CN106883873B - A kind of method of modifying low-quality heavy oil viscosity reduction - Google Patents
A kind of method of modifying low-quality heavy oil viscosity reduction Download PDFInfo
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- CN106883873B CN106883873B CN201510931414.0A CN201510931414A CN106883873B CN 106883873 B CN106883873 B CN 106883873B CN 201510931414 A CN201510931414 A CN 201510931414A CN 106883873 B CN106883873 B CN 106883873B
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- oil
- hydrogen supply
- heavy oil
- straight
- viscosity reduction
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A kind of method of modifying low-quality heavy oil viscosity reduction, includes the following steps：Step 1：Inferior heavy oil obtains straight-run oil and decompression residuum through atmospheric and vacuum distillation, includes wherein hydrogen supply agent fraction in straight-run oil；Step 2：Enter hydrogen supply thermal cracking unit after the decompression residuum and all or part of hydrogen supply agent fraction mixing to be reacted, generates gas, distillate and residual oil；Step 3：The residual oil that hydrogen supply heat cracking reaction generates is pumped into solvent deasphalting unit, obtains deasphalted oil and de-oiled asphalt after exchanging heat；And step 4：The distillate mixing that remaining straight-run oil, deasphalted oil and hydrogen supply heat cracking reaction obtain, modification oil of the production API greater than 19.The present invention can maximum production API be greater than 19 modification crude oil, meet storage and manage defeated requirement, invest stability that is low, while guaranteeing modification oil.
Description
Technical field
The present invention relates to a kind of methods of modifying low-quality heavy oil viscosity reduction.
Background technique
Currently, Global Oil residual recoverable reserves is 2,750,200,000,000 barrels, (including conventional oil, heavy oil and oil-sand can adopt storage
Amount), wherein conventional oil is 1,326,000,000,000 barrels, accounts for 48%, and 714,700,000,000 barrels of heavy oil mining resources amount, oil-sand mining resources amount is
709500000000 barrels, heavy oil and oil-sand mining resources amount account for global remaining mining resources amount 52%.Non-conventional oil (such as various viscous crude,
Oil sands bitumen etc.) exploitation ratio will gradually increase, and important one of the strategic making & breaking in China will be become.China's energy
Huge notch will rely primarily on the unconventional energy resource such as viscous crude and oil sands bitumen to make up.This kind of resource mostly use at present SAGD,
The viscosity of the technological development such as CSS and ore mining (oil-sand), extra heavy oil and oil sands bitumen is high, and density is big, does not flow or is difficult under room temperature
Flowing is not able to satisfy the defeated requirement with ocean shipping of oil pipe, needs to reduce viscosity by modification, improve API degree, to meet storage
Deposit and manage defeated requirement.
Modifying low-quality heavy oil mostly uses decarburization technique, and coking is one of common means, but obtained distillate is unstable,
Hydrotreating is needed, investment is high.Exclusive use visbreaking, hydrogen supply thermal cracking are unable to reach the requirement that API degree is greater than 19, and single
Solely API degree is set to reach 19 using solvent deasphalting, oily yield is low, and unit scale is big.
Summary of the invention
The object of the present invention is to provide a kind of methods of modifying low-quality heavy oil viscosity reduction.
To achieve the above object, the present invention provides a kind of method of modifying low-quality heavy oil viscosity reduction, includes the following steps：
Step 1：Inferior heavy oil obtains straight-run oil and decompression residuum through atmospheric and vacuum distillation, wherein in straight-run oil
Include hydrogen supply agent fraction；
Step 2：The decompression residuum enters hydrogen supply thermal cracking unit after mixing with all or part of hydrogen supply agent fraction
It is reacted, generates gas, distillate and residual oil；
Step 3：The residual oil that hydrogen supply heat cracking reaction generates is pumped into solvent deasphalting unit, is taken off after exchanging heat
Coal tar and de-oiled asphalt；And
Step 4：The distillate mixing that remaining straight-run oil, deasphalted oil and hydrogen supply heat cracking reaction obtain, production
Modification oil of the API greater than 19；It is residue that straight-run oil obtained in step 1, which subtracts the hydrogen supply agent fraction used up in step 2,
Straight-run oil.
Wherein, the boiling range of straight-run oil is 500 DEG C hereinafter, wherein the boiling range of hydrogen supply agent fraction includes in the step 1
Between 280~500 DEG C, the boiling range for the hydrogen supply agent fraction that different inferior heavy oils is often evaporated under reduced pressure may be different, supply
Hydrogen agent fraction is the fraction that naphthenic base is more enriched with.
Wherein, in step 1 gained hydrogen supply agent fraction 20~100% be used for step 2 hydrogen supply heat cracking reaction.
