CN107267203A - Alkylate oil sulfur removal technology - Google Patents
Alkylate oil sulfur removal technology Download PDFInfo
- Publication number
- CN107267203A CN107267203A CN201710646461.XA CN201710646461A CN107267203A CN 107267203 A CN107267203 A CN 107267203A CN 201710646461 A CN201710646461 A CN 201710646461A CN 107267203 A CN107267203 A CN 107267203A
- Authority
- CN
- China
- Prior art keywords
- acid
- alkylate oil
- effluent
- unqualified
- washing
- 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.)
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Classifications
-
- 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
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/10—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one acid-treatment step
-
- 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
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/12—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one alkaline treatment step
-
- 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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- 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
The invention discloses a kind of alkylate oil sulfur removal technology, this method comprises the following steps：Step 1：A freshening pipeline from unqualified alkylate oil storage tank is equipped with to be connected to before alkyl plant Reactor inlet by freshening pump；Step 2：Unqualified alkylate oil is squeezed at alkyl plant reactor inlet by freshening pump, while original production pipeline is connected at alkyl plant reactor inlet；Step 3：The material of unqualified alkylate oil in step 2 and original production pipeline is together entered into reactor, pickling is carried out in the presence of eo-acid makees catalyst, settled again into acid settler, rear portion effluent process part is delivered to jointly with other materials, carrying out alkali cleaning, washing, rear portion rectifying column is arrived again and carries out oil, qi leel from qualified tank is sent outside, the sulfur content of unqualified alkylate oil is dropped to by 50ppm within 10PPM, is reached qualified products standard.The beneficial effects of the invention are as follows reduce substandard product, improve economic benefit.
Description
Technical field
The present invention relates to alkyl plant field, particularly a kind of alkylate oil sulfur removal technology.
Background technology
Alkyl plant (is mainly made up of low molecular weight olefins) in the presence of catalyst (sulfuric acid) propylene and butylene
Combine with iso-butane, form alkylates (mainly by high octane, side chain alkane composition).Alkylate oil is a kind of gasoline
Additive, with the product that cleaning is produced after anti-detonation and burning.The octane number of alkylate oil is by alkene species used
It is relevant with the reaction condition of use.Due to the presence of many destabilizing factors during device goes into operation, it is certain to produce some not
Product up to standard（The content of sulphur reaches 50ppm even more highs in alkylate oil）, can not realize and not conform on original Process ba- sis
The freshening of lattice alkylate oil, causes sales difficulty, deficiency in economic performance, it is impossible to meet market and environmental requirement.
The content of the invention
The invention aims to solve the above problems, a kind of alkylate oil sulfur removal technology is devised.
Realize above-mentioned purpose the technical scheme is that, a kind of alkylate oil sulfur removal technology, this method includes following step
Suddenly：
Step 1：It is equipped with a freshening pipeline from unqualified alkylate oil storage tank and alkyl plant is connected to by freshening pump
Before Reactor inlet；
Step 2：Unqualified alkylate oil is squeezed at alkyl plant reactor inlet by freshening pump, while by original production pipe
Line is connected at alkyl plant reactor inlet；
Step 3：The material of unqualified alkylate oil in step 2 and original production pipeline is together entered into reactor, done in eo-acid
Pickling is carried out in the presence of catalyst, then is settled into acid settler, and other materials are delivered at the effluent of rear portion jointly
Part is managed, alkali cleaning, washing is being carried out, then oil, qi leel are carried out from qualified tank is sent outside to rear portion rectifying column, makes unqualified alkylate oil
Sulfur content dropped to by 50ppm within 10PPM, reach qualified products standard.
Eo-acid uses continuous addition manner in the step 3, is added by eo-acid make-up pump to reactor, maintenance reaction acid
Concentration is not less than 90%.Adding amount is adjusted according to reaction acid concentration.
Complete acid-hydrocarbon the emulsion of progress pickling reaction passes through on one in the presence of eo-acid makees catalyst in the step 3
Riser is directly entered acid settler, and the sedimentation separation of acid and hydro carbons herein, and the acid solution separated flow to down-comer Returning reactor
Reuse.
In the step 3 and other materials deliver to the effluent of rear portion effluent process part with circulation alkali liquor in stream jointly
Go out after alkaloids wash and mixed in blender, Determining Micro Acid is removed to effluent caustic treater, followed from outflow alkaloids cleaning of evaporator bottom with alkali cleaning
Ring pumped, after being exchanged heat with alkylate oil sending mixer entrance back to is circulated.Effluent after alkali cleaning is through washing blender
After middle mixing, into effluent water washing tank.The buck of sulfur acid sodium and sulphite, enters washing from effluent washing pot bottom
Circulation pumped is washed with water in settling tank, sends mixer entrance back to and is circulated, according to the operational circumstances of caustic washing system, to note alkali pump
It is interrupted the fresh alkali lye that 4% concentration is supplemented to system, to maintain the pH value for circulating buck between 8-10.
