CN1212369C - Delayed coking process with low circulation ratio - Google Patents
Delayed coking process with low circulation ratio Download PDFInfo
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- CN1212369C CN1212369C CN 01134273 CN01134273A CN1212369C CN 1212369 C CN1212369 C CN 1212369C CN 01134273 CN01134273 CN 01134273 CN 01134273 A CN01134273 A CN 01134273A CN 1212369 C CN1212369 C CN 1212369C
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Abstract
The present invention relates to a delayed coking method with low circulation ratio. Fresh coking stock is firstly preheated by a convection section of a heating furnace and is mixed with heavy coker gatch from a cyclone separator, and then the mixture enters a radiation section of the heating furnace for heated and then is coked in a coke tower. Coking oil gas generated by coking enters the cyclone separator, the cold heavy coker gatch is injected from the top of the cyclone separator, the purified coking oil gas enters a fractionation tower to be separated, wherein a small amount of the heavy coker gatch enters the cyclone separator for washing oil after cooled. Coke powder, asphaltene and the heavy coker gatch used for washing the high temperature coking oil gas, which are separated from the coking oil gas, are mixed with the fresh coking stock and orderly enter the radiation section of the heating furnace and the coke tower. The method not only can increase the process capability of the existing delayed coking device, but also can produce the heavy coker gatch with good quality.
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 coking delay process of low recycle ratio.
Background technology
Delayed coking is a kind of heat processing technique that the residual oil drastic cracking is converted into gas, light ends oil, middle matter distillate and coke, it has advantages such as reduced investment, flow process are simple, technology maturation, the character that do not processed raw material restriction, is the main means of residual oil processing in the current refinery.
In the delay coking process of routine, stock oil enters separation column after the preheating of process furnace convection zone, after the high-temperature-coked oil gas heat exchange of Ta Nei and coke drum, flow into the bottom of separation column, oil is extracted out with hot oil pump at the bottom of the separation column, enters the process furnace radiation section and is heated to coking temperature and enters the coke drum coking.The high-temperature oil gas that coking produces is then returned separation column.Therefore in conventional delay coking process, pyrogenic charging by fresh feed oil and coking oil gas in separation column condensation and flow into separation column at the bottom of heavy wax tailings form, the so-called recycle ratio of one of important operational condition in the coking process, be meant the part by weight of this heavy wax tailings, be generally 0.4: 1 fresh feed oil.
In recent years, because crude oil becomes heavy and to the increase in demand of lightweight oil, the refinery all requires to enlarge the working ability of delayed coking both at home and abroad, therefore requires to reduce the recycle ratio of delayed coking one after another, because reduce the ability increase that recycle ratio means coker processing fresh feed oil.
In order to improve the working ability of coker, Ding Zongyu etc. (" refining of petroleum ", the 38th volume, 1988 the 8th phases) developed a kind of delay coking process of zero recycle ratio, in the technology of being developed, fresh feed oil does not enter separation column and the direct heat exchange of high-temperature-coked oil gas, but, be heated to coking temperature through process furnace by behind heat exchanger and the coke chemicals indirect heat exchange, enter the coke drum coking, the resulting heavy wax tailings of coking does not carry out freshening but as coke chemicals; At the bottom of separation column, discharge.
USP4,518,487, USP4,549,934, USP4, the delayed coking of the zero recycle ratio of exploitation such as 661, the 241 delay coking process flow processs of being announced and principle of operation and Ding Zongyu is similar.
Above-mentioned delay coking process weak point is: often contain the impurity that some carries out from coke drum in the resulting heavy wax tailings, thereby heavy wax tailings poor quality.
In order to improve the quality of above-mentioned heavy wax tailings, USP4,534,854 and CN1176287A introduce, with heavy wax tailings through solvent treatment or solvent deasphalting telling high carbon residue material wherein, the low carbon residue wax tailings after refining is then wanted the raw material of hydrocracking as catalytic cracking.
USP5,645,711 propositions will weigh wax tailings and remove by filter wherein solid matter, carry out hydrofining then.
The common feature of above-mentioned patent is for improving heavy wax tailings quality, to need to build new solvent deasphalting, solvent treatment or hydro-refining unit, thereby need high construction investment and process cost.
