CN102899077A - Coking method - Google Patents
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- CN102899077A CN102899077A CN201110210997XA CN201110210997A CN102899077A CN 102899077 A CN102899077 A CN 102899077A CN 201110210997X A CN201110210997X A CN 201110210997XA CN 201110210997 A CN201110210997 A CN 201110210997A CN 102899077 A CN102899077 A CN 102899077A
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Abstract
The invention discloses a coking method. The method comprises the following steps: heating raw oil in a 360-450DEG C heating furnace, allowing the heated raw oil to enter a viscosity-reduction cracking reactor with the top pressure in the reactor of 0.30-3.5Mpa and stay for 6-210min, allowing the resultant reaction oil gas to enter the radiation chamber of a coking heating furnace, to be heated to 480-515DEG C and to enter a coking tower, quenching the coked high temperature oil gas, allowing the quenched oil gas to enter a coking fractionation tower, fractionating, returning parts of the tower bottom oil of the coking fractionation tower to the coking fractionation tower, allowing the other parts of the tower bottom oil to be mixed with a normal pressure residuum and then to enter a vacuum tower, and separating a vacuum residuum which can be adopted as a raw material for the viscosity reduction cracking. The method can increase the liquid product yield and improve the properties of heavy-coking gas oil.
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 is a kind of deep processing technique that heavy oil is converted into gas, light ends oil and middle matter distillate and coke through degree of depth thermally splitting, the characteristics such as have that the charcoal of taking off is thorough, flow process is simple, technology maturation, plant investment are lower are so become one of important process in the heavy oil upgrading technique.
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.In charging, add low boiling component to substitute turning oil such as patent US4518487; Patent US4455219, CN1138843C add thinner in charging; Patent US4784744, US5006223, US4378288 add free radical inhibitors in charging; Patent CN101037618A adds the arene coking inhibitor in coking raw material; 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 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.
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 charging quality, aggravate the coking of heating furnace tube, thereby can shorten the on-stream time of device.
Summary of the invention
A kind of new Technology that the present invention be directed to the deficiencies in the prior art and propose, specifically, this technique is a kind of new Technology that the unit operation of underpressure distillation, viscosity breaking and delayed coking is organically combined to process heavy oil.Use method processing heavy oil of the present invention can improve the liquid product yield of delayed coking unit, reduce dry gas and coking yield, and can improve the character of heavy wax tailings, can prolong the on-stream time of delayed coking unit simultaneously.
A kind of coking method provided by the invention may further comprise the steps:
1) stock oil is at 360～450 ℃, and after heating in preferred 380～430 ℃ process furnace, entering top pressure is 0.30～3.5Mpa visbreaking reactor, stops 6～210min, preferred 30～120min, reaction oil gas is to step 2);
2) enter coking tower after the radiation chamber that enters coking heater from the oil gas of visbreaking reactor is heated to 480 ℃～515 ℃ and carry out pyrogenic reaction, the gauge pressure of coking tower cat head is 0.103～1.0Mpa, preferred 0.103～0.25Mpa, filling the burnt time is 3～48hr, preferred 6～20hr, high-temperature oil gas after the coking enters coking fractional distillation column through chilling and carries out fractionation, an oil part is returned coking fractional distillation column at the bottom of the coking fractional distillation column tower, another part with enter vacuum distillation tower after long residuum mixes, the isolated vacuum residuum of vacuum distillation tower turns back to step 1).
Described vacuum residuum cutting temperature is 400 ℃～605 ℃, preferred 500 ℃～565 ℃.
The cutting temperature of oil is 350 ℃～500 ℃ at the bottom of the described coking fractional distillation column tower, preferred 400 ℃～480 ℃.
Described stock oil is vacuum residuum, at least a in the turning oil of the extraction of long residuum, heavy crude, decompressed wax oil, de-oiled asphalt, deasphalted oil, residual hydrogenation heavy oil, thermal cracking residue, lube oil finishing oil, catalytic cracking and clarified oil, cracking of ethylene residual oil and the tar-bitumen etc.
Described visbreaking reactor is tower reactor or shell-and-tube reactor.When being tower reactor, reactor is a reactor or a plurality of, is series system during two above reactors.
