CN107267203B - Alkylate oil sulfur removal technology - Google Patents
Alkylate oil sulfur removal technology Download PDFInfo
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- CN107267203B CN107267203B CN201710646461.XA CN201710646461A CN107267203B CN 107267203 B CN107267203 B CN 107267203B CN 201710646461 A CN201710646461 A CN 201710646461A CN 107267203 B CN107267203 B CN 107267203B
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- Prior art keywords
- acid
- alkylate oil
- effluent
- unqualified
- washing
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Classifications
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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
- 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 technologies, and this method comprises the following steps: step 1: before one freshening pipeline from unqualified alkylate oil storage tank of outfit is connected to alkyl plant Reactor inlet by freshening pump；Step 2: unqualified alkylate oil being squeezed at alkyl plant reactor inlet by freshening pump, while original production pipeline being connected at alkyl plant reactor inlet；Step 3: the unqualified alkylate oil in step 2 is entered into reactor together with the material of original production pipeline, pickling is carried out under the action of eo-acid makees catalyst, it is settled again into acid settler, it is sent jointly with other materials to rear portion effluent and handles part, carrying out alkali cleaning, washing, arrive again rear portion rectifying column carry out oil, gas separation send qualified tank outside, drop to the sulfur content of unqualified alkylate oil within 10PPM by 50ppm, reach qualified products standard.The invention has the advantages that reducing substandard product, economic benefit is improved.
Description
Technical field
The present invention relates to alkyl plant field, especially a kind of alkylate oil sulfur removal technology.
Background technique
Alkyl plant (is mainly made of low molecular weight olefins) under the action 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 has anti-detonation and generates clean product after burning.The octane number of alkylate oil is by alkene type used
It is related with the reaction condition of use.The presence of many unstable factors during being gone into operation due to device, be certain to produce it is some not
Product (it is even higher to reach 50ppm for the content of sulphur in alkylate oil) up to standard, cannot achieve on original Process ba- sis and does not conform to
The freshening of lattice alkylate oil, causes sales difficulty, and deficiency in economic performance is unable to satisfy market and environmental requirement.
Summary of the invention
The purpose of the present invention is to solve the above problems, devise a kind of alkylate oil sulfur removal technology.
Realize above-mentioned purpose the technical scheme is that, a kind of alkylate oil sulfur removal technology, this method includes following step
It is rapid:
Step 1: with a freshening pipeline from unqualified alkylate oil storage tank by freshening pump and be connected to alkylation
Before device reaction device import；
Step 2: unqualified alkylate oil being squeezed at alkyl plant reactor inlet by freshening pump, while will be primary
Pipeline is produced to be connected at alkyl plant reactor inlet；
Step 3: the unqualified alkylate oil in step 2 being entered into reactor together with the material of original production pipeline, new
Acid carries out pickling under the action of making catalyst, then is settled into acid settler and other materials send jointly to rear portion and flow out
Object handles part, is carrying out alkali cleaning, washing, then to rear portion rectifying column carries out oil, qualified tank is sent in gas separation outside, make unqualified alkyl
The sulfur content of carburetion is dropped within 10PPM by 50ppm, reaches qualified products standard.
Eo-acid uses continuous addition manner in the step 3, is added by eo-acid make-up pump to reactor, maintains reaction acid
Concentration is not less than 90%.Adding amount is adjusted according to reaction acid concentration.
Eo-acid, which is done, in the step 3 carries out acid-hydrocarbon emulsion of pickling fully reacting under the action of catalyst by one
Riser is directly entered acid settler, and the sedimentation separation of acid and hydro carbons, the acid solution separated flow to down-comer Returning reactor herein
It reuses.