Summary of the invention
The objective of the invention is to overcome the shortcoming of prior art, a kind of improved coking delay process is proposed, this method can improve the working ability of existing delayed coking unit, can produce the heavy preferably wax tailings of quality again, and not need high construction investment and process cost.
Method provided by the invention comprises:
1), fresh coking raw material oil is heated to 350 ℃～370 ℃ through the convection zone of process furnace earlier, incoming stock tundish, in the raw material tundish coking raw material oil with from coke powder, the bituminous matter of cyclonic separator and to be used to wash temperature be after heavy wax tailings behind 420 ℃～460 ℃ the high-temperature-coked oil gas mixes, the radiation section that enters process furnace is heated to 490 ℃～500 ℃, enter coke drum and carry out coking, the coke that coking generates is stayed in the coke drum;
2), the coking oil gas that coking generates enters cyclonic separator with tangential way, coking oil gas is 10 seconds to 5 minutes in the residence time of cyclonic separator, temperature is 420 ℃～460 ℃, and at the cold heavy wax tailings of the top of cyclonic separator injection from separation column, the coke powder and the bituminous matter of carrying in the high-temperature-coked oil gas are separated, coking oil gas after the purification enters in the separation column, separate and obtain dry gas, gasoline, diesel oil, light wax tailings, heavy wax tailings, enter above-mentioned cyclonic separator after the wherein heavy on a small quantity wax tailings cooling, the weight ratio of cold heavy wax tailings and fresh feed oil is 0.05～0.1: 1;
3), the then incoming stock tundish of heavy wax tailings that wash behind the high-temperature-coked oil gas of coke powder, the bituminous matter separated from coking oil gas and being used to mix with fresh coking raw material oil, enter radiation section, the coke drum of process furnace successively.
Embodiment
Method provided by the invention comprises:
1), fresh coking raw material oil is heated to 350 ℃～370 ℃ through the convection zone of process furnace earlier, incoming stock tundish, in the raw material tundish coking raw material oil with from coke powder, the bituminous matter of cyclonic separator and to be used to wash temperature be after heavy wax tailings behind 420 ℃～460 ℃ the high-temperature-coked oil gas mixes, the radiation section that enters process furnace is heated to 490 ℃～500 ℃, enter coke drum and carry out coking, the coke that coking generates is stayed in the coke drum;
2), the coking oil gas that coking generates enters cyclonic separator with tangential way, coking oil gas is 10 seconds to 5 minutes in the residence time of cyclonic separator, temperature is 420 ℃～460 ℃, and at the cold heavy wax tailings of the top of cyclonic separator injection from separation column, the coke powder and the bituminous matter of carrying in the high-temperature-coked oil gas are separated, coking oil gas after the purification enters in the separation column, separate and obtain dry gas, gasoline, diesel oil, light wax tailings, heavy wax tailings, enter above-mentioned cyclonic separator after the wherein heavy on a small quantity wax tailings cooling, the weight ratio of cold heavy wax tailings and fresh feed oil is 0.05～0.1: 1;
3), the then incoming stock tundish of heavy wax tailings that wash behind the high-temperature-coked oil gas of coke powder, the bituminous matter separated from coking oil gas and being used to mix with fresh coking raw material oil, enter radiation section, the coke drum of process furnace successively.
The separating effect of cyclonic separator is relevant with the coking oil gas residence time and temperature therein, coking oil gas is in the residence time of cyclonic separator, it can be 10 seconds to 5 minutes, be preferably 30 seconds to 1 minute, its temperature can be 420 ℃～460 ℃, be preferably 425 ℃～435 ℃, the temperature of coking oil gas in cyclonic separator can be regulated by the cold heavy wax tailings amount of squeezing into, and the cold heavy wax tailings amount of squeezing into usually is about 0.05～0.1 to fresh feed oil: 1.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.
Accompanying drawing 1 is conventional delay coking process flow process, and recycle ratio is generally 0.4: 1 in this flow process, and coking oil gas does not carry out any purifying treatment.