Wherein, decompression residuum described in the step 2 is introduced into heating furnace after mixing with the hydrogen supply agent fraction and is added
Hydrogen supply thermal cracking unit is entered back into after heat to be reacted.
Wherein, decompression residuum described in the step 2 is with heating temperature of the hydrogen supply agent fraction in heating furnace
400~450 DEG C.
Wherein, hydrogen supply heat cracking reaction temperature is 400~450 DEG C, 0.6~1.0Mpa of reaction pressure, the residence time 5~30
Minute.
Wherein, it is molten that solvent deasphalting process, which is with one or more of propane, butane and pentane, in the step 3
Agent is stripped, and extraction temperature is 50~190 DEG C, and extraction pressure is 3~5.5Mpa.
Wherein, the inferior heavy oil refers to heavy oil of the API less than 10.
The beneficial effects of the invention are as follows：
Using method of the present invention can maximum production API be greater than 19, the modification crude oil that has good stability, meet storage
Defeated requirement is deposited and managed, stability that is low, while guaranteeing modification oil is invested.
Detailed description of the invention
Fig. 1 is the flow diagram of the method for modifying low-quality heavy oil viscosity reduction of the present invention.
Specific embodiment
In order to which the present invention is further detailed, spy enumerates following embodiment, but the present invention is not limited in implementing
Example.
A kind of method of modifying low-quality heavy oil viscosity reduction, includes the following steps：
Step 1：Inferior heavy oil obtains straight-run oil and decompression residuum through atmospheric and vacuum distillation, wherein in straight-run oil
Include hydrogen supply agent fraction；
Step 2：The decompression residuum enters hydrogen supply thermal cracking unit after mixing with all or part of hydrogen supply agent fraction
It is reacted, generates gas, distillate and residual oil；
Step 3：The residual oil that hydrogen supply heat cracking reaction generates is pumped into solvent deasphalting unit, is taken off after exchanging heat
Coal tar and de-oiled asphalt；And
Step 4：The distillate mixing that remaining straight-run oil, deasphalted oil and hydrogen supply heat cracking reaction obtain, production
Modification oil of the API greater than 19；It is residue that straight-run oil obtained in step 1, which subtracts the hydrogen supply agent fraction used up in step 2,
Straight-run oil.
Wherein, the boiling range of straight-run oil is 500 DEG C hereinafter, wherein the boiling range of hydrogen supply agent fraction includes in the step 1
Between 280~500 DEG C, the boiling range for the hydrogen supply agent fraction that different inferior heavy oils is often evaporated under reduced pressure may be different, supply
Hydrogen agent fraction is the fraction that naphthenic base is more enriched with.
Wherein, in step 1 gained hydrogen supply agent fraction 20~100% be used for step 2 hydrogen supply heat cracking reaction.
Wherein, decompression residuum described in the step 2 is introduced into heating furnace after mixing with the hydrogen supply agent fraction and is added
Hydrogen supply thermal cracking unit is entered back into after heat to be reacted.
Wherein, decompression residuum described in the step 2 is with heating temperature of the hydrogen supply agent fraction in heating furnace
400~450 DEG C.
Wherein, hydrogen supply heat cracking reaction temperature is 400~450 DEG C, 0.6~1.0Mpa of reaction pressure, the residence time 5~30
Minute.
Wherein, it is molten that solvent deasphalting process, which is with one or more of propane, butane and pentane, in the step 3
Agent is stripped, and extraction temperature is 50~190 DEG C, and extraction pressure is 3~5.5Mpa.
Wherein, the inferior heavy oil refers to heavy oil of the API less than 10.
Embodiment 1
A kind of inferior heavy oil raw material, API 8.6, according to process shown in Fig. 1, frequent decompression separation obtains straight-run oil
And decompression residuum, straight-run oil yield are 30.33%, wherein 350-420 DEG C of fraction is hydrogen supply agent fraction, decompression residuum and complete
Portion's hydrogen supply agent fraction enters hydrogen supply thermal cracking unit, and 430 DEG C of reaction temperature, pressure 0.8Mpa, the residence time is 8 minutes, instead
Product after answering, which is fractionated, obtains distillate, and yield 39.50%, residual oil enters solvent deasphalting unit, using pentane as solvent, extraction
Taking temperature is 170 DEG C, pressure 5.0Mpa, deasphalted oil yield 74.35%, by remaining straight-run oil, deasphalted oil and
The distillate mixing that hydrogen supply heat cracking reaction obtains obtains the modification oil that API is 19.5.
