CN101724436B - Thermal cracking method for reducing viscosity and condensation point of extra-heavy crude oil - Google Patents
Thermal cracking method for reducing viscosity and condensation point of extra-heavy crude oil Download PDFInfo
- Publication number
- CN101724436B CN101724436B CN 200810224024 CN200810224024A CN101724436B CN 101724436 B CN101724436 B CN 101724436B CN 200810224024 CN200810224024 CN 200810224024 CN 200810224024 A CN200810224024 A CN 200810224024A CN 101724436 B CN101724436 B CN 101724436B
- Authority
- CN
- China
- Prior art keywords
- extra
- vacuum
- distillate
- oil
- accordance
- 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.)
- Active
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a thermal cracking method for reducing the viscosity and the condensation point of extra-heavy crude oil, comprising the following steps: separating the extra-heavy crude oil into ordinary pressure distillate oil, vacuum distillate oil and vacuum residuum through distillation; respectively carrying out high-temperature thermal cracking for the vacuum distillate oil and mitigated thermal treatment for the vacuum residuum; and mixing all liquid distillates and liquid products so as to obtain synthetic crude oil. The synthetic crude oil prepared by the thermal cracking method has high yield coefficient, low viscosity and condensation point and high stability.
Description
Technical field
The present invention relates to a kind of method for thermal cracking that reduces extra-heavy oil viscosity and condensation point, belong in the situation that there is not the thermal non-catalytic cracking of hydrogen hydrocarbon ils.
Background technology
Along with the worsening shortages of conventional crude resource, the development and utilization of non-conventional oil resource seems more and more important, and the heavy crude particularly produced quantity of extra-heavy oil increases year by year.The viscosity of extra-heavy oil is large, condensation point is high, be difficult to carry out pipeline and carry, serious restriction the further development and use of extra-heavy oil.
Satisfy pipeline and carry requirement, must effectively reduce viscosity and the condensation point of extra-heavy oil, a kind of simple method is to mix light crude or outsourcing thinner in extra-heavy oil, but the method is subject to the restriction that incorporation is large, light crude is short and outsourcing thinner cost is high, and the method for mixing simultaneously light crude or thinner in the extra-heavy oil does not meet the requirement of modern refining of petroleum yet.Another kind method is to add emulsifying agent in extra-heavy oil, forms oil-in-water type emulsified oil, and its viscosity and condensation point can satisfy pipeline and carry requirement, but the oil in water emulsion temperature influence is larger, is prone to demulsifying phenomenon, causes extra-heavy oil to separate out blocking pipe.In addition, the price of emulsifying agent is high, consumption is large, and economy is relatively poor.
Set up on the spot extra-heavy oil deep processing device in the oil field, can produce and satisfy lightweight synthetic crude or the light weight fluid petroleum products that pipeline is carried requirement, the shortcoming of the method is that facility investment, operation and maintenance cost are higher, and is unreasonable economically.
Set up the simple extra-heavy oil modifying apparatus of a cover in the oil field, low sticking, the crude oil of low-coagulation of its production can directly or by mixing a small amount of thinner satisfy the requirement that pipeline is carried.The facility investment of the method and Operation and Maintenance expense are low, and better economy is the direction that solves at present the extra-heavy oil difficulty of transportation.The technique of viscosity breaking and thermally splitting is simple, facility investment and process cost are lower, is a kind of technology that is suitable in the oil field extra-heavy oil being carried out elementary processing.
CN1325605C discloses a kind for the treatment of process of oil sands bitumen, and the method is the combination process of a kind of viscosity breaking and solvent deasphalting, and it is to the not restriction of order of viscosity breaking and solvent deasphalting.Produce outer output oil after the visbreaking oil that finally obtains mixes with atmospheric distillate, de-oiled asphalt can be used for producing steam and synthetic gas.The viscosity breaking condition is 350～500 ℃ of temperature, pressure 0.3～15MPa, and the residence time is 1～6h.The method need to be deviate from bituminous matter could satisfy the crude pipeline transportation requirement, and its synthetic crude yield is lower; Although de-oiled asphalt can be used for gasifying process, equipment for gasification investment and process cost are higher, and economy is relatively poor.
US2006/0144754A1 discloses a kind of method from heavy crude production pipeline oil.The method at first is divided into two portions with raw material, and a part of raw material is divided into distillate and residual oil by distillation; Residual oil is carried out thermally splitting, and the thermally splitting product is divided into cracking benzoline, cracking intermediate oil and pressure fuel by distillation; Can again carry out thermally splitting and fractionation by distillation to the cracking intermediate oil; Distillate in the above steps, cracking benzoline and another part raw material are mixed, obtain synthetic crude, pressure fuel can be used for generating or produces heat energy.The method technical process is complicated, need to deviate from thermally splitting heavy oil and could satisfy the crude pipeline transportation requirement, and its synthetic crude yield is lower.
