CN110423633A - A kind of oil product defluorination method - Google Patents
A kind of oil product defluorination method Download PDFInfo
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- CN110423633A CN110423633A CN201910752645.3A CN201910752645A CN110423633A CN 110423633 A CN110423633 A CN 110423633A CN 201910752645 A CN201910752645 A CN 201910752645A CN 110423633 A CN110423633 A CN 110423633A
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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
- C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption 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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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to defluorination technology fields, and in particular to arrive a kind of oil product defluorination method.The fluorine in alkylated tar is removed in the method chemically reacted and physical absorption combines, is allowed to meet the needs of recycling.Treated by means of the present invention oil product, fluorine content hereinafter, be able to carry out recycling, or is sold in 1ppm as product, not only environmentally protective, moreover it is possible to economize on resources, reduce cost.
Description
Technical field
The invention belongs to defluorination technology fields, and in particular to arrive a kind of oil product defluorination method.
Background technique
Linear alkylbenzene (LAB) (LAB) typically refers to the alkylbenzene that straight chained alkyl carbon number is 10~14, is fine chemical product
Important intermediate is mainly used for the production of linear alkyl benzene sulfonic acid (LAS) and its salt, and it is generation that LAS, which is important detergent monomer,
The maximum synthetic surfactant of yield in boundary, has good biological degradability, dissolubility and dirt-removing power and price is low
It is honest and clean, it is therefore widely used in various types of articless for washing.
Industrially, LAB is mainly made through being alkylated using benzene and alpha-olefin as raw material under the action of catalyst.UOP technique
In, first by catalytic dehydrogenation of n-alkanes monoolefine, then under hydrofluoric acid catalysis, benzene and linear alkene are alkylated instead
It answers, generates linear alkylbenzene (LAB).Catalyst of the hydrofluoric acid as Alkylbenzene Unit is present in the form of hydrogen fluoride and two kinds of hydrofluoric acid
In Alkylbenzene Unit.Some side reactions such as isomerization, polymerization, chain rupture, disproportionation etc. also occur while alkylated reaction, thus
Also generate some by-products.These by-products are finally separated as high-boiling components from alkylbenzene Fractionator Bottom, due to wherein containing
There are a large amount of fluorine, special processing processed in units can only be given as dangerous liquid wastes always, not only the wasting of resources is difficult to realize comprehensive
It closes using but also environment is caused greatly to pollute.
In order to reduce by-product --- fluorine content in alkylated tar, traditional method be exactly use potassium hydroxide neutralize,
Washing, but still fluorine content in tar cannot be effectively reduced, achieve the purpose that resource reutilization.This not only waste of resource, cause to give birth to
It produces cost to increase, needs to discharge pollutants into environment.
Summary of the invention
To solve problems of the prior art, the present invention provides a kind of simple process, operating flexibilities greatly, defluorinate effect
Rate height, environmentally protective oil product defluorination method remove alkylated tar by chemically reacting the method combined with physical absorption
In fluorine, the needs of being allowed to meet recycling.
In order to achieve the above object, the technical solution adopted by the present invention are as follows: a kind of oil product defluorination method, comprising the following steps:
(1) alkali cleaning
Fluorine-containing oil product is reacted at a certain temperature with alkaline aqueous solution, the reaction solution sedimentation separation that will be obtained, upper layer obtains
To defluorinate oil, lower layer obtains the lye containing fluoride salt.
(2) it washes
Defluorinate oil obtained in step (1) is mixed with water, obtained liquid is separated, upper layer obtains dealkalize liquid
Oil product, lower layer obtain the water containing micro alkali.
(3) it is dehydrated
Upper layer oil obtained in step (2) is heated, or vacuumizes and is heated to normal pressure relevant temperature, 10~60min of time,
Isolate water content in oil；Remaining dewatered oil product.
(4) it adsorbs
It mixes, is then separated by solid-liquid separation, liquid contains for fluorine with adsorbent after oil product heating after being dehydrated obtained in step (3)
Qualified oil product is measured, solid is adsorbent.
