CN1286947C - Dalayed coking method of ungraded materials - Google Patents
Dalayed coking method of ungraded materials Download PDFInfo
- Publication number
- CN1286947C CN1286947C CN 03102271 CN03102271A CN1286947C CN 1286947 C CN1286947 C CN 1286947C CN 03102271 CN03102271 CN 03102271 CN 03102271 A CN03102271 A CN 03102271A CN 1286947 C CN1286947 C CN 1286947C
- Authority
- CN
- China
- Prior art keywords
- coking
- oil
- coke
- time period
- raw material
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Landscapes
- Coke Industry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a delayed coking method of inferior raw materials. A coking period is divided into three time periods, distillate oil is heated to 200 to 490 DEG C by a heating furnace and enters a coke tower in the first time period of the coking period; in the second time period of the coking period, the distillate oil is converted into inferior raw materials and is heated by the heating furnace to 200 to 490 DEG C, and then the inferior raw materials enter the coke tower; in the third time period of the coking period, the inferior raw materials are converted into the distillate oil and are heated by the heating furnace to 490 to 530 DEG C, and then the distillate oil enters the coke tower; coke generated in the reaction stays in the coke tower, and generated coking oil gas enters a fractionation tower for further separation so as to obtain coking gas, coking gasoline, coking diesel oil and coking gas oil; the tower is changed when the coking period ends so as to go on the next coking period and repeat processes. Compared with conventional methods for processing the inferior raw materials, the method basically increases no energy consumption, and operation cycles of a furnace tube of the heating furnace is extended.
Description
Technical field
The invention belongs to a kind of under the situation that does not have hydrogen the thermal non-catalytic cracking technology of hydrocarbon ils, more particularly, be a kind of delayed coking method of inferior raw material.
Background technology
Because investment and process cost are low, can become heavy oil conversion products such as costly liquid and refinery coke, delayed coking still is to be subjected to the Heavy Oil Processing Technology that people generally pay attention to.In the actual procedure, people run into such technical barrier, be that the coking raw material quality is too poor, be mixed with the gilsonite that pitch more than 5% such as propane deasphalting device are produced as asphalt content up to the raw material more than 5% or coking raw material, existing delayed coking unit faces processing difficulties, though can adopt measures such as improving recycle ratio to adapt to such inferior raw material, amount of finish descends, the energy consumption height but exist, and bituminous matter green coke speed occurs and is directed at shortcomings such as the heating furnace tube coking is fast, operational cycle shortening soon.Utilize coker, do not improving substantially under the condition of energy consumption, how to operate and process special poor residuum be a problem with practical value to long period.Process special poor residuum or even bituminous related work patent is not seen patent report with coker.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of delayed coking method of inferior raw material, substantially do not improving under the condition of energy consumption, utilize common delayed coking unit, adopt operating method such as different temperature, pressure, the inferior raw material of the high asphalt content of long period ground processing.
Method provided by the invention comprises: a coking cycle is divided into three time periods, a described coking cycle is 16～48 hours, very first time section accounts for 1～10% of this coking cycle, second time period accounted for 50～74% of this coking cycle, the 3rd time period accounted for 25～40% of this coking cycle, a coking cycle very first time section, distillate enters coke drum after process furnace is heated to 200 ℃～490 ℃, in very first time section, the furnace outlet temperature is 200～490 ℃, coke tower top pressure 0.1～1.0MPa, recycle ratio is 0～1.0, water filling is 0～2 heavy %; In this second time period of coking cycle, distillate is changed to inferior raw material, after being heated to 200 ℃～490 ℃, process furnace enters coke drum, in second time period, the furnace outlet temperature is 200～490 ℃, coke tower top pressure 0.1～1.0MPa, recycle ratio is 0～0.2, and water filling is 0～5 heavy %; In this 3rd time period of coking cycle, inferior raw material is changed to distillate, after being heated to 490 ℃～530 ℃, process furnace enters coke drum, in the 3rd time period, the furnace outlet temperature is 490～530 ℃, coke tower top pressure 0.1～1.0MPa, recycle ratio is 0～1.0, water filling is 0～2 heavy %, and the coke that reaction generates is stayed in the coke drum, and the coking oil gas of generation goes separation column further to separate and obtains cooking gas, coker gasoline, coker gas oil and coker gas oil; This coking cycle changes tower when finishing, and enters next coking cycle, repeats said process, and the described inferior raw material of this method is crude oil, residual oil, pitch or its mixture of asphalt content greater than 5 heavy %.
