CN1417294A - Delayed coking process capable of flexibly regulating circulation ratio - Google Patents
Delayed coking process capable of flexibly regulating circulation ratio Download PDFInfo
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- CN1417294A CN1417294A CN 01131528 CN01131528A CN1417294A CN 1417294 A CN1417294 A CN 1417294A CN 01131528 CN01131528 CN 01131528 CN 01131528 A CN01131528 A CN 01131528A CN 1417294 A CN1417294 A CN 1417294A
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Abstract
In the delayed coking process of the present invention, the raw material oil is first preheated in the convection zone of the heating furnace, then passed through the buffering tank and pump and heated in the radiation zone of the heating furnace to coking temperature, and coked in the coking tower. The high temperature oil gas after coking reaction are fractionated in the fractionating tower to obtain the product, and the wax oil from the bottom of the fractionating tower is returned to the buffering tank and is mixed with raw material oil preheated in the convection zone of the heating furnace, with the circulation ratio being regulated in 0-0.65. The said process can increase the processing capacity of the equipment, regulate product structure and improve product distribution.
Description
One, technical field:
The present invention relates to the refinery delay coking process, but particularly relate to a kind of delay coking process of flexible recycle ratio.
Two, prior art overview:
Delayed coking is a kind of heat processing technique that residual oil is converted into gas, light, middle matter distillate and coke through drastic cracking.Conventional delay coking process is: stock oil enters separation column and the next coking oil gas heat exchange of coke drum after the process furnace preheating, entering the process furnace radiation section again is heated to coking temperature and enters the coke drum coking, coking oil gas from the coke cat head distillate enter separation column fractionate out gas, gasoline, diesel oil and, the coking wax slop recycles, coke is flocked in the coke drum, and Fig. 1 is seen in its technical process.The weak point of this technology is: recycle ratio is bigger, is generally about 0.4, therefore causes the device processing power to descend, and the liquid oils product yield is low, coking yield and rich gas productive rate height.Particularly when taking low recycle ratio 0～0.25, separation column bottom heat exchanging segment temperature height, easily coking influences the normal operation of radiation fresh feed pump, causes the radiating furnace tube coking and shortens the device cycle of operation.
Three, summary of the invention:
But the delay coking process that the purpose of this invention is to provide a kind of flexible recycle ratio is to overcome the deficiency of existing coking process.
Technology of the present invention is achieved in that on delayed coking unit stock oil is introduced into the preheating of process furnace convection zone, enters surge tank again, enters the process furnace radiation section through pump then and is heated to coking temperature and enters the coke drum coking; High-temperature oil gas after the pyrogenic reaction enters separation column separate after directly as product, the wax slop at the bottom of the separation column can be circulated to surge tank by pump to be mixed with the vacuum residuum of process furnace convection zone preheating, recycle ratio can flexible in 0～0.65 scope.
When recycle ratio was 0～0.25, fractionator bottom temperature was controlled at 340～360 ℃.
Described coking raw material comprises that the long residuum, vacuum residuum, visbreaking residue, catalytically cracked oil, hydrocracking tail oil, ethylene bottom oil, lubricating oil of any crude oil extract oil and two or more out.
Adopt delay coking process of the present invention, compare, have the advantage of the following aspects with traditional coking process:
1, device has flexibility of operation preferably, and recycle ratio can be adjustable arbitrarily.
2, when recycle ratio is 0～0.25, reduced the cracking once more of turning oil, improved the device working ability, reduced the rich gas productive rate simultaneously, improve liquid yield, reduced coke output.Overcome the coking of separation column feed zone simultaneously, improved the running environment of radiation fresh feed pump.
Four, description of drawings:
Fig. 1 is the technical process of former coking process.
Fig. 2 is a delay coking process schema of the present invention.
Five, embodiment:
Further describe characteristics of the present invention below in conjunction with example.