In the step (1), the fluorine-containing oil product is any fluorine-containing oil product, particularly relates to alkylated tar.
In the step (1), fluorine-containing oil product is reacted with lye at 20~90 DEG C, this is because the low liquid viscosity of temperature is big,
Poor fluidity, power consumption is big, and it is best to work as 60~90 DEG C of effects of temperature for discovery after many experiments.
In the step (1), lye is sodium hydrate aqueous solution, potassium hydroxide aqueous solution, calcium hydroxide aqueous solution, ethyl alcohol
One or more of amine aqueous solution, the KOH aqueous solution of preferred concentration 10%~30%.
In the step (1), 10~60min of reaction time.
In the step (1), lye can be recycled.
In the step (1), alkali cleaning reaction can carry out in batch device, can also carry out in continuous device.
In the step (2), defluorinate oil is mixed with water, and mixing temperature is 20~90 DEG C, preferably 60~90 DEG C；This is
Because the low liquid viscosity of temperature is big, poor fluidity.
In the step (2), 10~60min of incorporation time.
In the step (2), water can be recycled.
In the step (3), washing oil product exchanges heat to 100~200 DEG C；Water can be in gaseous form from oil at this temperature
In separate, be higher than 200 DEG C, energy consumption increase.
In the step (4), dehydration oil product is heated to 20~300 DEG C.
In the step (4), 1~200min of adsorption time.
In the step (4), adsorbent is one or more of aluminum sulfate, resin, activated alumina.
The granularity of the activated alumina can be selected according to actual needs.
If do not required the alkali metal content in oil product, step (2) be can be omitted；If step (1) layering when
Between it is long, step (3) can be omitted.
The beneficial effects of the present invention are:
(1) oil product defluorination method of the invention has started the new road of industrial oil defluorination technology, through method of the invention
The oil product of defluorinate meets the related request of fluorine content.
(2) simple process, it is easy to operate, it realizes burnt with the method removing alkylation chemically reacted and physical absorption combines
Fluorine in oil is allowed to meet the needs of recycling.
(3) defluorinate is high-efficient, and fluorine content can be down to 1mg/L hereinafter, alkylated tar can be into oil product after defluorinate
Row recycles, or sells as product；And treated that alkylated tar can drop to 0.2mg/L or less for method of the invention.
(4) operating flexibility is big, applied widely, lye appropriate can be selected to use according to the fluorine content of fluorine-containing oil product
The operating conditions such as amount, reaction temperature, reaction time, the defluorinate especially suitable for high fluorocarbon oil product.
(5) environmentally protective, good in economic efficiency, lye and water can be recycled, although must have part spent lye and give up
There is still a need for processing for water, but compare with fluorine-containing oil, and waste liquid amount significantly reduces, and reduce three waste discharge.
Specific embodiment
A kind of oil product defluorination method, includes the following steps.
(1) alkali cleaning.
Fluorine-containing oil product is reacted with 10%~30%KOH aqueous solution, and reaction temperature is 60~90 DEG C, and the reaction time 10~
60min, the reaction solution sedimentation separation that will be obtained, upper layer obtain the oil product after defluorinate, and lower layer obtains the lye containing fluoride salt.
(2) it washes.
Alkali cleaning oil product is mixed with water, and mixing temperature is 60~90 DEG C, 10~60min of incorporation time, the liquid that will be obtained
Body separation, upper layer obtains the oil product of dealkalize liquid.
(3) it is dehydrated.
Washing oil product is heated to 100~200 DEG C or vacuumizes be heated to normal pressure relevant temperature, 10~60min of time, separation
Water content in oil out.Remaining dewatered oil product.
(4) it adsorbs.
Oil product is heated to 20~300 DEG C and mixes with adsorbent after dehydration, then 1~200min of time is separated by solid-liquid separation, obtains
The oil product of fluorine content qualification.
Oil product fluorine content determination method.