The present invention utilizes inferior raw material low temperature little by the furnace coking tendency, distillate high temperature is difficult for the principle of coking by process furnace, this method is compared with the ordinary method of operating by less recycle ratio, and energy consumption does not increase substantially, has prolonged the operational cycle of heating furnace tube; In other words, this method with by comparing than the ordinary method of operation than systemic circulation, under identical situation of the operational cycle of heating furnace tube, reduced energy consumption.
Description of drawings
Accompanying drawing is the delayed coking method synoptic diagram of inferior raw material provided by the invention.
Embodiment
Method provided by the invention is so concrete enforcement:
A coking cycle is divided into three time periods, and a coking cycle very first time section, distillate enters coke drum after process furnace is heated to 200 ℃～490 ℃; In this second time period of coking cycle, distillate is changed to inferior raw material, after being heated to 200 ℃～490 ℃, process furnace enters coke drum; In this 3rd time period of coking cycle, inferior raw material is changed to distillate, after being heated to 490 ℃～530 ℃, process furnace enters coke drum, the coke that reaction generates is stayed in the coke drum, and the coking oil gas of generation goes separation column further to separate and obtains cooking gas, coker gasoline, coker gas oil and coker gas oil; This coking cycle changes tower when finishing, and enters next coking cycle, repeats said process.
The coke drum outer wall is established thermal insulation layer, the operation coke drum fills burnt behind suitable height, change the tower operation, change coking raw material and advance second coke drum, the origin operation coke drum carries out cold Jiao and decoking operation, to change tower be a coking operation cycle to each coke drum to being full of coke from feed switched, and a coking cycle is 16～48 hours.Similar with last coking cycle, in the very first time section that next coking cycle begins, still with distillate as charging, after process furnace is heated to 200 ℃～490 ℃, enter coke drum; In second time period, distillate is changed to inferior raw material, after being heated to 200 ℃～490 ℃, inferior raw material enters coke drum; In the 3rd time period, inferior raw material is changed to distillate, this distillate enters the coke drum reaction after coking heater is heated to 490 ℃～530 ℃.
Described inferior raw material is crude oil, residual oil, pitch or its mixture of asphalt content greater than 5 heavy % best 5～50 heavy % (N.heptane insolubles), as mixes bituminous residual oil, and its asphalt content can be used as inferior raw material of the present invention greater than 5 heavy %.The coker gas oil that described distillate is coker gas oil that this device produces or other coker, coker gas oil, straight run gas oil or its mixture.
A described coking cycle is 16～48 hours, and the 50～74%, the 3rd time period that 1～10%, second time period that very first time section accounts for this coking cycle accounts for this coking cycle accounts for 25～40% of this coking cycle.In very first time section, the furnace outlet temperature is 200～490 ℃, coke tower top pressure 0.1～1.0MPa, and recycle ratio is 0～1.0, water filling is 0～2 heavy %.In second time period, the furnace outlet temperature is 200～490 ℃, coke tower top pressure 0.1～1.0MPa, and recycle ratio is 0～0.2, water filling is 0～5 heavy %.In the 3rd time period, the furnace outlet temperature is 490～530 ℃, coke tower top pressure 0.1～1.0MPa, and recycle ratio is 0～1.0, water filling is 0～2 heavy %.
