CN106833735A - Petroleum fluids extraction desulfurization group technology - Google Patents
Petroleum fluids extraction desulfurization group technology Download PDFInfo
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- CN106833735A CN106833735A CN201710041315.4A CN201710041315A CN106833735A CN 106833735 A CN106833735 A CN 106833735A CN 201710041315 A CN201710041315 A CN 201710041315A CN 106833735 A CN106833735 A CN 106833735A
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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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- 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
The present invention relates to a kind of petroleum fluids desulfurization group technology, for 30 260 DEG C of cut petroleum fluids desulfurization, the method includes raw material Cutting Tap, extraction distillation tower, liquid liquid extraction tower and recovery tower；It is characterized in that：After the petroleum fluids pass into upstream selectivity pre-hydrotreating, the raw material Cutting Tap is sent into, fractionate out light distillate and heavy distillate, light distillate enters the extraction distillation tower, and the extraction of extractive distillation tower top is rich in the light of alkene and raffinates oil；Extractive distillation bottom of towe produces the light rich solvent containing sulphur, light aromatic hydrocarbons and solvent, and light rich solvent enters the recovery tower.Heavy distillate enters the liquid liquid extraction tower, liquid liquid extracting overhead extraction heavy is raffinated oil, bottom of towe heavy rich solvent of the extraction rich in heavy aromatics, sulphur and solvent, weight rich solvent and the light rich solvent enter the recovery tower together, reclaim sulfur component and the blending ingredients of aromatic hydrocarbons that overhead extraction contains sulphur and aromatic hydrocarbons.
Description
Technical field
The present invention relates to a kind of petroleum fluids extraction desulfurization group technology.
Background technology
Increasingly strict with environmental requirement, the sulfur content requirement of various oil products is increasingly stricter, from petroleum fluids
It is particularly important that middle removing sulphur just shows.
This technique uses component oil refining new concept, while extraction desulfurization, petroleum fluids component is reconfigured, and is applicable
In the component for increasing octane number, separate and call in gasoline；Component suitable for increasing diesel cetane-number, separates
Diesel oil is called in, individually hydrogenation is removed in sulfur-bearing part.
The current main process that sulphur is removed from petroleum fluids is hydrogenation, and current hydrogenation technique is both for specific product
Product are focused on, and petroleum fluids each component are not accounted for the tolerance that is hydrogenated with, while the fractionation of product is also both for evaporating
Cheng Butong, is cut into each components such as gasoline, diesel oil, and its alkane, aromatic hydrocarbons, alkene each component are considered not the contribution of different oil products
Greatly.This technique is combined by extractive distillation and liquid liquid extraction process, and distillation is stripped respectively after being cut to target petroleum fluids
With liquid liquid extracting treatment, sulfur component and aromatic hydrocarbons mixture after extractive distillation treatment enter back end hydrogenation, as Gaoxin after hydrogenation
Alkane value component reconciles into gasoline；Extractive distillation not sulfur component out is directly entered downstream, carries out product mediation, and the cut contains
Sulphur is not more than 20ppm, can directly reconcile to meeting national standard；And the cut contains a large amount of alkene, these alkene avoid adding
Hydrogen saturation, reduces loss of octane number.The alkane containing a small amount of sulphur after liquid liquid extracting treatment is used as diesel oil blending component Qu Quan factories
Diesel systems, the component condensation point is low, and Cetane number is high, and sulfur content is low；Aromatic hydrocarbons and extractive distillation part after liquid liquid extracting treatment
Recovery tower is shared, the aromatic hydrocarbons and sulphur after the logistics and extractive distillation treatment are joined after downstream hydrogenation as antiknock component together
Reconciled with gasoline.Petroleum fluids first pass through pre-hydrotreating before extracting group technology into extractive distillation and liquid liquid, after treatment
Prefractionation is carried out, light oil is cut out in prefractionation part.
The content of the invention
An object of the present invention is to provide efficient, environmentally friendly sulfur method.
