CN102899076A - Delayed coking method - Google Patents
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- CN102899076A CN102899076A CN2011102109749A CN201110210974A CN102899076A CN 102899076 A CN102899076 A CN 102899076A CN 2011102109749 A CN2011102109749 A CN 2011102109749A CN 201110210974 A CN201110210974 A CN 201110210974A CN 102899076 A CN102899076 A CN 102899076A
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Abstract
The invention discloses a delayed coking method. The method comprises the following steps: heating mixed heavy oil to 360-450DEG C, carrying out viscosity breaking, carrying out gas-liquid separation of viscosity breaking products, allowing the separated oil gas to enter a fractionating tower, heating the separated viscosity breaking heavy oil to 480-515DEG C, allowing the heated viscosity breaking heavy oil to enter a coking tower, coking, allowing the coked high temperature oil gas to enter a cracking fractionating tower, allowing coking high-temperature oil gas fractionation coking products to be discharged from the cracking fractionating tower, allowing parts of coking fractionating bottom oil to be returned to the cracking fractionating tower and the other parts of the coking fractionating bottom oil to enter a vacuum tower, fractionating, and using the fractionated vacuum residuum as a part of the mixed heavy oil. The method improves the properties of heavy coal gas oil, and alleviates the coking of the fractionating tower bottom and heating furnace tubes.
Description
Technical field
The present invention relates to not exist in the situation of hydrogen, the thermal non-catalytic cracking of hydrocarbon ils, particularly a kind of have viscosity breaking, underpressure distillation and delay coking process to make up the coking process method.
Technical background
Delayed coking be a kind of with heavy oil through degree of depth thermally splitting be converted into gas, light in the heavy oil deep processing technique of matter distillate and coke, the characteristics such as have that the charcoal of taking off is thorough, flow process is simple, technology maturation, plant investment are lower, it has become one of important process in the Heavy Oil Processing Technology.
Pursuing a goal exactly of delayed coking unit is converted into liquid product on lower heavy oil maximum of the condition ground that guarantees production safety and long-term operation, and the recycle ratio of reduction delayed coking unit is one of important method of raising liquid yield.But along with crude oil becomes applying of heavy and decompression deep drawing technology, so that the feed properties of delayed coking unit worse and worse, it is large to be mainly manifested in density, viscosity is high, heavy metal content is high, sulphur content is high, nitrogen content is high, resin and asphalt content is high, although adopt low recycle ratio even one way by improving the yield of liquid product after operating, but mainly be the yield of heavy wax tailings, and the degradation of heavy wax tailings, be mainly manifested in the carbon residue height, coke powder is high, also can accelerate simultaneously the coking of process furnace radiant coil, thereby have influence on the long-term operation of delayed coking unit.
In order to slow down the coking of delayed coker unit furnace boiler tube, improve the liquid product yield of delayed coking unit, and the quality of improving heavy wax tailings, the refining of petroleum investigator has researched and developed the relevant technology such as technique.
US Patent No. 4518487 adds low boiling component to substitute turning oil in charging; Patent US4455219, CN1138843C add thinner in charging; US Patent No. 4784744, US5006223, US4378288 add free radical inhibitors in charging; Chinese patent CN101037618A adds the arene coking inhibitor in coking raw material; Chinese patent CN100457856C adds preferred inhibitor in coking raw material, and sneaks into a certain amount of lower carbon number hydrocarbons (C in the charging of coke drum bottom
1-C
4), and Chinese patent CN1710032A adds anticoking agent etc. in charging.The inhibition that these patents have the coking of heating furnace tube, prolonged on-stream time; The yield that has also improved liquid product that has, the yield of wax tailings especially, but all have emphatically the problems such as wax tailings character is relatively poor, the viscosity that is mainly manifested in heavy wax tailings is large, carbon residue is high.