In sum, the all or part of heavy component that prior art must be deviate from raw material just can be produced and meet the synthetic crude that crude pipeline transportation requires, not only lost the synthetic crude yield, and the heavy component of deviating from there is not preferably the treatment process with economy yet in relatively remote oil field.
Summary of the invention
The technical problem to be solved in the present invention provides a kind of method for thermal cracking that reduces extra-heavy oil viscosity and condensation point, and the method can be produced to greatest extent and be satisfied the synthetic crude that pipeline is carried requirement.
All pressure all refer to gauge pressure among the present invention.
A kind of method for thermal cracking that reduces extra-heavy oil viscosity and condensation point may further comprise the steps:
(1) extra-heavy oil often, underpressure distillation, be divided into atmospheric distillate, vacuum distillate and vacuum residuum;
(2) vacuum distillate carries out heat cracking reaction under 480～550 ℃, 0.4～2.0MPa and reaction times 1～10min;
(3) vacuum residuum relaxes thermal treatment under 380～420 ℃, 0～1.0MPa and reaction times 1～3h;
(4) product liquid in the atmospheric distillate in (1) and (2), (3) is mixed, obtain synthetic crude.
Density 〉=0.950g/cm when described extra-heavy oil refers to 20 ℃
3, viscosity 〉=10000mm in the time of 50 ℃
2The heavy crude of/s; Density 〉=0.980g/cm 20 ℃ time the particularly
3Heavy crude.
Atmospheric flashing and vacuum flashing are preferably adopted in described normal, underpressure distillation.
The boiling point of described atmospheric distillate is no more than 350 ℃, the highlyest is no more than 400 ℃; The boiling point of vacuum distillate is no more than 500 ℃, the highlyest is no more than 550 ℃.
In the step (2), reactor preferably adopts boiler tube formula reactor.
In the step (3), reactor preferably adopts tower reactor.
Compared with prior art, the present invention has the following advantages:
(1) viscosity of crude of producing is low, condensation point is low, stability is high, can satisfy the requirement that pipeline is carried.Viscosity can reduce by 80～95%, and condensation point can reduce by 10～30 ℃.
(2) the synthetic crude yield is high.
(3) adopt boiler tube formula reactor to carry out the high temperature heat cracking reaction of vacuum distillate, process furnace is long running period, and boiler tube decoking frequency is low.Adopt tower reactor to carry out the mitigation thermal treatment of vacuum residuum, owing to adopt the processing mode of low temperature long residence time, the basic noncoking of Delayed Visbreaking reaction tower, device is long running period.
Description of drawings
Accompanying drawing is the schematic flow sheet of the inventive method.
Wherein, 2-atmospheric pressure kiln, 3-atmospheric flash tower, the 6-process furnace that reduces pressure, 7-vacuum flasher, 9-tower reactor, 12-boiler tube formula reactor, 14-cracking flashing tower.
Embodiment
Elaborate method of the present invention below in conjunction with accompanying drawing.
Extra-heavy oil enters atmospheric pressure kiln 2 by pipeline 1, enters atmospheric flash tower 3 after being heated to 370 ℃; In atmospheric flash tower 3, extra-heavy oil is separated into atmospheric distillate and long residuum, long residuum enters decompression process furnace 6 through pipeline 5, enters vacuum flasher 7 after being heated to 380～420 ℃; In vacuum flasher 7, long residuum is separated into vacuum distillate and vacuum residuum; Vacuum residuum enters in the tower reactor 9 through pipeline 8, and temperature of reaction is 380～420 ℃, and reaction pressure is 0～1.0MPa, and the reaction times is 1～3h; Vacuum distillate enters boiler tube formula reactor 12 through pipeline 11, temperature of reaction is 480～550 ℃, reaction pressure is 0.4～2.0MPa, reaction times is 1～10min, furnace tubing can adopt online coke cleaning or on-line decoking technology to remove coking, the oil gas of pyrolytic cracking enters cracking flashing tower 14 after lowering the temperature from the quenching oil of pipeline 13, be separated into thermally splitting light oil and thermally splitting heavy oil through cracking flashing tower 14; Will be from the atmospheric distillate of pipeline 4, from the visbreaker tar of pipeline 10, mix from the thermally splitting light oil of pipeline 15 with from the thermally splitting heavy oil of pipeline 16, obtain synthetic crude.
Further specify by the following examples method of the present invention.The character of used extra-heavy oil sees Table 1 among the embodiment.