Example 1
As shown in Figure 2, adopt pipe oil transportation vacuum residuum, coking raw material I enters surge tank 2 after process furnace 1 convection zone preheating, enter process furnace 1 radiation section by pump 3 again and be heated to coking temperature, advances coke drum 4/5 coking again.Coking oil gas enters separation column 6 by coke drum 4/5 overhead line, and fractionation obtains gas II, gasoline III, diesel oil IV, light wax oil V and wax slop VI.Wax slop is extracted out from 6 ends of separation column and is all gone out device, and recycle ratio is 0, the main technique condition and the results are shown in Table 1, table 2.
Example 2
As shown in Figure 2, adopt pipe oil transportation vacuum residuum, coking raw material I enters surge tank 2 after process furnace 1 convection zone preheating, enter process furnace 1 radiation section by pump 3 again and be heated to coking temperature, advances coke 4/5 coking again.Coking oil gas enters separation column 6 by coke drum 4/5 overhead line, and fractionation obtains gas II, gasoline III, diesel oil IV, light wax oil V and wax slop VI.Wax slop was extracted out from 6 ends of separation column, and wherein a part is circulated to surge tank 2 by pump 7 and mixes with the stock oil I of process furnace 1 convection zone preheating, and recycle ratio is 0.1, and a part directly goes out device in addition, the main technique condition and the results are shown in Table 1, table 2.
Example 3
As shown in Figure 2, adopt the defeated vacuum residuum of pipe, coking raw material I enters surge tank 2 after process furnace 1 convection zone preheating, enter process furnace 1 radiation section by pump 3 again and be heated to coking temperature, advances coke 4/5 coking again.Coking oil gas enters separation column 6 by coke drum 4/5 overhead line, and fractionation obtains gas II, gasoline III, diesel oil IV, light wax oil V and wax slop VI.Wax slop was extracted out from 6 ends of separation column, and wherein a part is circulated to surge tank 2 by pump 7 and mixes with the stock oil I of process furnace 1 convection zone preheating, and recycle ratio is 0.25, and a part directly goes out device in addition, the main technique condition and the results are shown in Table 1, table 2.
Example 4
As shown in Figure 2, adopt defeated vacuum residuum of pipe and catalytically cracked oil to be mixed into coking raw material.Coking raw material I enters surge tank 2 after process furnace 1 convection zone preheating, enter process furnace 1 radiation section by pump 3 again and be heated to coking temperature, advances coke drum 4/5 coking again.Coking oil gas enters separation column 6 by coke drum 4/5 overhead line, and fractionation obtains gas II, gasoline III, diesel oil IV, light wax oil V and wax slop VI.Wax slop was extracted out from 6 ends of separation column, and wherein a part is circulated to surge tank 2 by pump and mixes with the stock oil I of process furnace 1 convection zone preheating, and recycle ratio is 0.4, and a part directly goes out device in addition, the main technique condition and the results are shown in Table 1,, table 2.
Example 5
As shown in Figure 2, adopt the defeated vacuum residuum of pipe, coking raw material I enters surge tank 2 after process furnace 1 convection zone preheating, enter process furnace 1 radiation section by pump 3 again and be heated to coking temperature, advances coke drum 4/5 coking again.Coking oil gas enters separation column 6 by coke drum 4/5 overhead line, and fractionation obtains gas II, gasoline III, diesel oil IV, light wax oil V and wax slop VI.Wax slop was extracted out from 6 ends of separation column, and wherein a part is circulated to surge tank 2 by pump and mixes with the stock oil I of process furnace 1 convection zone preheating, and recycle ratio is 0.5, and a part directly goes out device in addition, the main technique condition and the results are shown in Table 1, table 2.