The 3rd time period finishes to be one-period and finishes, the operation coke drum fills burnt behind suitable height, change the tower operation, change distillate and advance second coke drum, the origin operation coke drum carries out cold Jiao and decoking operation, after displacement tower to be installed finished, the inferior raw material that again distillate is gained high asphalt content repeated said process as charging.Said process makes the big flow of inferior raw material low temperature of the high asphalt content of easy coking pass through process furnace, make distillate (coker gas oil, coker gas oil or the straight run gas oil) high temperature that is difficult for coking by process furnace, for the inferior raw material of high asphalt content react the heat that necessity is provided in coke drum.The total energy consumption of apparatus of the present invention is not compared with ordinary method and is improved, and has slowed down the coking tendency of process furnace, has guaranteed the amount of finish and the required heat of material reaction of device.
Method provided by the invention is applicable to a Lu Erta, two Lu Sita and three stoves, six tower flow processs.For two stove four-column process flows, wherein a stove two towers are processed common residual oil by common flow process and operational condition, another stove two towers are processed the inferior raw material of high asphalt content by this method, this raw material or the distillate (coker gas oil, coker gas oil or straight run gas oil) that is difficult for coking are through laggard process furnace convection current of heat exchange and radiation section, be heated to the coke drum of the laggard correspondence of temperature of reaction, its reaction oil gas advances separation column.Two stoves, four towers are established a coking fractional distillation column, and the reaction oil gas that a utilization stove two towers are wherein processed common residual oil generation comes the mass flow of HYDROGEN ISOTOPE EQUILIBRIUM FRACTIONATION BETWEEN tower to fluctuate.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.
Accompanying drawing is an inferior raw material delayed coking method synoptic diagram provided by the invention.This figure is a stove two tower flow processs, is an operational cycle by 24 hours.But therefore do not limit two Lu Sita and three stoves, six towers and use the inventive method.
The flow process of this method is described below: a coking cycle very first time section, distillate enters surge tank 2 through pipeline 14 earlier, enter the bottom and the heat exchange of coking oil gas part of coking fractional distillation column 11 then through pipeline 3, after pipeline 4 enters coking heater 5 heating, enter coke drum 7 respectively with turning oil through pipeline 6; In second time period of this coking cycle, coking raw material is changed to inferior raw material, this inferior raw material enters surge tank 2 through pipeline 1 earlier, enter the bottom and the heat exchange of coking oil gas part of coking fractional distillation column 11 then through pipeline 3, with turning oil after pipeline 4 enters coking heater 5 heating, enter coke drum 7 respectively through pipeline 6, pyrogenic reaction takes place in coke drum; In this 3rd time period of coking cycle, inferior raw material is changed to distillate, this distillate enters surge tank 2 through pipeline 14 earlier, enter the bottom and the heat exchange of coking oil gas part of coking fractional distillation column 11 then through pipeline 3, with turning oil after pipeline 4 enters coking heater 5 heating, enter coke drum 7 reactions respectively through pipeline 6, the coke that generates is stayed in the coke drum, coking oil gas enters coking fractional distillation column 11 through pipeline 10, isolated cooking gas, coker gasoline, coker gas oil, coker gas oil is respectively through pipeline 12,13,15,16 derive, and coking recycle oil returns coking system; This coking cycle changes the tower operation when finishing, distillate or inferior raw material heating enter next coking cycle after pipeline 8 enters another coke drum 9, repeat said process.
The present invention utilizes inferior raw material low temperature little by the furnace coking tendency, distillate high temperature is difficult for the principle of coking by process furnace, this method is compared with the ordinary method of operating by less recycle ratio, and energy consumption does not increase substantially, has prolonged the operational cycle of heating furnace tube; In other words, this method with by comparing than the ordinary method of operation than systemic circulation, under identical situation of the operational cycle of heating furnace tube, reduced energy consumption.
The following examples will give further instruction to present method, but therefore not limit present method.
Comparative Examples 1
This Comparative Examples is by less recycle ratio 0.4 operation, and inferior raw material is that asphalt content is the crude oil with poor quality of 12.8 heavy %, and its character is as shown in table 1, and the weight ratio of turning oil and crude oil with poor quality is 0.4.Operational condition, operational cycle, energy consumption and product distribute and see Table 2.Test-results shows that the operational cycle is 90 days, and energy consumption is the 987.7MJ/t raw material.