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. after the feed properties of coking heater radiation section is improved, not only can improve the linear speed of logistics in the boiler tube, and can improve the flow state of logistics, thereby suppress generation and the deposition of coking precursor at radiation section, slow down tube coking, thereby prolonged 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 charging, 5. visbreaking reactor, 6. viscosity breaking oil gas, 7. burnt tower charging, 8A, 8B. coke drum, 9. top of coke tower oil gas, 10. coking fractional distillation column, 11. wax tailings be to gas, oil at the bottom of the 12. fractionation Tatas, 13. pump at the bottom of the coking fractional distillation column, 14. enter oil at the bottom of the fractionation Tata of vacuum distillation tower, 15. long residuums, 16 vacuum distillation towers, 17. vacuum distillates, 18. vacuum residuum.
Embodiment
As shown in Figure 1, be mixed into convection chamber or convection chamber and the radiation chamber heating that enters coking heater 3 through coking heater convection zone charging 2 separately or with fresh feed from vacuum distillation tower 16 vacuum residuum 18; Visbreaking reactor charging 4 enters Visbreaking reactor 5 after being heated to 360 ℃～450 ℃, and gauge pressure 0.3MPa～3.5Mpa, the residence time are the heat cracking reaction that carries out appropriateness under the condition of 6min～210min; Enter the radiation chamber heating of process furnace 3 from Visbreaking reactor 5 visbreaking oil gas 6 out, coking heater radiation section outlet material 7 enters coke drum 8A (or 8B) and carries out pyrogenic reaction after being heated to 480 ℃～515 ℃, coke Tata operational condition is: gauge pressure is 0.103MPa～1.0Mpa, and filling the burnt time is 3hr～48hr; Top of coke tower oil gas 9 chillings carry out fractionation by entering coking fractional distillation column 10, the wax tailings that fractionates out to gas 11 goes out device, oil 12 is extracted out by pump at the bottom of the coking fractional distillation column 13 at the bottom of the coking fractional distillation column tower, a part is returned coking fractional distillation column the oil gas from the coke drum cat head is washed heat exchange etc., and another part carries out underpressure distillation as entering vacuum distillation tower 16 after entering at the bottom of the coking fractional distillation column tower of vacuum distillation tower oil 14 and long residuum mixing; The vacuum distillate 17 of vacuum distillation tower 16 goes out device, and the vacuum residuum 18 at the bottom of the decompression Tata goes process furnace 3 to heat.
Embodiment
The below describes the present invention in detail with specific embodiment, but does not limit the scope of the invention.
Embodiment 1:
From the vacuum residuum I character of atmospheric and vacuum distillation unit vacuum distillation tower see Table 1 with cut point be the mixing oil of oil at the bottom of 520 ℃ of coking fractional distillation column towers, be transported to convection chamber and the radiation chamber heating of coking heater; Remove visbreaking reactor after being heated to 410 ℃, at 0.30～3.5Mpa pressure, the cold oil residence time is to carry out the viscosity breaking reaction under the condition of 42min; The viscosity breaking reaction oil gas turns back to the radiation chamber heating of coking heater again, is heated to 498 ℃ of laggard coking towers and carries out pyrogenic reaction; 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 coking fractional distillation column 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 ℃ (usual termss) 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, and a part is washed etc. the oil gas from coke drum, and another part directly goes out device (coking single-pass operation).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 see Table 1 with cut point be convection chamber and the radiation chamber heating that the mixing oil of oil enters coking heater at the bottom of 565 ℃ of coking fractional distillation column towers; Being heated to and removing visbreaking reactor after 400 ℃ is to carry out the viscosity breaking reaction under the condition of 48min in the 3.5Mpa pressure cold oil residence time; The oil gas that goes out visbreaking reactor turns back to the radiation chamber heating of coking heater again, 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, 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 mixes (natural circulation ratio), mixing oil heats to convection chamber and the radiation chamber of coking heater; Be heated to and go 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 (11)
1. a coking method is characterized in that, may further comprise the steps:
1) after stock oil heated in 360～450 ℃ process furnace, entering top pressure was 0.30～3.5Mpa visbreaking reactor, stopped 6～210min, and reaction oil gas is to step 2);
2) enter coking tower after the radiation chamber that comes the oil gas of visbreaking reactor to enter coking heater is heated to 480 ℃～515 ℃ 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, high-temperature oil gas after the coking enters coking fractional distillation column through chilling and carries out fractionation, an oil part is returned coking fractional distillation column at the bottom of the coking fractional distillation column tower, another part with enter vacuum distillation tower after long residuum mixes, the isolated vacuum residuum of vacuum distillation tower turns back to step 1).