Chinese patent CN101619237A and CN101619238A are vacuum distillation process and delay coking process combination, improved the liquid product yield of delayed coking unit, improved the character of heavy wax tailings, but the variation of coking heater radiation section feed properties, aggravate the coking of boiler tube, thereby can shorten the on-stream time of device.
Summary of the invention
The method of a kind of delayed coking that the present invention be directed to the deficiencies in the prior art and propose, the method for this delayed coking is with the unit operation of underpressure distillation, viscosity breaking and the delayed coking processing heavy oil that organically combines.Method provided by the invention may further comprise the steps:
1) mixes heavy oil and enter the process furnace heating, to mix heavy oil and be heated to 360～450 ℃, preferred 380～430 ℃, enter visbreaking reactor from the visbreaking reactor bottom, stop 6～210min, preferred 30～120min, visbreaking reactor top gauge pressure is 0.30～3.5Mpa, the viscosity breaking product enters and carries out gas-liquid separation, and isolated oil gas enters coking fractional distillation column, and isolated visbreaker tar enters step 2);
2) from step 1) visbreaker tar be heated to 480 ℃～515 ℃, enter coking tower and carry out pyrogenic reaction, the gauge pressure of coking tower cat head is 0.103～1.0Mpa, preferred 0.103～0.25Mpa, and filling the burnt time is 3～48hr, preferred 6～20hr, the high-temperature oil gas of coking tower enters coking fractional distillation column, and coke chemicals go out device, and an oil part is returned coking fractional distillation column at the bottom of the coking fractional distillation column, another part enters vacuum distillation tower and carries out fractionation, and the vacuum residuum that fractionates out returns step 1 as mixing heavy oil).
The oil depth of cut is 350 ℃～500 ℃ at the bottom of the described coking fractional distillation column, preferred 400 ℃～480 ℃.Described mixing heavy oil is at least a in the turning oil of extraction oil, catalytic cracking of vacuum residuum, long residuum, heavy crude, decompressed wax oil, de-oiled asphalt, deasphalted oil, residual hydrogenation heavy oil, thermal cracking residue, lube oil finishing and clarified oil, cracking of ethylene residual oil and the tar-bitumen etc.
Described visbreaking reactor is tower reactor or shell-and-tube reactor, and when being tower reactor, reactor is at least one, and what reactor was when two or above reactor is connected in series.
The present invention compared with prior art has the following advantages:
1. can improve the liquid product yield of delayed coking unit, improve the character of heavy wax tailings;
2. can reduce the temperature at the bottom of the coking fractional distillation column, slow down the coking at the bottom of the tower;
3. can improve coking heater radiation section feed properties, slow down tube coking, thereby prolong the cycle of operation of delayed coking unit;
4. oil is after underpressure distillation at the bottom of the coking fractional distillation column, and the circulation oil mass can significantly reduce, thereby has reduced the load of coking heater, has namely relatively improved the processing power of coker.
5. technical process is simple, and facility investment is very low, and process cost is also lower;
The below is described in further detail the present invention with the drawings and specific embodiments, but do not limit the scope of the invention, those skilled in the art can be according to raw material properties, and the requirement of purpose product is easy to select suitable operating parameters within the scope of the present invention.
Accompanying drawing and description of drawings
Accompanying drawing is a kind of simple process flow diagram of the inventive method.
Among the figure:
1. fresh feed 2. mixes heavy oil, 3. process furnace, 4. visbreaking reactor raw material, 5. visbreaking reactor, 6. viscosity breaking reaction effluent, 7. flash tank, 8. flash drum overhead light oil and gas, 9. flash tank bottom heavy oil, 10. coking tower charging, 11A, 11B. coke drum, 12. top of coke tower oil gas, 13. mixed oil and gas, 14. separation columns, 15. coke chemicals, 16. Fractionator Bottom is oily, 17. oil pumps, and 18. advance the Fractionator Bottom oil of vacuum distillation tower, 19. long residuum, 20. vacuum distillation tower, 21. vacuum distillates, 22. VACUUM TOWER BOTTOM oil.