To achieve the above object, the present invention takes following technical scheme：
The present invention relates to a kind of petroleum fluids desulfurization group technology, the technique is mainly for 30-260 DEG C of cut petroleum fluids
Desulfurization, the method includes raw material Cutting Tap, extraction distillation tower, liquid liquid extraction tower and recovery tower；It is characterized in that：The petroleum streams
After body passes into upstream selectivity pre-hydrotreating, the raw material Cutting Tap is sent into, light fraction is fractionated out in raw material Cutting Tap
Oil and heavy distillate, light distillate enter the extraction distillation tower, and the extraction of extractive distillation tower top is rich in the light of alkene and raffinating oil, gently
Raffinate oil and directly go out device, participate in gasoline and reconcile；Extractive distillation bottom of towe produces the light rich solvent containing sulphur, light aromatic hydrocarbons and solvent,
Light rich solvent enters the recovery tower.Heavy distillate enters the liquid liquid extraction tower, liquid liquid extraction tower overhead extraction heavy raffinate
Oil, as low-coagulation diesel oil blend component, bottom of towe heavy rich solvent of the extraction rich in heavy aromatics, sulphur and solvent, weight rich solvent and described
Light rich solvent enters the recovery tower together, and the recovery overhead extraction contains the mixing of the sulfur component and aromatic hydrocarbons of sulphur and aromatic hydrocarbons
Component, by after the treatment of downstream hydrogenation device, used as high-knock rating gasoline blend component, the recovery tower bottom produces lean solvent,
Lean solvent delivers to the extractive distillation tower top respectively and liquid liquid extracting tower top is recycled.
Reconfigured by race's composition it is another object of the present invention to each component to petroleum fluids, according to product requirement
Different choice difference place to go, comprehensive effective utilization is carried out to race's composition.
Above-mentioned purpose of the invention reaches by the following technical programs：
Petroleum fluids extraction desulfurization group technology, its step is as follows：30-260 DEG C of petroleum fluids are delivered into raw material Cutting Tap
Light distillate and heavy distillate are separated, light distillate boiling range is adjusted according to product requirement between 30-230 DEG C, and heavy distillate evaporates
Journey is adjusted according to product requirement between 70-260 DEG C；Light distillate enters extraction distillation tower, and the extraction of extractive distillation tower top is rich in
Raffinating oil for alkene, raffinates oil and directly goes out device, participates in gasoline and reconciles；The extraction of extractive distillation bottom of towe contains sulphur, light aromatic hydrocarbons and molten
The light rich solvent of agent, light rich solvent enters recovery tower.Heavy distillate enters liquid liquid extraction tower, and liquid liquid extraction tower overhead extraction is free of
Aromatic hydrocarbons and the heavy containing Determination of Trace Sulfur are raffinated oil, and used as low-coagulation diesel oil blend component, bottom of towe extraction is rich in heavy aromatics, sulphur and solvent
Heavy rich solvent, weight rich solvent and the light rich solvent together enter the recovery tower, reclaim overhead extraction contain sulphur and aromatic hydrocarbons
High-knock rating gasoline blend component, recovery tower bottom extraction lean solvent, lean solvent delivers to extractive distillation tower top respectively and liquid liquid is taken out
Stripper top recycles.
A kind of optimal technical scheme, it is characterised in that：Extraction distillation tower and liquid liquid extraction tower are applied in combination, and share and reclaim
Tower.A kind of optimal technical scheme, it is characterised in that：Extraction distillation tower operating pressure is 0.05-0.35MPa, liquid liquid extraction tower behaviour
Make pressure for 0.30-0.90MPa.
A kind of optimal technical scheme, it is characterised in that：30-260 DEG C of petroleum fluids are delivered to raw material Cutting Tap and separated and is gently evaporated
Oil and heavy distillate, light distillate boiling range is divided to be adjusted between 30-230 DEG C according to product requirement, heavy distillate boiling range is according to product
Product requirement is adjusted between 70-260 DEG C；Light distillate enters extraction distillation tower, and heavy distillate enters liquid liquid extraction tower.It is a kind of excellent
Selecting technology scheme, it is characterised in that：Extraction distillation tower solvent quality ratio is 1.2-6.5, and liquid liquid extraction tower solvent quality ratio is
1.2-6.5。
A kind of optimal technical scheme, it is characterised in that：The group technology is not limited for raw material, selected from 30-260 DEG C
Cut petroleum fluids.