2. according to a kind of coking method claimed in claim 1, it is characterized in that: after stock oil heated in 380～430 ℃ process furnace, entering the top was 0.30～3.5Mpa visbreaking reactor, stopped 30～120min.
3. according to a kind of coking method claimed in claim 1, it is characterized in that, enter coking tower after the radiation chamber that enters coking heater from the oil gas of visbreaking reactor is heated to 480 ℃～515 ℃ and carry out pyrogenic reaction, the gauge pressure of coking tower cat head is 0.103～0.25Mpa, fills burnt time 6～20hr.
4. according to a kind of coking method claimed in claim 1, it is characterized in that: described vacuum residuum cutting temperature is 400 ℃～605 ℃.
5. according to a kind of coking method claimed in claim 1, it is characterized in that: described vacuum residuum cutting temperature is 500 ℃～565 ℃.
6. according to a kind of coking method claimed in claim 1, it is characterized in that: the cutting temperature of oil is 350 ℃～500 ℃ at the bottom of the described coking fractional distillation column tower.
7. according to a kind of coking method claimed in claim 1, it is characterized in that: the cutting temperature of oil is 400 ℃～480 ℃ at the bottom of the described coking fractional distillation column tower.
8. according to a kind of coking method claimed in claim 1, it is characterized in that: described stock oil is vacuum residuum, at least a in the turning oil of the extraction of long residuum, heavy crude, decompressed wax oil, de-oiled asphalt, deasphalted oil, residual hydrogenation heavy oil, thermal cracking residue, lube oil finishing oil, catalytic cracking and clarified oil, cracking of ethylene residual oil and the tar-bitumen etc.
9. according to a kind of coking method claimed in claim 1, it is characterized in that: described visbreaking reactor is tower reactor or shell-and-tube reactor.
10. according to a kind of coking method claimed in claim 1, it is characterized in that: described visbreaking reactor is tower reactor.
11. according to a kind of coking method claimed in claim 1, it is characterized in that: when visbreaking reactor is two above tower reactors, reactors in series.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110210997XA CN102899077A (en) | 2011-07-27 | 2011-07-27 | Coking method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110210997XA CN102899077A (en) | 2011-07-27 | 2011-07-27 | Coking method |
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| CN102899077A true CN102899077A (en) | 2013-01-30 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108611118A (en) * | 2018-05-28 | 2018-10-02 | 中石化（洛阳）科技有限公司 | A kind of coking delay process and system |
| CN108624353A (en) * | 2018-05-28 | 2018-10-09 | 中石化（洛阳）科技有限公司 | A kind of delayed coking method, equipment and product |
| CN109777458A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | A kind of preparation method of high-quality needle coke |
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| CN101280212A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for processing highly acid crude oil by using delayed coking process |
| 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 |
| CN101619237A (en) * | 2008-07-04 | 2010-01-06 | 中国石油化工股份有限公司 | Combined processing method capable of improving coking liquid-phase product yield |
-
2011
- 2011-07-27 CN CN201110210997XA patent/CN102899077A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101280212A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for processing highly acid crude oil by using delayed coking process |
| 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 |
| CN101619237A (en) * | 2008-07-04 | 2010-01-06 | 中国石油化工股份有限公司 | Combined processing method capable of improving coking liquid-phase product yield |
Non-Patent Citations (1)
| Title |
|---|
| 陈绍洲，常可怡: "《石油加工工艺学》", 31 December 1997, article "减粘裂化", pages: 133 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109777458A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | A kind of preparation method of high-quality needle coke |
| CN108611118A (en) * | 2018-05-28 | 2018-10-02 | 中石化（洛阳）科技有限公司 | A kind of coking delay process and system |
| CN108624353A (en) * | 2018-05-28 | 2018-10-09 | 中石化（洛阳）科技有限公司 | A kind of delayed coking method, equipment and product |
| CN108611118B (en) * | 2018-05-28 | 2020-09-01 | 中石化（洛阳）科技有限公司 | Delayed coking process method and system |
| CN108624353B (en) * | 2018-05-28 | 2020-09-01 | 中石化（洛阳）科技有限公司 | Delayed coking method, equipment and product |
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Application publication date: 20130130 |