Accompanying drawing 2 is conventional zero recycle ratio delay coking process flow processs, and recycle ratio is 0 in this flow process, does not promptly have the wax tailings circulation, and coking oil gas does not carry out any purifying treatment yet.
Accompanying drawing 3 is low recycle ratio delay coking process flow processs provided by the invention, and recycle ratio is 0.05～0.1: 1 in this flow process, and coking oil gas is through the cyclonic separator purifying treatment.
Method flow provided by the invention is as follows: fresh coking raw material oil enters heat exchanger 15 and heavy wax tailings heat exchange through pipeline 12 first, then the convection section that enters heating furnace 2 through pipeline 1 is heated to 350 ℃～370 ℃, enter raw material pans 5 through pipeline 13, the heavy wax tailings that coking raw material oil and the impurity of separating through cyclone separator from high-temperature-coked oil gas, carried out by coke drum 7 and some are used for washing behind the high-temperature-coked oil gas in raw material pans 5 mixes, the radiant section of sending into heating furnace 2 through pipeline 3 with hot oil pump is heated to 490 ℃～500 ℃ and enters coke drum 7 and carry out coking, the coke that coking generates is stayed in the coke drum 7, and the coking oil gas that coking generates enters cyclone separator 10 through pipeline 8 with tangential way. In high-temperature-coked oil gas, some coke powder and the asphalitine of carrying out from coke drum, because its proportion is larger, thereby in cyclone separator 10, be separated, for these impurity can be separated from coking oil gas fully, at the top of cyclone separator and squeeze into a small amount of cooled heavy wax tailings with the washing coking oil gas. Coking oil gas after the purification enters in the fractionating column 4 through pipeline 11, separates to obtain dry gas, gasoline, diesel oil, light wax tailings, heavy wax tailings, and wherein a small amount of heavy wax tailings cooling enters cyclone separator 10 by pipeline 9; The impurity of from coking oil gas, separating and be used for flushing high-temperature-coked oil gas after heavy wax tailings then flow into raw material pans 5 through pipeline 14, high-temperature oil gas for fear of cyclone separator 10 seals in raw material pans 5, and pipeline 14 should insert following 2～3 meters of raw material pans liquid level.
The separating effect of cyclone separator 10 is relevant with the coking oil gas time of staying and temperature therein, coking oil gas is in the time of staying of cyclone separator, it can be 10 seconds to 5 minutes, be preferably 30 seconds to 1 minute, its temperature can be 420 ℃～460 ℃, be preferably 425 ℃～435 ℃, the temperature of coking oil gas in cyclone separator can be regulated by the cold heavy wax tailings amount of squeezing into, and the cold heavy wax tailings amount of usually squeezing into is about 0.05～0.1 to fresh feed oil: 1.
Accompanying drawing 4 is the connection diagram that is used for cyclone separator of the present invention and is adjacent equipment.
The coking oil gas that coking generates enters cyclone separator 10 through pipeline 8 with tangential way. In high-temperature-coked oil gas, some coke powder and the asphalitine of carrying out from coke drum, because its proportion is larger, thereby in cyclone separator 10, be separated, for these impurity can be separated from coking oil gas fully, at the top of cyclone separator and squeeze into a small amount of cooled heavy wax tailings with the washing coking oil gas. The impurity of from coking oil gas, separating and be used for flushing high-temperature-coked oil gas after heavy wax tailings then flow into raw material pans 5 through pipeline 14, high-temperature oil gas for fear of cyclone separator 10 seals in raw material pans 5, and pipeline 14 should insert following 2～3 meters of raw material pans liquid level. Mix with heavy wax tailings from pipeline 14 in raw material pans 5 from the fresh coking raw material of the preheating of pipeline 13, then go the radiant section heating of heating furnace through pipeline 3.
Method provided by the invention can improve the working ability of existing delayed coking unit, can produce again preferably heavy wax tailings of quality, and not need high construction investment and operating cost.
The following examples will be further described this method, but therefore not limit this method.
Comparative Examples 1
The situation of conventional delay coking process is adopted in the explanation of this Comparative Examples.