Table 1
Stability is divided into 5 grades by rank, and higher its stability of progression is poorer, carries for the standing storage and the pipeline that satisfy oil product, generally needs the stability of control oil product to be no more than 2 grades.
Comparative Examples 1
Extra-heavy oil is after the normal pressure flash distillation, and long residuum adopts the processing of boiler tube formula viscosity breaking technology, and the furnace outlet temperature is 480 ℃, and reaction pressure is 0.4MPa, and the reaction times is 2min.The crude oil of producing after atmospheric distillate mixes with visbreaker tar is 275.2mm 80 ℃ kinematic viscosity
2/ s, condensation point is 10 ℃, stability reaches 2 grades.Be 3 months the running period of boiler tube formula reactor.
Comparative Examples 2
Extra-heavy oil is after the normal pressure flash distillation, and long residuum enters and enters vacuum flasher after the decompression process furnace is heated to 400 ℃.The vacuum residuum of extracting out at the bottom of the vacuum flasher enters into tower reactor, carries out the mitigation thermal treatment of 2h, and temperature of reaction is 395 ℃, and pressure is 0.2MPa.The crude oil of producing after atmospheric distillate, vacuum distillate and visbreaker tar mix is 664.8mm 80 ℃ kinematic viscosity
2/ s, condensation point is 15 ℃, stability reaches 1 grade.Can reach more than 36 months the running period of tower reactor.
Extra-heavy oil is after the normal pressure flash distillation, and long residuum enters and enters vacuum flasher after the decompression process furnace is heated to 390 ℃.The vacuum residuum of extracting out at the bottom of the vacuum flasher enters into tower reactor, carries out the mitigation thermal treatment of 2.5h, and temperature of reaction is 385 ℃, and pressure is 0.2MPa.Vacuum distillate enters into boiler tube formula reactor and carries out heat cracking reaction, and temperature of reaction is 500 ℃, and reaction pressure is 0.4MPa, and the reaction times is 4min.The crude oil of producing after atmospheric distillate, visbreaker tar, thermally splitting light oil and thermally splitting heavy oil mix is 185.5mm 80 ℃ kinematic viscosity
2/ s, condensation point is 8 ℃, stability reaches 1 grade.Be 18 months the running period of boiler tube formula reactor.
Extra-heavy oil is after the normal pressure flash distillation, and long residuum enters and enters vacuum flasher after the decompression process furnace is heated to 410 ℃.The vacuum residuum of extracting out at the bottom of the vacuum flasher enters into tower reactor, carries out the mitigation thermal treatment of 1.5h, and temperature of reaction is 405 ℃, and pressure is 0.2MPa.Vacuum distillate enters into boiler tube formula reactor and carries out heat cracking reaction, and temperature of reaction is 530 ℃, and reaction pressure is 1.0MPa, and the reaction times is 2min.The crude oil of producing after atmospheric distillate, visbreaker tar, thermally splitting light oil and thermally splitting heavy oil mix is 54.35mm 80 ℃ kinematic viscosity
2/ s, condensation point is 2 ℃, stability reaches 2 grades.Be 9 months the running period of boiler tube formula reactor.
Can find out by embodiment and Comparative Examples, the viscosity of the synthetic crude that the inventive method is produced is low, condensation point is low, stability is high, and the running period of boiler tube formula reactor is long.The synthetic crude that the inventive method is produced can satisfy the requirement that the normal temperature pipeline is carried or the low-temperature heat pipeline is carried, and greatly reduces the conveying cost of crude oil.
Claims (9)
1. method for thermal cracking that reduces extra-heavy oil viscosity and condensation point may further comprise the steps:
(1) extra-heavy oil often, underpressure distillation, be divided into atmospheric distillate, vacuum distillate and vacuum residuum, described normal, underpressure distillation is atmospheric flashing and vacuum flashing;
(2) vacuum distillate carries out heat cracking reaction under 480～550 ℃, 0.4～2.0MPa and reaction times 1～10min;
(3) vacuum residuum relaxes thermal treatment under 380～420 ℃, 0～1.0MPa and reaction times 1～3h;
(4) product liquid in the atmospheric distillate in (1) and (2), (3) is mixed, obtain synthetic crude.
2. in accordance with the method for claim 1, it is characterized in that the density 〉=0.950g/cm of described extra-heavy oil
3, viscosity 〉=10000mm
2/ s.
3. in accordance with the method for claim 2, it is characterized in that the density 〉=0.980g/cm of described extra-heavy oil
3
4. in accordance with the method for claim 1, it is characterized in that the boiling point of described atmospheric distillate≤400 ℃.
5. in accordance with the method for claim 4, it is characterized in that the boiling point of described atmospheric distillate≤350 ℃.