A kind of optimal technical scheme, it is characterised in that：Extraction distillation tower is that non-liquid liquid contacts extraction tower, and liquid liquid extraction tower is
Liquid liquid contacts extraction tower.
A kind of optimal technical scheme, it is characterised in that：By the sulfur component and the blending ingredients of aromatic hydrocarbons that reclaim overhead extraction,
Processed by downstream hydrogenation device.
A kind of optimal technical scheme, it is characterised in that：Extraction distillation tower and liquid liquid extraction tower are real according to production requirement substep
Apply, first step extraction distillation tower and recovery tower are individually supporting, desulfurization process are carried out to light distillate；Second step is according to production requirement
Increase liquid liquid extraction tower.
A kind of optimal technical scheme, it is characterised in that：Extraction distillation tower and liquid liquid extraction tower are real according to production requirement substep
Apply, first step liquid liquid extraction tower and recovery tower are individually supporting, and desulfurization process are carried out to heavy distillate；Second step is according to production requirement
Increase extraction distillation tower.
Extraction distillation tower, liquid liquid extraction tower, recovery tower and Cutting Tap used of the invention are conventional extraction distillation tower, liquid
Liquid extraction tower, recovery tower.
Beneficial effect：
The present invention is for the group technology advantage of petroleum fluids extraction desulfurization：Conventional extraction desulfurization is compared, of the invention
Group technology uses different extracting modes to weight component, for light component, using extractive distillation mode desulfurization, by light component
After sulphur removing, sulfur component does not participate in oil product mediation directly；To heavy constituent, the desulfurization by the way of the extracting of liquid liquid, to heavy constituent
While desulfurization, each component to heavy distillate is reconfigured, and aromatic-free and raffinating oil again for sulphur coagulate hexadecane high as low
Value component, goes diesel systems；Recovery tower is shared after light distillate and heavy distillate extracting.Each component of the present invention to petroleum fluids
Reconfigured, according to product requirement different choice difference place to go, comprehensive effective utilization is carried out to each component.
Below by the drawings and specific embodiments, the present invention will be further described, but is not meant to protect the present invention
Protect the limitation of scope.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of one of the embodiment of the present invention.
Below by specific embodiment, the present invention will be further described, but is not meant to the scope of the present invention
Limitation.
Specific embodiment
Embodiment 1
As shown in figure 1, be the schematic flow sheet of case study on implementation of the present invention, some auxiliary equipments in figure such as tank, pump, heat exchange
Device, condenser etc. are not marked, but this is known to those of ordinary skill in the art.