Using oxygen bomb combustion, that is, allows sample in the oxygen bomb cylinder roasting filled with excessive oxygen, carry out fluorine ion conversion, so
Combustion product is absorbed with boric acid aqueous solution afterwards, with content of fluoride ion in potentiometric determination combustion product.
Instrument: automatic oxygen bomb magnitude instrument, crucible, assay balance (precision 0.1mg), potential measurement instrument, fluorine ion selectivity
Combination electrode, pipette.
Reagent: 1% boric acid absorbing liquid: 1g boric acid is taken to be dissolved in 100mL deionized water.Total cation buffer solution: it weighs
147g sodium citrate and 85g sodium nitrate are dissolved in 800mL water, with concentrated hydrochloric acid (general 10mL), pH meter tune pH=5.5, are transferred to
In 1000mL volumetric flask, it is diluted to scale.
(1) Oxygen Bomb Combustion.
The assay balance for being 0.1mg with precision weighs 0.6 ± 0.1g sample into crucible, and crucible is placed in tripod；
It connects ignition wire and guarantees that fiery silk contacts well with sample in oxygen bomb the two poles of the earth, and do not contacted with crucible internal walls, so as not to it is short-circuit, it measures
The boric acid absorbing liquid of 20mL 1% is in cylinder；Oxygen bomb lid carefully is tightened, the position of crucible and ignition wire is avoided to change because of vibration
Become.Oxygen is poured into oxygen bomb under 2.8-3.2MPa pressure, the oxygenation time is 1 minute；Oxygen bomb is fitted into calorimeter, is covered
Outer cover；Survey Software is opened, information, instrument are automatically performed combustion process to input sample again etc..
(2) content of fluoride ion in Potentiometric Determination combustion product.
Ionometer power supply is opened, electrode must carry out condition processing appropriate according to operation instructions, generally with distillation
Water rinses electrode to current potential 400mv or more.
Blank determination takes 1% boric acid of 20mL and 5mL water in 50mL beaker, moves into 5mL buffer solution, is put into stirring
Son measures its current potential V0。
Sample measures, and after all burnt, takes out oxygen bomb, is vented residual gas, absorbing liquid is transferred in 50mL beaker, uses
5mL distilled water flushing cylinder, flushing liquor are transferred in same beaker, and 5mL buffer solution is moved into beaker, is put into stirrer.
Residual moisture on dry electrode is carefully wiped with filter paper, is inserted into prepare liquid, after ionometer reading is stablized, records potential value
V。
(3) calibration curve is drawn.
Preparation uses fluorobenzene as standard substance, alkane be solvent prepare a series of concentration be 0.5,1,3,5,7,10mg/L
Fluorine ion standard solution, pass through Oxygen Bomb Combustion and potential measurement.
With the logarithm (lg) of concentration for X-axis, current potential is Y-axis, draws standard curve.
(4) it calculates.
Calculation formula.
Blank value
Fluorine content
Content of fluoride ion mg/L, (or ppm)=(F-F0)/M。
In formula: V0--- blank determination current potential, mV.
V --- sample measures current potential, mV.
M --- sample quality, g.
A, b --- the respectively intercept and slope of drawn standard curve, it is slightly poor according to each drafting standard curve
It is different.
(5) points for attention.
1., with distilled water flushing electrode, current potential is made to be restored to 400mV or more, dry discharge electrode after measurement.
2. the crucible for selecting thermal stability good, and strict control sample weighting amount, burn out to prevent crucible.
More specific description is carried out to the present invention by the following examples, but the present invention is not limited to the embodiment described.
Embodiment 1.
The alkylated tar of 50mL fluorinated volume 472.1mg/L, heat exchange to after 90 DEG C with 30% potassium hydroxide solution of 100mL
After mixing 30min, sedimentation separation, upper layer is the defluorinate oil after alkali cleaning, and defluorinate oil is mixed with water, is heated to 60 DEG C, after washed
Layering, then upper layer is heated to 110 DEG C, and sub-argument goes out the moisture in oil product, obtains oil product, is detected fluorine content and is down to 121.3mg/L.