It is sent jointly to the effluent of rear portion effluent processing part and circulation alkali liquor and is being flowed with other materials in the step 3
Alkaloids are washed in mixer after mixing out, until effluent caustic treater removes Determining Micro Acid, are followed from alkaloids cleaning of evaporator bottom is flowed out with alkali cleaning
Ring pumping goes out, and sends mixer entrance back to after exchanging heat with alkylate oil and is recycled.Effluent after alkali cleaning is through washing mixer
After middle mixing, into effluent water washing tank.The buck of sulfur acid sodium and sulphite enters washing from effluent washing pot bottom
Circulating pump extraction is washed with water in settling tank, sends mixer entrance back to and is recycled, according to the operational circumstances of caustic washing system, to infuse alkali pump
It is interrupted the fresh lye that 4% concentration is supplemented to system, to maintain the pH value of circulation buck between 8-10.
The alkylate oil sulfur removal technology made using technical solution of the present invention, the present invention are realized compared with existing technique
The unqualified alkylate oil (it is even higher that sulfur content reaches 50ppm) produced during going into operation becomes qualified product (sulfur content 10ppm
Within) effect, increase the economic benefit of company.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of alkylate oil sulfur removal technology of the present invention；
In figure, 1, new pipeline；2, freshening pumps；3, alkylation reactor；4, original production pipeline.
Specific embodiment
The present invention is specifically described with reference to the accompanying drawing, if Fig. 1 is alkylate oil sulfur removal technology of the present invention
Structural schematic diagram, as shown, increase the unqualified alkylate oil technique of pipeline freshening before alkyl plant Reactor inlet, step
Suddenly are as follows:
Step 1: with a pipeline from unqualified alkylate oil storage tank and be connected to alkyl plant Reactor inlet
Before；
Step 2: unqualified alkylate oil is squeezed at alkyl plant reactor inlet by freshening pump；
Step 3: entering reactor together with the material on the preceding road of device, (use continuous addition manner in eo-acid, pass through eo-acid
Make-up pump is added to reactor, and reaction acid concentration is maintained to be not less than 90%.Adding amount is adjusted according to reaction acid concentration.) do
Pickling is carried out under the action of catalyst, then settled into acid settler (acid of fully reacting-hydrocarbon emulsion by one rise
Pipe is directly entered acid settler, and the sedimentation separation of acid and hydro carbons, the acid solution separated flow to down-comer Returning reactor weight herein
It is new to use) and other materials sent jointly to rear portion effluent and handle part, carrying out alkali cleaning, washing (effluent and circulation alkali liquor
After being mixed in effluent alkali cleaning mixer, until effluent caustic treater removes Determining Micro Acid, from outflow alkaloids cleaning of evaporator bottom alkali
Circulating pump extraction is washed, mixer entrance is sent back to after exchanging heat with alkylate oil and is recycled.Effluent after alkali cleaning is mixed through washing
After being mixed in clutch, into effluent water washing tank.The buck of sulfur acid sodium and sulphite enters from effluent washing pot bottom
Circulating pump extraction is washed with water in washing precipitation tank, sends mixer entrance back to and is recycled.According to the operational circumstances of caustic washing system, with note
Alkali pump is interrupted the fresh lye that 4% concentration is supplemented to system, to maintain the pH value of circulation buck between 8-10), then it is smart to rear portion
Evaporate tower progress oil, qualified tank is sent in gas separation outside.It drops to the sulfur content of unqualified alkylate oil within 10PPM by 50ppm, reaches
Qualified products standard.
The characteristics of the technical program be make alkyl plant go into operation the stage generation unqualified alkylate oil (sulfur content reaches
50ppm is even higher) keep product qualified (sulfur content reaches within 10ppm) by processing such as the reaction of device freshening, rectifying.
In the technical scheme, it is first equipped with a new pipeline 1 from unqualified alkylate oil storage tank and is connected to alkylation
Before 3 import of device reaction device；Secondly, unqualified alkylate oil (sulfur content 50ppm is even higher) is squeezed into alkane by freshening pump 2
3 inlet of reactor is set in base makeup；
Finally, the material 4 with the preceding road of device enters reactor 3 together, (continuous addition manner is used, by new in eo-acid
Sour make-up pump is added to reactor, and reaction acid concentration is maintained to be not less than 90%.Adding amount is adjusted according to reaction acid concentration.)