Embodiment
As shown in Figure 1, be mixed into separately or with fresh feed from the VACUUM TOWER BOTTOM of vacuum distillation tower 20 oil 22 and mix heavy oil 2 and enter coking heater 3 and be heated to 360 ℃～450 ℃, as the visbreaking reactor raw material 4 of visbreaking reactor 5, be to carry out cracking reaction under the condition of 6min～210min in visbreaking reactor top gauge pressure 0.3MPa～3.5Mpa, the residence time; Ejecting the viscosity breaking reaction effluent 6 that comes from visbreaking reactor 5 enters flash tank 7 and carries out flash separation, isolated flash drum overhead light oil and gas 8 be mixed into mixed oil and gas 13 from top of coke tower oil gas 12 and enter coking fractional distillation column, the heavy oil 9 that flash separation goes out enters process furnace 3 and is heated to 480 ℃～515 ℃ and enters coke drum 11A as coking tower charging 10 or 11B carries out pyrogenic reaction, the gauge pressure of coke drum cat head is 0.103MPa～1.0Mpa, and filling the burnt time is 3hr～48hr; Coking tower generates oil gas 12 flash drum overhead light oil and gas 8 is mixed into mixed oil and gas 13, enter coking fractional distillation column 14 and carry out fractionation, coking light wax oil to the gas that fractionates out goes out coke chemicals 15, oil 16 parts are returned coking fractional distillation column the oil gas from the coke drum cat head are washed heat exchange at the bottom of the coking tower, another part advances the Fractionator Bottom oil 18 of vacuum distillation tower and comes long residuum 19 to be mixed into vacuum distillation tower 20 and distill, vacuum distillate 21-directly goes out device, and oil 22 enters into process furnace 3 and heats as mixing one of heavy oil at the bottom of the tower of vacuum distillation tower, visbreaking and coking.
Embodiment
Embodiment 1:
From the vacuum residuum I of atmospheric and vacuum distillation unit vacuum distillation tower, character sees Table 1, and vacuum residuum I and cut point are to remove visbreaking reactor after the mixing oil of 520 ℃ of coking recycle oils is heated to 410 ℃, in the residence time is to carry out the viscosity breaking reaction under the condition of 42min; The visbreaking reaction mass enters flash tank to be separated; The heavy oil that flashes off is heated to 498 ℃ and goes coke drum to carry out pyrogenic reaction; The oil gas that generates behind chilling with from the oil gas of flash distillation tank deck together defocusing separation column carry out fractionation, obtain gas, gasoline fraction, diesel oil distillate and light wax oil cut, oil is extracted out with pump at the bottom of the tower, a part is washed the oil gas from coke drum etc., another part mixes with long residuum to atmospheric and vacuum distillation unit, then again heat exchange, be heated to and enter vacuum distillation tower after the predetermined temperature and carry out vacuum fractionation, the depth of cut of oil is 520 ℃ at the bottom of the control tower, and main processing condition, the product of coking distribute and the character of heavy wax tailings sees Table 2.