Embodiment 2.
The alkylated tar of 50mL fluorinated volume 472.1mg/L, heat exchange to after 50 DEG C with 30% potassium hydroxide solution of 100mL
After mixing 30min, sedimentation separation, upper layer is the defluorinate oil after alkali cleaning, and defluorinate oil is mixed with water, is heated to 70 DEG C, after washed
Layering, then upper layer is heated to 140 DEG C, and sub-argument goes out the moisture in oil product, obtains oil product, is detected fluorine content and is down to 151.6mg/L.
Embodiment 3.
The alkylated tar of 50mL fluorinated volume 472.1mg/L, heat exchange to after 90 DEG C with 30% potassium hydroxide solution of 250mL
After mixing 30min, sedimentation separation, upper layer is the defluorinate oil after alkali cleaning, and defluorinate oil is mixed with water, is heated to 90 DEG C, after washed
Layering, then upper layer is heated to 180 DEG C, and sub-argument goes out the moisture in oil product, obtains oil product, is detected fluorine content and is down to 58.5mg/L.
Embodiment 4.
Alkylated tar after 50mL fluorine content 58.5mg/L alkali cleaning rinse dehydration, is heated to 100 DEG C and 20g active oxidation
Aluminium carries out mixing and absorption, and after adsorption time 30min, tar fluorine content is 2.9mg/L.
Embodiment 5.
Alkylated tar after 50mL fluorine content 58.5mg/L alkali cleaning rinse dehydration, is heated to 200 DEG C and 40g active oxidation
Aluminium carries out mixing and absorption, and after adsorption time 60min, tar fluorine content is 0.13mg/L.
Embodiment 6.
Alkylated tar after 50mL fluorine content 151.6mg/L alkali cleaning rinse dehydration, is heated to 200 DEG C and 40g active oxygen
Change aluminium and carry out mixing and absorption, after adsorption time 60min, tar fluorine content is 0.14mg/L.Comparative example 1 (no absorption).
The alkylated tar of 50mL fluorinated volume 472.1mg/L, heat exchange is to mixed with 30% ethanolamine solutions of 100mL after 90 DEG C
After closing 30min, sedimentation separation, upper layer is the oil product after alkali cleaning, and fluorine content is down to 273.6mg/L.
Comparative example 2.
Alkylated tar after 50mL fluorine content 58.5mg/L alkali cleaning rinse dehydration, is heated to 100 DEG C and 20g ion exchange
Resin carries out mixing and absorption, and after adsorption time 30min, tar fluorine content is 32.6mg/L.
Claims (6)
1. a kind of oil product defluorination method, which comprises the following steps:
(1) alkali cleaning
Fluorine-containing oil product is reacted at a certain temperature with alkaline aqueous solution, obtained reaction solution sedimentation separation, upper layer obtains defluorinate
Oil, lower layer obtain the lye containing fluoride salt；
(2) it washes
Defluorinate oil obtained in step (1) is mixed with water, obtained liquid is separated, upper layer obtains the oil of dealkalize liquid
Product, lower layer obtain the water containing micro alkali；
(3) it is dehydrated
Upper layer oil obtained in step (2) is heated, or vacuumizes and is heated to normal pressure relevant temperature, 10 ~ 60min of time, separation
Water content in oil out；Remaining dewatered oil product；
(4) it adsorbs
It mixes after oil product heating with adsorbent after being dehydrated obtained in step (3), is then separated by solid-liquid separation, liquid is fluorine content conjunction
The oil product of lattice, solid are adsorbent.
2. oil product defluorination method according to claim 1, which is characterized in that in the step (1), fluorine-containing oil product is any
Fluorine-containing oil product, particularly relates to alkylated tar；
In the step (1), fluorine-containing oil product is reacted with lye at 20 ~ 90 DEG C；
In the step (1), lye is that sodium hydrate aqueous solution, potassium hydroxide aqueous solution, calcium hydroxide aqueous solution, ethanol amine are molten
One or more of liquid, the KOH aqueous solution of preferred concentration 10% ~ 30%；
In the step (1), 10 ~ 60min of reaction time；
In the step (1), lye can be recycled.