6. in accordance with the method for claim 1, it is characterized in that the boiling point of vacuum distillate≤550 ℃.
7. in accordance with the method for claim 6, it is characterized in that the boiling point of vacuum distillate≤500 ℃.
8. in accordance with the method for claim 1, it is characterized in that, step (2) adopts boiler tube formula reactor to carry out heat cracking reaction.
9. in accordance with the method for claim 1, it is characterized in that, step (3) adopts tower reactor to relax thermal treatment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200810224024 CN101724436B (en) | 2008-10-10 | 2008-10-10 | Thermal cracking method for reducing viscosity and condensation point of extra-heavy crude oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200810224024 CN101724436B (en) | 2008-10-10 | 2008-10-10 | Thermal cracking method for reducing viscosity and condensation point of extra-heavy crude oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101724436A CN101724436A (en) | 2010-06-09 |
| CN101724436B true CN101724436B (en) | 2013-01-09 |
Family
ID=42446001
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200810224024 Active CN101724436B (en) | 2008-10-10 | 2008-10-10 | Thermal cracking method for reducing viscosity and condensation point of extra-heavy crude oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101724436B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102277192B (en) * | 2011-07-15 | 2014-01-15 | 中国石油天然气股份有限公司 | Method for lowering viscosity of overweight heavy oil |
| CN102304386B (en) * | 2011-08-12 | 2014-04-02 | 中国石油天然气股份有限公司 | Method for improving storage stability of superheavy thick oil |
| CN110067942B (en) * | 2019-03-07 | 2023-01-06 | 青岛科技大学 | Crude oil heating furnace |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1151430A (en) * | 1995-11-24 | 1997-06-11 | 中国石油天然气管道局 | Method of molecular sieve cracking for modifying, coagulation and viscosity reducing for pipeline crude oil transfer |
| CN1275156A (en) * | 1997-10-15 | 2000-11-29 | 尤尼普瑞公司 | Process for upgrading heavy crude oil production |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001254083A (en) * | 2000-03-10 | 2001-09-18 | Nippon Shoene Kankyo Seihin:Kk | Method and apparatus for removing bromine component in decomposition oil of waste plastics |
-
2008
- 2008-10-10 CN CN 200810224024 patent/CN101724436B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1151430A (en) * | 1995-11-24 | 1997-06-11 | 中国石油天然气管道局 | Method of molecular sieve cracking for modifying, coagulation and viscosity reducing for pipeline crude oil transfer |
| CN1275156A (en) * | 1997-10-15 | 2000-11-29 | 尤尼普瑞公司 | Process for upgrading heavy crude oil production |
Non-Patent Citations (1)
| Title |
|---|
| JP特开2001-254083A 2001.09.18 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101724436A (en) | 2010-06-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101970611B (en) | Process to upgrade heavy oil by hot pressurized water and ultrasonic wave generating pre-mixer | |
| RU2403275C2 (en) | Production refinement of bitumen with common or different solvents | |
| CN101597518B (en) | Improved delayed coking process | |
| CN101591561B (en) | Delayed coking process | |
| CA2878357C (en) | A method for recovering a hyrdocarbon mixture from a subterranean formation | |
| CN105452421A (en) | Method and system for preparing a pipelineable hydrocarbon mixture | |
| CN101724436B (en) | Thermal cracking method for reducing viscosity and condensation point of extra-heavy crude oil | |
| CN104449829B (en) | Coking delaying method | |
| CN107177372B (en) | The suspended bed hydrogenation method and hydrogenation system of heavy oil feedstock | |
| CN101463266B (en) | Viscosity breaking method | |
| CN102220166A (en) | Delayed coking method | |
| CN101892065B (en) | Coal tar processing method | |
| CN101892064A (en) | Coal tar separation method | |
| CA2878343C (en) | A system and a method of recovering and processing a hydrocarbon mixture from a subterranean formation | |
| CN102899079A (en) | Delayed coking method | |
| CN205907221U (en) | Vacuum residue's refining device | |
| CN108251143B (en) | Method for preparing asphalt coke by adopting tower bottom asphalt | |
| RU2456328C2 (en) | Processing method of bituminous sands | |
| CA2878359C (en) | A method and a system of recovering and processing a hydrocarbon mixture from a subterranean formation | |
| CN110747003B (en) | Coke tower and delayed coking method using same | |
| CN109554194B (en) | Cracking device for preparing low-carbon olefin by cracking petroleum hydrocarbon under reduced pressure | |
| CN102911717B (en) | Process and equipment for vacuum distillation | |
| CN106867581A (en) | A kind of method that ultrasonic wave delayed coking processes acid starting material high | |
| CN104449830A (en) | Coking delaying method |
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 |