As shown in figure 1,37-220 DEG C of petroleum distillate, sulfur content is 1000ppm, and aromatics quality content is 27.8% (raw material
Property is shown in Table 1-1) raw material Cutting Tap 1, the overhead extraction light distillate 63 of raw material Cutting Tap 1 are entered with the flow of 100 ton hours
Ton hour, boiling range is that HK-170 DEG C (light distillate property is shown in Table 1-2) and solvent are added and taken out together with the flow of 315 ton hours
Carry destilling tower 2 to be stripped, the tower top temperature of extraction distillation tower 2 is 102 DEG C, and pressure is 0.15MPa, and solvent ratio is 5, and gained is taken out
The sulfur content of excess oil is 10ppm, and solvent is 1ppm.The first rich solvent obtained from extraction distillation tower 2 with 326.8 tons/it is small
When flow by the bottom of towe of extraction distillation tower 1 enter recovery tower 3.The bottom of towe of raw material Cutting Tap 1 produces the ton hour of heavy distillate 37,
Boiling range is that 175-230 DEG C (heavy distillate property is shown in Table 1-3) and solvent add liquid liquid to extract together with the flow of 148 ton hours
Tower 4 is stripped, and the tower top temperature of liquid liquid extraction tower 4 is 90 DEG C, and pressure is 0.7MPa, and solvent ratio is 4, the sulphur that gained is raffinated oil
Content is 30ppm, and solvent is 2ppm.The first rich solvent obtained from liquid liquid extraction tower 1 is with the flow of 165.7 ton hours
Recovery tower 3 is entered by the bottom of towe of liquid liquid extraction tower 1.The bottom of towe of recovery tower 3 extraction solvent with the flow of 463 ton hours, wherein with
The flow of 315 ton hours enters the top of extraction distillation tower 2；The top of liquid liquid extraction tower 4 is entered with the flow of 148 ton hours.Institute
The composition and property for obtaining raffinate oil product is shown in Table 1-2, and the composition and property of gained aromatic hydrocarbon product is shown in Table 1-3.；
The raw material of 1 embodiment of table 1 and product property table
Table 1-1 feedstock properties
| Project | Numerical value |
| 722 | |
| Sulfur content, μ g/g | 1000 |
| Saturated alkane, quality % | 41.7 |
| Alkene, quality % | 30.6 |
| Aromatic hydrocarbons, quality % | 27.7 |
| Boiling range/DEG C, ASTMD86 | |
| IBP | 37 |
| 10% | 55 |
| 30% | 66 |
| 50% | 105 |
| 70% | 130 |
| 90% | 175 |
| FBP | 220 |
Table 1-2 light distillate property lists
Table 1-3 heavy distillate property lists
| Project | Numerical value |
| 803 | |
| Sulfur content, μ g/g | 1557 |
| Saturated alkane, v% | 36.9 |
| Alkene, volume v% | 45.2 |
| Aromatic hydrocarbons, volume v% | 17.8 |
| Boiling range/DEG C, ASTMD86 | |
| IBP | 175 |
| 10% | 181 |
| 30% | 195 |
| 50% | 206 |
| 70% | 218 |
| 90% | 223 |
| FBP | 230 |
Table 1-4 gently raffinates oil property list
The light tapped oil property list project numerical value of table 1-5
| Project | Numerical value |
| 20 DEG C of density@, kg/m3 | 723 |
| Sulfur content, μ g/g | 3325 |
| Saturated alkane, v% | 15.0 |
| Alkene, volume v% | 5.3 |
| Aromatic hydrocarbons, volume v% | 79.7 |
| Boiling range/DEG C, ASTMD86 | |
| IBP | 39 |
| 10% | 61 |
| 30% | 83 |
| 50% | 105 |
| 70% | 136 |
| 90% | 161 |
| FBP | 174 |
Table 1-6 raffinates oil property list again
| Project | Numerical value |
| 20 DEG C of density@, kg/m3 | 798 |
| Sulfur content, μ g/g | 30 |
| Saturated alkane, v% | 88.5 |
| Alkene, volume v% | 7.8 |
| Aromatic hydrocarbons, volume v% | 3.7 |
| Boiling range/DEG C, ASTMD86 | 172 |
| IBP | 172 |
| 10% | 178 |
| 30% | 191 |
| 50% | 201 |
| 70% | 213 |
| 90% | 217 |
| FBP | 224 |
Table 1-7 reppears excess oil property list
| Project | Numerical value |
| 20 DEG C of density@, kg/m3 | 815 |
| Sulfur content, μ g/g | 57583.5 |
| Saturated alkane, v% | 7.5 |
| Alkene, volume v% | 2.9 |
| Aromatic hydrocarbons, volume v% | 89.6 |
| Boiling range/DEG C, ASTMD86 | |
| IBP | 176 |
| 10% | 178 |
| 30% | 198 |
| 50% | 211 |
| 70% | 214 |
| 90% | 229 |
| FBP | 236 |
Claims (10)
1. a kind of petroleum fluids desulfurization group technology, the technique is mainly for 30-260 DEG C of cut petroleum fluids desulfurization, the method
Including raw material Cutting Tap, extraction distillation tower, liquid liquid extraction tower and recovery tower；It is characterized in that：The petroleum fluids are passed into
After the selectivity pre-hydrotreating of upstream, the raw material Cutting Tap is sent into, light distillate and heavy distillat are fractionated out in raw material Cutting Tap