It does and carries out pickling under the action of catalyst, then settled that (acid of fully reacting-hydrocarbon emulsion is by one into acid settler
Riser is directly entered acid settler, and the sedimentation separation of acid and hydro carbons, the acid solution separated flow to down-comer Returning reactor herein
Reuse) and other materials send jointly to rear portion effluent handle part, carry out alkali cleaning, washing (effluent and circulation alkali
After liquid mixes in effluent alkali cleaning mixer, until effluent caustic treater removes Determining Micro Acid, used from alkaloids cleaning of evaporator bottom is flowed out
The extraction of alkali cleaning circulating pump, sends mixer entrance back to after exchanging heat with alkylate oil and is recycled.Effluent after alkali cleaning is through washing
After being mixed in mixer, into effluent water washing tank.The buck of sulfur acid sodium and sulphite, from effluent wash pot bottom into
Enter washing precipitation tank and circulating pump extraction is washed with water, sends mixer entrance back to and recycled.According to the operational circumstances of caustic washing system, with
Note alkali pump is interrupted the fresh lye that 4% concentration is supplemented to system, to maintain the pH value of circulation buck between 8-10), then arrive rear portion
Rectifying column carries out oil, qualified tank is sent in gas separation outside.It drops to the sulfur content of unqualified alkylate oil within 10PPM by 50ppm, reaches
To qualified products standard.
Above-mentioned technical proposal only embodies the optimal technical scheme of technical solution of the present invention, those skilled in the art
The principle of the present invention is embodied to some variations that some of them part may be made, belongs to the scope of protection of the present invention it
It is interior.
Claims (1)
1. a kind of alkylate oil sulfur removal technology, which is characterized in that this method comprises the following steps:
Step 1: with a freshening pipeline from unqualified alkylate oil storage tank by freshening pump and be connected to alkyl plant
Before Reactor inlet；
Step 2: unqualified alkylate oil being 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 unqualified alkylate oil in step 2 being entered into reactor together with the material of original production pipeline, is done in eo-acid
Pickling is carried out under the action of catalyst, then is settled into acid settler and other materials are sent jointly to the effluent of rear portion
Part is managed, is carrying out alkali cleaning, washing, then to rear portion rectifying column carries out oil, qualified tank is sent in gas separation outside, make unqualified alkylate oil
Sulfur content dropped within 10PPM by 50ppm, reach qualified products standard,
Eo-acid uses continuous addition manner in the step 3, is added by eo-acid make-up pump to reactor, maintains reaction acid concentration
Not less than 90%.Adding amount is adjusted according to reaction acid concentration,
Eo-acid carries out acid-hydrocarbon emulsion of pickling fully reacting by a tedge under the action of making catalyst in the step 3
It is directly entered acid settler, and the sedimentation separation of acid and hydro carbons, the acid solution separated flow to down-comer Returning reactor again herein
It uses,
It is sent jointly to the effluent of rear portion effluent processing part and circulation alkali liquor with other materials in effluent in the step 3
After being mixed in alkali cleaning mixer, until effluent caustic treater removes Determining Micro Acid, from outflow alkaloids cleaning of evaporator bottom alkali cleaning circulating pump
Extraction, sends mixer entrance back to after exchanging heat with alkylate oil and is recycled, and the effluent after alkali cleaning in washing mixer through mixing
After conjunction, into effluent water washing tank, the buck of sulfur acid sodium and sulphite enters washing sedimentation from effluent washing pot bottom
Circulating pump extraction is washed with water in tank, sends mixer entrance back to and is recycled, according to the operational circumstances of caustic washing system, to infuse alkali pump interruption
The fresh 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 CN107267203A (en) | 2017-10-20 |
| CN107267203B true CN107267203B (en) | 2019-07-23 |
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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 |
|---|---|
| CN107267203A (en) | 2017-10-20 |
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