3. oil product defluorination method according to claim 1, which is characterized in that in the step (2), defluorinate oil and water are carried out
Mixing, mixing temperature are 20 ~ 90 DEG C, preferably 60 ~ 90 DEG C；This is because the low liquid viscosity of temperature is big, poor fluidity；
In the step (2), 10 ~ 60min of incorporation time；
In the step (2), water can be recycled.
4. oil product defluorination method according to claim 1, which is characterized in that in the step (3), washing oil product exchange heat to
100~200℃；Water can be separated from oil in gaseous form at this temperature, be higher than 200 DEG C, energy consumption increases；
In the step (4), dehydration oil product is heated to 20 ~ 300 DEG C；
In the step (4), 1 ~ 200min of adsorption time；
In the step (4), adsorbent is one or more of aluminum sulfate, resin, activated alumina.
5. oil product defluorination method according to claim 1, which is characterized in that contain to the alkali metal in finally obtained oil product
Amount does not require, and step (2) can be omitted.
6. oil product defluorination method according to claim 1, which is characterized in that if the time of step (1) layering is long, step
Suddenly (3) can be omitted.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112608762A (en) * | 2020-12-18 | 2021-04-06 | 西安元创化工科技股份有限公司 | Liquid-phase defluorinating agent and preparation method and application thereof |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2347945A (en) * | 1941-06-16 | 1944-05-02 | Phillips Petroleum Co | Treatment of hydrocarbon materials |
| US3964993A (en) * | 1975-01-23 | 1976-06-22 | Continental Oil Company | Removal of HF from the sludge resulting from the treatment of a hydrocarbon |
| CN1068100A (en) * | 1991-06-28 | 1993-01-20 | 孟山都公司 | Make the method for alkylbenzene |
| US20110155670A1 (en) * | 2008-04-23 | 2011-06-30 | Uop Llc | Method for removing hydrofluoric acid and organic fluorides from a fluid stream |
| CN109516893A (en) * | 2018-11-16 | 2019-03-26 | 中国石油集团东北炼化工程有限公司沈阳分公司 | A kind of heavy-fluid wax dehydrogenation and re-request are alkylated heavy alkyl benzene technique processed |
-
2019
- 2019-08-15 CN CN201910752645.3A patent/CN110423633A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2347945A (en) * | 1941-06-16 | 1944-05-02 | Phillips Petroleum Co | Treatment of hydrocarbon materials |
| US3964993A (en) * | 1975-01-23 | 1976-06-22 | Continental Oil Company | Removal of HF from the sludge resulting from the treatment of a hydrocarbon |
| CN1068100A (en) * | 1991-06-28 | 1993-01-20 | 孟山都公司 | Make the method for alkylbenzene |
| US20110155670A1 (en) * | 2008-04-23 | 2011-06-30 | Uop Llc | Method for removing hydrofluoric acid and organic fluorides from a fluid stream |
| CN109516893A (en) * | 2018-11-16 | 2019-03-26 | 中国石油集团东北炼化工程有限公司沈阳分公司 | A kind of heavy-fluid wax dehydrogenation and re-request are alkylated heavy alkyl benzene technique processed |
Non-Patent Citations (1)
| Title |
|---|
| 陈向前: "《烷基苯生产和应用》", 31 May 1994, 中国石化出版社 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112608762A (en) * | 2020-12-18 | 2021-04-06 | 西安元创化工科技股份有限公司 | Liquid-phase defluorinating agent and preparation method and application thereof |
| CN112608762B (en) * | 2020-12-18 | 2022-05-03 | 西安元创化工科技股份有限公司 | Liquid-phase defluorinating agent and preparation method and application thereof |
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