Example 6
As shown in Figure 2, adopt the defeated vacuum residuum of pipe, coking raw material I enters surge tank 2, enters process furnace 1 radiation section by pump 3 again and be heated to coking temperature after process furnace 1 convection zone preheating, advances coke drum 4/5 coking again.Coking oil gas enters separation column 6 by coke drum 4/5 overhead line, and fractionation obtains gas II, gasoline III, diesel oil IV, light wax oil V and wax slop VI.Wax slop was extracted out from 6 ends of separation column, and wherein a part is circulated to surge tank 2 by pump and mixes with the stock oil I of process furnace 1 convection zone preheating, and recycle ratio is 0.65, and a part directly goes out device in addition, the main technique condition and the results are shown in Table 1, table 2.
Table 1
Project example 1 example 2 examples 3 examples 4 examples 5 examples 6
Recycle ratio 0 0.1 0.25 0.4 0.5 0.65
The device amount of finish
Ton/sky2,480 2,360 2,250 2,100 1,900 1400
Gas % 5.12 5.64 6.16 5.78 6.21 7.12
Gasoline % 8.87 9.12 8.75 8.39 9.32 10.61
Diesel oil % 31.22 31.32 33.69 37.44 37.15 36.64
Wax oil % 32.52 31.55 27.08 22.85 21.45 18.85
Coke % 22.26 22.37 24.32 25.54 25.87 26.78
Liquid yield: % 72.61 71.99 69.52 68.68 67.92 66.10
Fractionator bottom temperature ℃ 348 353 352 354 356 338
Liquid level % 15 28 37 40 40 48
Table 2 raw material and product property
The heavy wax of the light wax of project gasoline, diesel mixes petroleum tailings oil
d
20 4 0.72 0.84 0.91 0.99 0.93 0.98
KK 160 360
350℃％ 8 3 4.5
500℃％ 88 36.5 75 7.5
Rc 1.65 17.6 3.66 15.25
υ
50 33.4 76
υ
100 70 1080
Alkali nitrogen ppm 1,700 3,000 2,600 2000
C％ 86.11 85.6
H％ 11.69 11.3
Stable hydrocarbon % 57.77
Aromatic hydrocarbon % 25.79
Colloid+bituminous matter % 14.46
Coke % fugitive constituent 7.8 sulphur 1.8～2.5 ash contents 0.20
Claims (3)
1, a kind of delayed coking complete processing, it is characterized in that stock oil is introduced into the preheating of process furnace convection zone, enter surge tank again, entering the process furnace radiation section through pump then is heated to coking temperature and enters the coke drum coking, high-temperature oil gas after the pyrogenic reaction enters separation column separate after directly as product, wax oil at the bottom of the separation column can be circulated to surge tank by pump to be mixed with the stock oil of process furnace convection zone preheating, and recycle ratio is adjustable arbitrarily in 0～0.65 scope.
2, delayed coking complete processing according to claim 1 is characterized in that when recycle ratio is 0～0.25 fractionator bottom temperature is controlled at 340～360 ℃.