Embodiment 2
A kind of inferior heavy oil raw material, API 8.4, according to process shown in Fig. 1, frequent decompression separation obtains straight-run oil
And decompression residuum, straight-run oil yield are 25.2%, wherein 300-350 DEG C of fraction is hydrogen supply agent fraction, decompression residuum and
The hydrogen supply agent fraction of 50w% enters hydrogen supply thermal cracking unit, and 425 DEG C of reaction temperature, pressure 0.8Mpa, the residence time is 15 points
Clock, the product after reaction, which is fractionated, obtains distillate, and yield 35.1%, residual oil enters solvent deasphalting unit, is molten with butane
Agent, extraction temperature are 90 DEG C, pressure 4.0Mpa, deasphalted oil yield 50.2%, by remaining straight-run oil, deasphalted oil
And the distillate mixing that hydrogen supply heat cracking reaction obtains, obtain the modification oil that API is 19.6.
Certainly, the present invention can also have other various embodiments, without deviating from the spirit and substance of the present invention, ripe
Various corresponding changes and modifications, but these corresponding changes and modifications can be made according to the present invention by knowing those skilled in the art
It all should belong to the protection scope of the claims in the present invention.
Claims (6)
1. a kind of method of modifying low-quality heavy oil viscosity reduction, which is characterized in that include the following steps：
Step 1：Inferior heavy oil obtains straight-run oil and decompression residuum through atmospheric and vacuum distillation, wherein includes in straight-run oil
Hydrogen supply agent fraction, the boiling range of straight-run oil is 500 DEG C hereinafter, wherein the boiling range of hydrogen supply agent fraction is included in 280 in step 1
Between~500 DEG C；
Step 2：The decompression residuum enters hydrogen supply after mixing with the hydrogen supply agent fraction of gained 20~100% in the step 1
Thermal cracking unit is reacted, and gas, distillate and residual oil are generated；
Step 3：The residual oil that hydrogen supply heat cracking reaction generates is pumped into solvent deasphalting unit, obtains depitching after exchanging heat
Oil and de-oiled asphalt；And
Step 4：The distillate mixing that remaining straight-run oil, deasphalted oil and hydrogen supply heat cracking reaction obtain, produces API
Modification oil greater than 19.
2. the method for modifying low-quality heavy oil viscosity reduction according to claim 1, which is characterized in that subtract described in the step 2
Pressure residual oil is introduced into after heating furnace is heated after mixing with the hydrogen supply agent fraction enters back into the progress of hydrogen supply thermal cracking unit instead
It answers.
3. the method for modifying low-quality heavy oil viscosity reduction according to claim 2, which is characterized in that subtract described in the step 2
It presses residual oil and heating temperature of the hydrogen supply agent fraction in heating furnace is 400~450 DEG C.
4. the method for modifying low-quality heavy oil viscosity reduction according to claim 1 or 2, which is characterized in that hydrogen supply heat cracking reaction
Temperature is 400~450 DEG C, 0.6~1.0Mpa of reaction pressure, the residence time 5~30 minutes.
5. the method for modifying low-quality heavy oil viscosity reduction according to claim 1, which is characterized in that solvent is de- in the step 3
It is that solvent is stripped that pitch process, which is with one or more of propane, butane and pentane, and extraction temperature is 50~190 DEG C,
Extraction pressure is 3~5.5Mpa.
6. the method for modifying low-quality heavy oil viscosity reduction according to claim 1, which is characterized in that the inferior heavy oil refers to API
Heavy oil less than 10.
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| CN106883873B true CN106883873B (en) | 2018-11-16 |
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| CN111363589A (en) * | 2018-12-25 | 2020-07-03 | 中国石油天然气股份有限公司 | Method for reducing condensation point of wax-containing crude oil |
| CN111748370B (en) * | 2019-03-28 | 2022-08-05 | 中国石油天然气股份有限公司 | Thermal modification method for heavy oil by aid of aid |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1775909A (en) * | 2005-12-07 | 2006-05-24 | 中国海洋石油总公司 | Oil sand asphalt treating method |
| CN102304386A (en) * | 2011-08-12 | 2012-01-04 | 中国石油天然气股份有限公司 | Method for improving storage stability of superheavy thick oil |
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2015
- 2015-12-15 CN CN201510931414.0A patent/CN106883873B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1775909A (en) * | 2005-12-07 | 2006-05-24 | 中国海洋石油总公司 | Oil sand asphalt treating method |
| CN102304386A (en) * | 2011-08-12 | 2012-01-04 | 中国石油天然气股份有限公司 | Method for improving storage stability of superheavy thick oil |
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Effective date of registration: 20211229 Address after: 100007 Oil Mansion, 9 North Avenue, Dongcheng District, Beijing, Dongzhimen Patentee after: PETROCHINA Co.,Ltd. Patentee after: Sinopec Research Institute of Petrochemical Co., Ltd Address before: 100007 Oil Mansion, 9 North Avenue, Dongcheng District, Beijing, Dongzhimen Patentee before: PETROCHINA Co.,Ltd. |