Comparative Examples 2
This Comparative Examples is by operating than 1.0 than systemic circulation, and inferior raw material is identical with Comparative Examples 1, and the weight ratio of turning oil and crude oil with poor quality is 1.0.Operational condition, operational cycle, energy consumption and product distribute and see Table 2.Test-results shows that the operational cycle is 330 days, and energy consumption is the 1361.2MJ/t raw material.
Embodiment
Present embodiment carries out according to the flow process of accompanying drawing, inferior raw material is identical with Comparative Examples 1, coking cycle very first time section, second time period, the 3rd time period were respectively 1 hour, 16 hours, 7 hours, and the coking raw material of three time periods is respectively coker gas oil, crude oil with poor quality, coker gas oil.Operational condition, operational cycle, energy consumption and product distribute and see Table 2.As can be seen from Table 2, the operational cycle is 330 days, and energy consumption is the 989.2MJ/t raw material.Compare with Comparative Examples 1, the embodiment energy consumption is suitable, but the operational cycle increases by 240 days; Compare with Comparative Examples 2, the embodiment operational cycle is identical, but energy consumption reduces by 27%.
Table 1
| Material name | Crude oil with poor quality | Coker gas oil |
| Feedstock property | ||
| Proportion (15 ℃/4 ℃) | 0.9854 | 0.9012 |
| Bituminous matter (N.heptane insolubles), heavy % | 12.8 | 0.2 |
| Aromatic hydrocarbons and colloid, heavy % | 51.1 | 33.5 |
| Carbon residue, heavy % | 15.79 | 0.68 |
| Ash content, heavy % | 0.08 | 0.01 |
| Sulphur content, heavy % | 2.09 | 0.36 |
| Kinematic viscosity (100 ℃), mm 2/s | 873.5 | 4.4 |
Table 2
| Comparative Examples 1 | Comparative Examples 2 | Embodiment | |||
| Operational cycle, h | 24 | 24 | 24 | ||
| 1 | 16 | 7 | |||
| Coking raw material | Crude oil with poor quality | Crude oil with poor quality | Coker gas oil | Crude oil with poor quality | Coker gas oil |
| The furnace outlet temperature, ℃ | 500 | 500 | 490 | 420 | 520 |
| Recycle ratio | 0.4 | 1.0 | 0 | 0 | 0 |
| Water filling, heavy % | 3 | 3 | 1.5 | 1.5 | 1.5 |
| Coke tower top pressure (table), MPa | 0.15 | 0.15 | 0.15 | 0.15 | 0.15 |
| Energy consumption, the kJ/t raw material | 987.7 | 1361.2 | 989.2 | ||
| Operational cycle, day | 90 | 330 | 330 | ||
| Product distributes, heavy % | |||||
| Cooking gas | 6.3 | 7.5 | 6.4 | ||
| Coker gasoline | 14.5 | 18.4 | 14.7 | ||
| Coker gas oil | 29.4 | 40.4 | 30.6 | ||
| Coker gas oil | 22.6 | 5.2 | 20.8 | ||
| Coke | 25.2 | 26.5 | 25.5 | ||
| Get rid of oil and loss | 2.0 | 2.0 | 2.0 | ||
Claims (2)
1, a kind of delayed coking method of inferior raw material, it is characterized in that a coking cycle is divided into three time periods, a described coking cycle is 16～48 hours, very first time section accounts for 1～10% of this coking cycle, second time period accounted for 50～74% of this coking cycle, the 3rd time period accounted for 25～40% of this coking cycle, a coking cycle very first time section, distillate enters coke drum after process furnace is heated to 200 ℃～490 ℃, in very first time section, the furnace outlet temperature is 200～490 ℃, coke tower top pressure 0.1～1.0MPa, recycle ratio is 0～1.0, and water filling is 0～2 heavy %; In this second time period of coking cycle, distillate is changed to inferior raw material, after being heated to 200 ℃～490 ℃, process furnace enters coke drum, in second time period, the furnace outlet temperature is 200～490 ℃, coke tower top pressure 0.1～1.0MPa, recycle ratio is 0～0.2, and water filling is 0～5 heavy %; In this 3rd time period of coking cycle, inferior raw material is changed to distillate, after being heated to 490 ℃～530 ℃, process furnace enters coke drum, in the 3rd time period, the furnace outlet temperature is 490～530 ℃, coke tower top pressure 0.1～1.0MPa, recycle ratio is 0～1.0, water filling is 0～2 heavy %, and the coke that reaction generates is stayed in the coke drum, and the coking oil gas of generation goes separation column further to separate and obtains cooking gas, coker gasoline, coker gas oil and coker gas oil; This coking cycle changes tower when finishing, and enters next coking cycle, repeats said process, and the described inferior raw material of this method is crude oil, residual oil, pitch or its mixture of asphalt content greater than 5 heavy %.