3, delayed coking complete processing according to claim 1 is characterized in that described coking raw material comprises that the long residuum, vacuum residuum, visbreaking residue, catalytically cracked oil, hydrocracking tail oil, ethylene bottom oil, lubricating oil of any crude oil extract oil and two or more out.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01131528 CN1417294A (en) | 2001-11-06 | 2001-11-06 | Delayed coking process capable of flexibly regulating circulation ratio |
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|---|---|---|---|
| CN 01131528 CN1417294A (en) | 2001-11-06 | 2001-11-06 | Delayed coking process capable of flexibly regulating circulation ratio |
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| CN1417294A true CN1417294A (en) | 2003-05-14 |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1323131C (en) * | 2004-03-31 | 2007-06-27 | 中国石油化工股份有限公司 | Delayed coking method for increasing coke strength |
| CN104046385A (en) * | 2013-03-17 | 2014-09-17 | 中国石油化工股份有限公司 | Delayed coking process and device |
| CN104046384A (en) * | 2013-03-17 | 2014-09-17 | 中国石油化工股份有限公司 | Delayed coking process and device |
| CN104046386A (en) * | 2013-03-17 | 2014-09-17 | 中国石油化工股份有限公司 | Delayed coking process and device |
| CN104927920A (en) * | 2014-03-21 | 2015-09-23 | 中国石油化工股份有限公司 | Residue oil coking method |
| CN105400543A (en) * | 2015-12-18 | 2016-03-16 | 广东石油化工学院 | Blend oil product and preparation method thereof |
| CN105885933A (en) * | 2014-12-15 | 2016-08-24 | 中石化洛阳工程有限公司 | Deoiled asphalt processing method |
| CN105885939A (en) * | 2014-12-15 | 2016-08-24 | 中石化洛阳工程有限公司 | Method for processing deoiled asphalt |
| CN107541247A (en) * | 2017-10-04 | 2018-01-05 | 山东胜星化工有限公司 | A kind of sump oil continues uninterrupted freshening device |
| CN108219839A (en) * | 2018-01-02 | 2018-06-29 | 中和亚通能源科技有限公司 | A kind of needle coke production method and device |
| CN109321264A (en) * | 2018-10-31 | 2019-02-12 | 西北大学 | A kind of pyrolysis of coal oil increasing device and technique |
-
2001
- 2001-11-06 CN CN 01131528 patent/CN1417294A/en active Pending
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1323131C (en) * | 2004-03-31 | 2007-06-27 | 中国石油化工股份有限公司 | Delayed coking method for increasing coke strength |
| CN104046384B (en) * | 2013-03-17 | 2016-01-20 | 中国石油化工股份有限公司 | A kind of processing method of delayed coking and device |
| CN104046385A (en) * | 2013-03-17 | 2014-09-17 | 中国石油化工股份有限公司 | Delayed coking process and device |
| CN104046384A (en) * | 2013-03-17 | 2014-09-17 | 中国石油化工股份有限公司 | Delayed coking process and device |
| CN104046386A (en) * | 2013-03-17 | 2014-09-17 | 中国石油化工股份有限公司 | Delayed coking process and device |
| CN104046385B (en) * | 2013-03-17 | 2016-01-20 | 中国石油化工股份有限公司 | A kind of processing method of delayed coking and device |
| CN104046386B (en) * | 2013-03-17 | 2016-01-20 | 中国石油化工股份有限公司 | A kind of processing method of delayed coking and device |
| CN104927920B (en) * | 2014-03-21 | 2017-03-15 | 中国石油化工股份有限公司 | A kind of residuum coking method |
| CN104927920A (en) * | 2014-03-21 | 2015-09-23 | 中国石油化工股份有限公司 | Residue oil coking method |
| CN105885933A (en) * | 2014-12-15 | 2016-08-24 | 中石化洛阳工程有限公司 | Deoiled asphalt processing method |
| CN105885939A (en) * | 2014-12-15 | 2016-08-24 | 中石化洛阳工程有限公司 | Method for processing deoiled asphalt |
| CN105400543A (en) * | 2015-12-18 | 2016-03-16 | 广东石油化工学院 | Blend oil product and preparation method thereof |
| CN105400543B (en) * | 2015-12-18 | 2017-02-01 | 广东石油化工学院 | Blend oil product and preparation method thereof |
| CN107541247A (en) * | 2017-10-04 | 2018-01-05 | 山东胜星化工有限公司 | A kind of sump oil continues uninterrupted freshening device |
| CN108219839A (en) * | 2018-01-02 | 2018-06-29 | 中和亚通能源科技有限公司 | A kind of needle coke production method and device |
| CN108219839B (en) * | 2018-01-02 | 2024-04-09 | 亚通石化集团有限公司 | Needle coke production method and device |
| CN109321264A (en) * | 2018-10-31 | 2019-02-12 | 西北大学 | A kind of pyrolysis of coal oil increasing device and technique |
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