The alkylate oil sulfur removal technology made using technical scheme, it is of the invention compared with existing technique, realize
The unqualified alkylate oil of production during going into operation（Sulfur content reaches 50ppm even more highs）Become certified products（Sulfur content 10ppm
Within）Effect, add the economic benefit of company.
Brief description of the drawings
Fig. 1 is the structural representation of alkylate oil sulfur removal technology of the present invention；
In figure, 1, new pipeline；2nd, freshening pump；3rd, alkylation reactor；4th, original production pipeline.
Embodiment
The present invention is specifically described below in conjunction with the accompanying drawings, if Fig. 1 is alkylate oil sulfur removal technology of the present invention
Structural representation, as illustrated, increasing the unqualified alkylate oil technique of pipeline freshening before alkyl plant Reactor inlet, it is walked
Suddenly it is：
Step 1：A pipeline from unqualified alkylate oil storage tank is equipped with to be connected to before alkyl plant Reactor inlet；
Step 2：Unqualified alkylate oil is squeezed at alkyl plant reactor inlet by freshening pump；
Step 3：Together enter reactor with the material on the preceding road of device, in eo-acid（Using continuous addition manner, supplemented by eo-acid
Pump is added to reactor, and maintenance reaction acid concentration is not less than 90%.Adding amount is adjusted according to reaction acid concentration.）It is catalyzed
Pickling is carried out in the presence of agent, then is settled into acid settler（React complete acid-hydrocarbon emulsion straight by a tedge
Tap into acid settler, and the sedimentation separation of acid and hydro carbons herein, the acid solution separated flow to down-comer Returning reactor to be made again
With）, and other materials deliver to rear portion effluent process part jointly, are carrying out alkali cleaning, washing（Effluent is with circulation alkali liquor in stream
Go out after alkaloids wash and mixed in blender, Determining Micro Acid is removed to effluent caustic treater, followed from outflow alkaloids cleaning of evaporator bottom with alkali cleaning
Ring pumped, after being exchanged heat with alkylate oil sending mixer entrance back to is circulated.Effluent after alkali cleaning is through washing blender
After middle mixing, into effluent water washing tank.The buck of sulfur acid sodium and sulphite, enters washing from effluent washing pot bottom
Circulation pumped is washed with water in settling tank, sends mixer entrance back to and is circulated.According to the operational circumstances of caustic washing system, to note alkali pump
It is interrupted the fresh alkali lye that 4% concentration is supplemented to system, to maintain the pH value for circulating buck between 8-10）, then to rear portion rectifying column
Oil, qi leel are carried out from sending qualified tank outside.The sulfur content of unqualified alkylate oil is set to be dropped to by 50ppm within 10PPM, it is qualified to reach
Product standard.
The characteristics of the technical program be make alkyl plant go into operation the stage generation unqualified alkylate oil（Sulfur content reaches
50ppm even more highs）Make product qualified by the processing such as the reaction of device freshening, rectifying（Sulfur content is reached within 10ppm）.
In the technical program, first it is equipped with a new pipeline 1 from unqualified alkylate oil storage tank and is connected to alkylation
Before the import of device reaction device 3；Secondly, by unqualified alkylate oil（Sulfur content 50ppm even more highs）Alkane is squeezed into by freshening pump 2
The porch of reactor 3 is put in base makeup；
Finally, the material 4 with the preceding road of device together enters reactor 3, in eo-acid（Using continuous addition manner, mended by eo-acid
Fill pump to add to reactor, maintenance reaction acid concentration is not less than 90%.Adding amount is adjusted according to reaction acid concentration.）Urge
Pickling is carried out in the presence of agent, then is settled into acid settler（Complete acid-hydrocarbon emulsion is reacted by a tedge
Acid settler, and the sedimentation separation of acid and hydro carbons herein are directly entered, the acid solution separated flow to down-comer Returning reactor again
Use）, and other materials deliver to rear portion effluent process part jointly, are carrying out alkali cleaning, washing（Effluent exists with circulation alkali liquor
After being mixed in effluent alkali cleaning blender, Determining Micro Acid is removed to effluent caustic treater, from outflow alkaloids cleaning of evaporator bottom alkali cleaning
Pumped is circulated, sending mixer entrance back to after being exchanged heat with alkylate oil is circulated.Effluent after alkali cleaning is mixed through washing
After being mixed in device, into effluent water washing tank.The buck of sulfur acid sodium and sulphite, enters water from effluent washing pot bottom
Wash settling tank and circulation pumped is washed with water, send mixer entrance back to and circulated.According to the operational circumstances of caustic washing system, to note alkali
Pump is interrupted the fresh alkali lye that 4% concentration is supplemented to system, to maintain the pH value for circulating buck between 8-10）, then to rear portion rectifying
Tower carries out oil, qi leel from sending qualified tank outside.The sulfur content of unqualified alkylate oil is dropped to by 50ppm within 10PPM, reach conjunction
Lattice product standard.
