heavy crude | Heavy crude |
| Processing condition | ||
| Tower top pressure (table), MPa | 0.7 | 1.0 |
| The furnace outlet temperature, ℃ | 500 | 500 |
| Recycle ratio | 0.3 | 0.3 |
| Product yield, heavy % | ||
| Gas | 9.54 | 10.27 |
| Gasoline | 17.41 | 18.63 |
| Diesel oil | 42.45 | 42.82 |
| Wax oil | 4.10 | 1.32 |
| Coke | 26.50 | 26.96 |
Table 3
| Embodiment 4 | Embodiment 5 | |
| Raw material | Vacuum residuum | Deasphalted oil |
| Processing condition | ||
| Tower top pressure (table), MPa | 1.5 | 2.0 |
| The furnace outlet temperature, ℃ | 500 | 500 |
| Recycle ratio | 0.3 | 0.3 |
| Product yield, heavy % | ||
| Gas | 10.53 | 11.21 |
| Gasoline | 19.46 | 21.36 |
| Diesel oil | 42.80 | 38.13 |
| Wax oil | 0 | 0 |
| Coke | 27.21 | 29.30 |
Claims (4)
1, a kind of delayed coking method of more producing chemical industry light oil, stock oil enters with turning oil and enters coking tower after process furnace is heated to coking temperature, the oil gas that cracking reaction produces enters separation column and fractionates out gas, gasoline, diesel oil, wax oil and turning oil, wherein turning oil enters process furnace with stock oil, the coke that condensation produces accumulates in the coke drum, it is characterized in that coking cat head gauge pressure is 0.2～2.0MPa.
2,, it is characterized in that described stock oil is selected from the long residuum of heavy crude and any crude oil, vacuum residuum, visbreaking residue, fluid catalytic cracking decant oil, hydrocracking tail oil, ethylene bottom oil, lubricating oil and extracts one or more mixture among oil, deasphalted oil, the de-oiled asphalt out according to the method for claim 1.
3,, it is characterized in that coking temperature is 485～510 ℃ according to the method for claim 1.
4,, it is characterized in that coking cat head gauge pressure is 0.3～1.5MPa according to the method for claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03149945 CN1276963C (en) | 2003-07-31 | 2003-07-31 | High-yield chemical light oil delayed coking method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03149945 CN1276963C (en) | 2003-07-31 | 2003-07-31 | High-yield chemical light oil delayed coking method |
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| Publication Number | Publication Date |
|---|---|
| CN1580194A CN1580194A (en) | 2005-02-16 |
| CN1276963C true CN1276963C (en) | 2006-09-27 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 03149945 Expired - Lifetime CN1276963C (en) | 2003-07-31 | 2003-07-31 | High-yield chemical light oil delayed coking method |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103421538A (en) * | 2012-05-15 | 2013-12-04 | 中国石油天然气股份有限公司 | Method for adding coking distillate oil into residual oil for hydrogen supply coking |
| CN103215062B (en) * | 2013-05-07 | 2016-01-20 | 山东东明石化集团有限公司 | A kind of delayed coking working method of poor residuum |
| CN104673372B (en) * | 2013-12-02 | 2016-09-14 | 中石化洛阳工程有限公司 | A kind of method improving delayed coking product slates |
| CN105885939A (en) * | 2014-12-15 | 2016-08-24 | 中石化洛阳工程有限公司 | Method for processing deoiled asphalt |
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