Comparative Examples 1:
Vacuum residuum I convection chamber and radiation chamber to coking heater after heat exchange from the atmospheric and vacuum distillation unit vacuum distillation tower heats; Be heated to and go one of two coke drums to carry out pyrogenic reaction after 498 ℃; Oil gas the defocusing separation column behind chilling that generates carries out fractionation, obtain gas, gasoline fraction, diesel oil distillate and light wax oil cut, oil is extracted out with pump at the bottom of the tower, a part is washed the oil gas from coke drum etc., another part directly goes out device, and main processing condition, the product of coking distribute and see Table 2
Embodiment 2:
From the vacuum residuum II of atmospheric and vacuum distillation unit vacuum distillation tower, character sees Table 1, with depth of cut be that the mixing oil of 565 ℃ of coking recycle oils is heated to 400 ℃ and removes visbreaking reactor, be to carry out the viscosity breaking reaction under the condition of 48min in the cold oil residence time; The visbreaking reaction mass enters flash tank to be separated; After being heated to 495 ℃, go by the heavy oil that goes out to flash off coke drum to carry out pyrogenic reaction; The oil gas that generates behind chilling with from the oil gas of flash distillation tank deck together defocusing separation column carry out fractionation, obtain gas, gasoline fraction, diesel oil distillate and light wax oil cut, oil is extracted out with pump at the bottom of the tower, a part is washed the oil gas from coke drum etc., another part is to atmospheric and vacuum distillation unit and again heat exchange after long residuum mixes, heating, then enter vacuum distillation tower and carry out vacuum fractionation, the cut point of oil is 565 ℃ at the bottom of the control tower, and main processing condition, the product of coking distribute and the character of heavy wax tailings sees Table 3.
Comparative Examples 2:
From the vacuum residuum II of atmospheric and vacuum distillation unit vacuum distillation tower through after the heat exchange with from coking fractional distillation column at the bottom of oil mix, mixing oil is heated to and goes one of two coke drums to carry out pyrogenic reaction after 495 ℃; Oil gas the defocusing separation column behind chilling that generates carries out fractionation, obtain gas, gasoline fraction, diesel oil distillate and light wax oil cut, oil is extracted out with pump at the bottom of the tower, and a part is washed the oil gas from coke drum, and another part mixes with vacuum residuum II from atmospheric and vacuum distillation unit.Main processing condition, the product of coking distribute and see Table 3
The fresh feed main character of table 1 embodiment 1 and embodiment 2
The operational condition of table 2 patent technique of the present invention and existing technique and product distribute and contrast
The operational condition of table 3 patent technique of the present invention and existing technique and product distribute and contrast
Claims (7)
1. the method for a delayed coking may further comprise the steps:
1) mixes heavy oil and enter the process furnace heating, to mix heavy oil and be heated to 360～450 ℃, enter visbreaking reactor from the visbreaking reactor bottom, stop 6～210min, visbreaking reactor top gauge pressure is 0.30～3.5Mpa, the viscosity breaking product enters and carries out gas-liquid separation, and isolated oil gas enters coking fractional distillation column, and isolated visbreaker tar enters step 2);
2) from step 1) visbreaker tar be heated to 480 ℃～515 ℃, enter coking tower and carry out pyrogenic reaction, the gauge pressure of coking tower cat head is 0.103～1.0Mpa, filling the burnt time is 3～48hr, the high-temperature oil gas of coking tower enters coking fractional distillation column, and coke chemicals go out device, and an oil part is returned coking fractional distillation column at the bottom of the coking fractional distillation column, another part enters vacuum distillation tower and carries out fractionation, and the vacuum residuum that fractionates out returns step 1 as mixing heavy oil).
2. according to the method for a kind of delayed coking claimed in claim 1, it is characterized in that: 1) mix heavy oil and enter the process furnace heating, to mix heavy oil and be heated to 380～430 ℃, enter visbreaking reactor from the visbreaking reactor bottom, stop 30～120min, visbreaking reactor top gauge pressure is 0.30～3.5Mpa, and the viscosity breaking product enters and carries out gas-liquid separation, isolated oil gas enters coking fractional distillation column, and isolated visbreaker tar enters step 2);
2) from step 1) visbreaker tar be heated to 480 ℃～515 ℃, enter coking tower and carry out pyrogenic reaction, the gauge pressure of coking tower cat head is 0.103～0.25Mpa, filling the burnt time is 6～20hr.
3. according to the method for a kind of delayed coking claimed in claim 1, it is characterized in that: the oil depth of cut is 350 ℃～500 ℃ at the bottom of the described coking fractional distillation column.