2,, it is characterized in that described distillate is coker gas oil, coker gas oil, straight run gas oil or its mixture according to the method for claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03102271 CN1286947C (en) | 2003-01-30 | 2003-01-30 | Dalayed coking method of ungraded materials |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03102271 CN1286947C (en) | 2003-01-30 | 2003-01-30 | Dalayed coking method of ungraded materials |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1521235A CN1521235A (en) | 2004-08-18 |
| CN1286947C true CN1286947C (en) | 2006-11-29 |
Family
ID=34281657
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03102271 Expired - Lifetime CN1286947C (en) | 2003-01-30 | 2003-01-30 | Dalayed coking method of ungraded materials |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1286947C (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103102986B (en) * | 2011-11-10 | 2015-05-13 | 中国石油化工股份有限公司 | Combined process of hydrotreatment and delayed coking for residual oil |
-
2003
- 2003-01-30 CN CN 03102271 patent/CN1286947C/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| CN1521235A (en) | 2004-08-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101597518B (en) | Improved delayed coking process | |
| CN106811234B (en) | A kind of delayed coking system and method | |
| CN101591561A (en) | A kind of delay coking process | |
| CN102295943A (en) | Method for coking needle coke by large recycle ratio oil system | |
| CN103555363A (en) | High-acid-content raw material oil hydrogen-donating delayed coking method | |
| CN1142247C (en) | Dalayed coking method of deoiled asphalt | |
| CN104673372B (en) | A kind of method improving delayed coking product slates | |
| CN1286947C (en) | Dalayed coking method of ungraded materials | |
| CN102373080A (en) | Coking delaying method | |
| CN104164254A (en) | Heavy oil processing process | |
| CN208949197U (en) | A kind of needle coke process units | |
| CN103215062A (en) | Delay coking processing method of inferior residual oil | |
| CN103805226B (en) | A kind of delayed coking method | |
| CN104164253A (en) | Heavy oil processing method | |
| CN1317358C (en) | Improved delayed coking method | |
| CN1323130C (en) | Hydro-delayed coking method | |
| CN1068623C (en) | Method for inhibiting coke generation of heating-furnace | |
| CN1151232C (en) | Method for regulating heat balance of catalytic conversion technological reaction-regeneration system | |
| CN1276963C (en) | High-yield chemical light oil delayed coking method | |
| CN209383711U (en) | The full fraction ethylene bottom oil delayed coking production system of non-impurity-doped | |
| CN209636177U (en) | A kind of light tar mixes refining wax oil processing unit (plant) | |
| CN101643658A (en) | Process for producing heavy bitumen and fuel oil | |
| CN1238470C (en) | Improved delayed coking process for increasing yield of gasoline and diesel oil | |
| CN108251143B (en) | Method for preparing asphalt coke by adopting tower bottom asphalt | |
| CN1206318C (en) | Delayed coking method capable of reducing coked gas oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20061129 |