Vacuum residuum feed enters fractionating column after the preheating of heating furnace convection section, after the high-temperature-coked oil gas heat exchange of Ta Nei and coke drum, flow into the bottom of fractionating column, heavy wax tailings is 0.4: 1 to the part by weight of fresh vacuum residuum feed, Fractionator Bottom oil is extracted out with hot oil pump, enter the coke drum coking after the heating furnace radiant section is heated to 500 ℃, the high-temperature oil gas that coking produces then enters fractionating column and separates.
Product distributes, the character of wax tailings is listed in respectively table 2, table 3.
Comparative Examples 2
The situation of the delay coking process of zero recycle ratio is adopted in the explanation of this Comparative Examples.
The vacuum residuum feed identical with Comparative Examples 1 by interchanger and coke chemicals indirect heat exchange after, after process furnace is heated to 500 ℃, enter the coke drum coking, the high-temperature oil gas that coking produces then enters separation column and separates.
The relative working ability of device, product distribute, the character of wax tailings is listed in table 1, table 2, table 3 respectively.Working ability in conventional delay coking process is 100%, and the relative working ability of the delayed coking unit of zero recycle ratio is 140%, though working ability is greatly improved the obvious variation of character of heavy wax tailings.
Embodiment
The situation of low recycle ratio delay coking process provided by the invention is adopted in the present embodiment explanation.
The vacuum residuum feed identical with Comparative Examples 1 is heated to 360 ℃ through the convection zone of process furnace earlier, incoming stock tundish, after coking raw material heavy wax tailings oily and from cyclonic separator mixed by weight 0.08: 1 in the raw material tundish, the radiation section that enters process furnace is heated to 500 ℃, enter coke drum and carry out coking, the coke that coking generates is stayed in the coke drum; The coking oil gas that coking generates enters cyclonic separator with tangential way, and at a small amount of cooled heavy wax tailings of the top of cyclonic separator injection, coking oil gas is 1 minute in the residence time of cyclonic separator, temperature is 430 ℃, the coke powder and the bituminous matter of carrying in the high-temperature-coked oil gas are separated, coking oil gas after the purification enters in the separation column, separate obtaining dry gas, gasoline, diesel oil, light wax tailings, heavy wax tailings, enter cyclonic separator after the wherein heavy on a small quantity wax tailings cooling; The then incoming stock tundish of heavy wax tailings that the coke powder of separating from coking oil gas, bituminous matter and being used to washed behind the high-temperature-coked oil gas mix with fresh coking raw material oil, enter radiation section, the coke drum of process furnace successively.
The relative working ability of device, product distribute, the character of wax tailings is listed in table 1, table 2, table 3 respectively.Working ability in conventional delay coking process is 100%, the relative working ability of the delayed coking unit of low recycle ratio is 130%, working ability improves 30%, the character of wax tailings and Comparative Examples 2 are relatively, carbon residue is reduced to 0.42m% by 0.94m%, gum level is reduced to 6.1m% by 9.5m%, and nitrogen content is reduced to 0.43m% by 0.57m%.