Oil, light distillate enters the extraction distillation tower, and extractive distillation tower top extraction gently raffinating oil rich in alkene is gently raffinated oil directly
Go out device, participate in gasoline and reconcile；Extractive distillation bottom of towe produces the light rich solvent containing sulphur, light aromatic hydrocarbons and solvent, and light rich solvent enters
Enter the recovery tower.Heavy distillate enters the liquid liquid extraction tower, and liquid liquid extraction tower overhead extraction heavy is raffinated oil, used as low solidifying
Diesel oil blending component, bottom of towe heavy rich solvent of the extraction rich in heavy aromatics, sulphur and solvent, weight rich solvent and the light rich solvent are together
Into the recovery tower, the recovery overhead extraction contains the sulfur component and the blending ingredients of aromatic hydrocarbons of sulphur and aromatic hydrocarbons, under
After trip hydrogenation device for treatment, used as high-knock rating gasoline blend component, the recovery tower bottom produces lean solvent, and lean solvent send respectively
Recycled to the extractive distillation tower top and liquid liquid extracting tower top.
2. each component of pair petroleum fluids is reconfigured, and according to product requirement different choice difference place to go, each component is entered
The comprehensive effective utilization of row.
3. petroleum fluids desulfurization group technology according to claim 1, it is characterised in that：Extraction distillation tower and liquid liquid are extracted
Tower is applied in combination, and shares recovery tower.
4. petroleum fluids desulfurization group technology according to claim 1, it is characterised in that：Extraction distillation tower operating pressure is
0.05-0.35MPa, liquid liquid extraction tower operating pressure is 0.30-0.90MPa.
5. petroleum fluids desulfurization group technology according to claim 1, it is characterised in that：A kind of optimal technical scheme, its
It is characterised by：30-260 DEG C of petroleum fluids are delivered into raw material Cutting Tap and separates light distillate and heavy distillate, light distillate boiling range
According to product requirement between 30-230 DEG C, heavy distillate boiling range is according to product requirement between 70-260 DEG C；Light distillate is entered
Enter extraction distillation tower, heavy distillate enters liquid liquid extraction tower.
6. petroleum fluids desulfurization group technology according to claim 1, it is characterised in that：The group technology is for raw material
Without limitation, selected from 30-260 DEG C of cut petroleum fluids.
7. petroleum fluids desulfurization group technology according to claim 1, it is characterised in that：Extraction distillation tower connects for non-liquid liquid
Extraction tower is touched, liquid liquid extraction tower is that liquid liquid contacts extraction tower.Extraction distillation tower solvent quality ratio is 1.2-6.5, liquid liquid extraction tower
Solvent quality ratio is 1.2-6.5.
8. petroleum fluids desulfurization group technology according to claim 1, it is characterised in that：The sulfur-bearing of overhead extraction will be reclaimed
The blending ingredients of component and aromatic hydrocarbons, are processed by downstream hydrogenation device.
9. petroleum fluids desulfurization group technology according to claim 1, it is characterised in that：Extraction distillation tower and liquid liquid are extracted
Tower is implemented step by step according to production requirement, and first step extraction distillation tower and recovery tower are individually supporting, and light distillate is carried out at desulfurization
Reason；Second step increases liquid liquid extraction tower according to production requirement.
10. petroleum fluids desulfurization group technology according to claim 1, it is characterised in that：Extraction distillation tower and liquid liquid are taken out
Stripper is implemented step by step according to production requirement, and first step liquid liquid extraction tower and recovery tower are individually supporting, and desulfurization is carried out to heavy distillate
Treatment；Second step increases extraction distillation tower according to production requirement.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110628459A (en) * | 2019-10-15 | 2019-12-31 | 北京宝晨能源工程技术有限公司 | Aromatic hydrocarbon extraction combined device and process |
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Application publication date: 20170613 |