4. according to the method for a kind of delayed coking claimed in claim 1, it is characterized in that: the oil depth of cut is 400 ℃～480 ℃ at the bottom of the described coking fractional distillation column.
5. according to the method for a kind of delayed coking claimed in claim 1, it is characterized in that: described mixing heavy oil is at least a in the turning oil of extraction oil, catalytic cracking of vacuum residuum, long residuum, heavy crude, decompressed wax oil, de-oiled asphalt, deasphalted oil, residual hydrogenation heavy oil, thermal cracking residue, lube oil finishing and clarified oil, cracking of ethylene residual oil and the tar-bitumen etc.
6. according to the method for a kind of delayed coking claimed in claim 1, it is characterized in that: described visbreaking reactor is tower reactor or shell-and-tube reactor.
7. according to the method for a kind of delayed coking claimed in claim 1, it is characterized in that: described visbreaking reactor is tower reactor, and reactor is at least one, and reactor is for being connected in series when two or above reactor.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104164254A (en) * | 2013-05-15 | 2014-11-26 | 中石化洛阳工程有限公司 | Heavy oil processing process |
| CN104178214A (en) * | 2013-05-27 | 2014-12-03 | 任相坤 | Method for preparing liquid fuel through co-refining of visbreaking heavy oil and coal |
| CN104178216A (en) * | 2013-05-27 | 2014-12-03 | 任相坤 | Method for preparing liquid fuel through co-refining of viscosity-reduced heavy oil and coal |
| CN104212473A (en) * | 2013-06-03 | 2014-12-17 | 中国石油化工股份有限公司 | Device for producing road asphalt raw material |
| WO2015199797A1 (en) * | 2014-05-01 | 2015-12-30 | Exxonmobil Research And Engineering Company | Methods and systems for improving liquid yields and coke morphology from a coker |
| US9688925B2 (en) | 2014-05-01 | 2017-06-27 | Exxonmobil Research And Engineering Company | System and methods of trim dewaxing distillate fuels |
| CN114958418A (en) * | 2021-02-18 | 2022-08-30 | 中国石油化工股份有限公司 | Method for producing residual oil by using heating furnace |
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| CN101619238A (en) * | 2008-07-04 | 2010-01-06 | 中国石油化工股份有限公司 | Delayed coking and reduced pressure distillation combined processing method |
| CN101638585A (en) * | 2009-06-25 | 2010-02-03 | 中国石油化工集团公司 | Delayed coking method |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104164254A (en) * | 2013-05-15 | 2014-11-26 | 中石化洛阳工程有限公司 | Heavy oil processing process |
| CN104178214A (en) * | 2013-05-27 | 2014-12-03 | 任相坤 | Method for preparing liquid fuel through co-refining of visbreaking heavy oil and coal |
| CN104178216A (en) * | 2013-05-27 | 2014-12-03 | 任相坤 | Method for preparing liquid fuel through co-refining of viscosity-reduced heavy oil and coal |
| CN104212473A (en) * | 2013-06-03 | 2014-12-17 | 中国石油化工股份有限公司 | Device for producing road asphalt raw material |
| CN104212473B (en) * | 2013-06-03 | 2016-12-28 | 中国石油化工股份有限公司 | A kind of device producing road asphalt raw material |
| WO2015199797A1 (en) * | 2014-05-01 | 2015-12-30 | Exxonmobil Research And Engineering Company | Methods and systems for improving liquid yields and coke morphology from a coker |
| US9688925B2 (en) | 2014-05-01 | 2017-06-27 | Exxonmobil Research And Engineering Company | System and methods of trim dewaxing distillate fuels |
| CN114958418A (en) * | 2021-02-18 | 2022-08-30 | 中国石油化工股份有限公司 | Method for producing residual oil by using heating furnace |
| CN114958418B (en) * | 2021-02-18 | 2023-08-08 | 中国石油化工股份有限公司 | Method for producing residual oil by heating furnace |
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Application publication date: 20130130 |