Table 1
| Comparative Examples 1 | Comparative Examples 2 | Embodiment | |
| Flow process | Conventional delayed coking | Zero recycle ratio delayed coking | Low recycle ratio delayed coking |
| Relative working ability, % | 100 | 140 | 130 |
Table 2
| Comparative Examples 1 | Comparative Examples 2 | Embodiment | |
| Flow process | Conventional delayed coking | Zero recycle ratio delayed coking | Low recycle ratio delayed coking |
| Recycle ratio | 0.4 | 0 | 0.08 |
| Product distributes, m%＜C 4The total liquid of+loss gasoline, diesel weight wax tailings coke is received | 8.3 15.9 32.3 20.7 22.8 68.9 | 5.9 13.6 24.4 37.2 18.9 75.2 | 6.2 14.0 25.5 35.1 19.2 74.6 |
Table 3
| Comparative Examples 1 | Comparative Examples 2 | Embodiment | |
| Flow process | Conventional delayed coking | Zero recycle ratio delayed coking | Low recycle ratio delayed coking |
| Density, g/cm 3Carbon residue, the m% sulphur content, the m% nitrogen content, m% C/H atomic ratio stable hydrocarbon, m% aromatic hydrocarbons, the m% colloid, m% | 0.888 0.33 0.65 0.41 1.70 64.5 29.8 5.7 | 0.911 0.94 0.80 0.57 1.63 55.3 35.2 9.5 | 0892 0.42 0.69 0.43 1.68 62.4 31.5 6.1 |
Claims (2)
1, a kind of coking delay process of low recycle ratio comprises:
1), fresh coking raw material oil is heated to 350 ℃～370 ℃ through the convection zone of process furnace earlier, incoming stock tundish, in the raw material tundish coking raw material oil with from coke powder, the bituminous matter of cyclonic separator and to be used to wash temperature be after heavy wax tailings behind 420 ℃～460 ℃ the high-temperature-coked oil gas mixes, the radiation section that enters process furnace is heated to 490 ℃～500 ℃, enter coke drum and carry out coking, the coke that coking generates is stayed in the coke drum;
2), the coking oil gas that coking generates enters cyclonic separator with tangential way, coking oil gas is 10 seconds to 5 minutes in the residence time of cyclonic separator, temperature is 420 ℃～460 ℃, and at the cold heavy wax tailings of the top of cyclonic separator injection from separation column, the coke powder and the bituminous matter of carrying in the high-temperature-coked oil gas are separated, coking oil gas after the purification enters in the separation column, separate and obtain dry gas, gasoline, diesel oil, light wax tailings, heavy wax tailings, enter above-mentioned cyclonic separator after the wherein heavy on a small quantity wax tailings cooling, the weight ratio of cold heavy wax tailings and fresh feed oil is 0.05～0.1: 1;
3), the then incoming stock tundish of heavy wax tailings that wash behind the high-temperature-coked oil gas of coke powder, the bituminous matter separated from coking oil gas and being used to mix with fresh coking raw material oil, enter radiation section, the coke drum of process furnace successively.
2, according to the method for claim 1, it is characterized in that coking oil gas is 30 seconds to 1 minute in the residence time of cyclonic separator, temperature is 425 ℃～435 ℃.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01134273 CN1212369C (en) | 2001-10-30 | 2001-10-30 | Delayed coking process with low circulation ratio |
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| CN 01134273 CN1212369C (en) | 2001-10-30 | 2001-10-30 | Delayed coking process with low circulation ratio |
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| CN1417293A CN1417293A (en) | 2003-05-14 |
| CN1212369C true CN1212369C (en) | 2005-07-27 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104046383A (en) * | 2013-03-17 | 2014-09-17 | 中国石油化工股份有限公司 | Delayed coking process and device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101445744B (en) * | 2008-12-25 | 2013-03-27 | 上海华畅环保设备发展有限公司 | Method for removing coke powder in raw oil and device thereof |
| 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 |
| 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 |
| 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 |
| CN104449830B (en) * | 2013-09-16 | 2017-01-25 | 中国石油化工股份有限公司 | Coking delaying method |
| CN104449829B (en) * | 2013-09-16 | 2017-01-25 | 中国石油化工股份有限公司 | Coking delaying method |
| CN105985796B (en) * | 2015-01-29 | 2017-11-28 | 中国石油化工股份有限公司 | A kind of delayed coking method |
| CN106520181A (en) * | 2016-11-08 | 2017-03-22 | 中石化炼化工程（集团）股份有限公司 | Method and device for delayed coking of heavy oil |
| CN106433740A (en) * | 2016-11-08 | 2017-02-22 | 中石化炼化工程（集团）股份有限公司 | Delayed coking method and apparatus for heavy oil |
| CN113058332B (en) * | 2021-03-01 | 2022-10-11 | 上海灿越化工科技有限公司 | Method and device for removing coke powder in delayed coking fractionating tower |
-
2001
- 2001-10-30 CN CN 01134273 patent/CN1212369C/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104046383A (en) * | 2013-03-17 | 2014-09-17 | 中国石油化工股份有限公司 | Delayed coking process and device |
| CN104046383B (en) * | 2013-03-17 | 2016-01-13 | 中国石油化工股份有限公司 | A kind of processing method of delayed coking and device |
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| CN1417293A (en) | 2003-05-14 |
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