Above-mentioned technical proposal only embodies the optimal technical scheme of technical solution of the present invention, those skilled in the art
Some of which part may be made some variation embodies the present invention principle, belong to protection scope of the present invention it
It is interior.
Claims (4)
1. a kind of alkylate oil sulfur removal technology, it is characterised in that this method comprises the following steps：
Step 1：It is equipped with a freshening pipeline from unqualified alkylate oil storage tank and alkyl plant is connected to by freshening pump
Before Reactor inlet；
Step 2：Unqualified alkylate oil is squeezed at alkyl plant reactor inlet by freshening pump, while by original production pipe
Line is connected at alkyl plant reactor inlet；
Step 3：The material of unqualified alkylate oil in step 2 and original production pipeline is together entered into reactor, done in eo-acid
Pickling is carried out in the presence of catalyst, then is settled into acid settler, and other materials are delivered at the effluent of rear portion jointly
Part is managed, alkali cleaning, washing is being carried out, then oil, qi leel are carried out from qualified tank is sent outside to rear portion rectifying column, makes unqualified alkylate oil
Sulfur content dropped to by 50ppm within 10PPM, reach qualified products standard.
2. alkylate oil sulfur removal technology according to claim 1, it is characterised in that eo-acid is using continuous in the step 3
Addition manner, is added by eo-acid make-up pump to reactor, and maintenance reaction acid concentration is not less than 90%, and adding amount is according to reaction acid
Concentration is adjusted.
3. alkylate oil sulfur removal technology according to claim 1, it is characterised in that eo-acid makees catalyst in the step 3
In the presence of carry out pickling and react complete acid-hydrocarbon emulsion being directly entered acid settler by a tedge, and herein acid with
The sedimentation separation of hydro carbons, the acid solution separated flow to down-comer Returning reactor and reused.
4. alkylate oil sulfur removal technology according to claim 1, it is characterised in that be total in the step 3 with other materials
After being mixed with the effluent for delivering to rear portion effluent process part with circulation alkali liquor in effluent alkali cleaning blender, to effluent
Caustic treater removes Determining Micro Acid, and from outflow alkaloids cleaning of evaporator bottom, alkali cleaning circulates pumped, is sent back to after being exchanged heat with alkylate oil
Mixer entrance is circulated, and the effluent after alkali cleaning is after washing and being mixed in blender, into effluent water washing tank, sulfur acid
The buck of sodium and sulphite, washes pot bottom from effluent and circulation pumped is washed with water into washing precipitation tank, send mixing back to
Device entrance is circulated, according to the operational circumstances of caustic washing system, is interrupted with to note alkali pump and the fresh alkali lye of 4% concentration is supplemented to system,
To maintain the pH value of circulation buck between 8-10.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710646461.XA CN107267203B (en) | 2017-08-01 | 2017-08-01 | Alkylate oil sulfur removal technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710646461.XA CN107267203B (en) | 2017-08-01 | 2017-08-01 | Alkylate oil sulfur removal technology |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107267203A true CN107267203A (en) | 2017-10-20 |
| CN107267203B CN107267203B (en) | 2019-07-23 |
Family
ID=60074627
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710646461.XA Active CN107267203B (en) | 2017-08-01 | 2017-08-01 | Alkylate oil sulfur removal technology |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107267203B (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1583970A (en) * | 2003-08-20 | 2005-02-23 | 中国石油化工股份有限公司 | Desulfurizing method for distillate |
| CN102977911A (en) * | 2012-12-05 | 2013-03-20 | 北京化工大学 | Method for removing thiophene sulfides in fuel oil by catalytic oxidation extraction |
-
2017
- 2017-08-01 CN CN201710646461.XA patent/CN107267203B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1583970A (en) * | 2003-08-20 | 2005-02-23 | 中国石油化工股份有限公司 | Desulfurizing method for distillate |
| CN102977911A (en) * | 2012-12-05 | 2013-03-20 | 北京化工大学 | Method for removing thiophene sulfides in fuel oil by catalytic oxidation extraction |
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| Publication number | Publication date |
|---|---|
| CN107267203B (en) | 2019-07-23 |
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