CN110003941A - A kind of solvent dephenolization method of mixed triolein or long distillate carbolic oil - Google Patents
A kind of solvent dephenolization method of mixed triolein or long distillate carbolic oil Download PDFInfo
- Publication number
- CN110003941A CN110003941A CN201910362937.6A CN201910362937A CN110003941A CN 110003941 A CN110003941 A CN 110003941A CN 201910362937 A CN201910362937 A CN 201910362937A CN 110003941 A CN110003941 A CN 110003941A
- Authority
- CN
- China
- Prior art keywords
- extractant
- tower
- solvent
- oil
- phenol
- 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.)
- Pending
Links
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
- C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
Landscapes
- 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)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to coal tar processing technology field, the solvent dephenolization method of a kind of mixed triolein or long distillate carbolic oil is disclosed.This method uses two kinds of solvent extraction technologies, the rudimentary phenol in long distillate oil is extracted with extractant A first under higher temperature and pressure condition, then rudimentary phenol is extracted from solvent A with extractant B, finally solvent B and rudimentary phenol are separated with the method for distillation, obtain rudimentary phenolic product.This method can realize that two kinds of solvents are recycled by solvent recovery process, and extractant loss is small, and operating cost is low.This method is suitable for the dephenolize process of high temperature coal-tar mixed triolein, can be used for dephenolize process of the middle coalite tar less than 300 DEG C of long distillate carbolic oils, and wherein the rate of recovery of the rudimentary phenolic compound such as phenol, cresols is up to 90% or more, and does not have pollutant emission.
Description
Technical field
The invention belongs to coal tar processing technology fields, and in particular to the solvent of a kind of mixed triolein or long distillate carbolic oil is de-
Phenol method.
Background technique
Contain multi-chemical in coal tar, for a long time, the resource always as a kind of speciality chemical is domestic and international
Enterprise development and utilization.Rudimentary phenol is one of the staple product separated from coal tar, since the molecule of phenol is weakly acidic,
So with acid-base method (react with phenol generation sodium phenolate with sodium hydroxide solution, sodium phenolate is reduced into phenol by stronger acids again, finally from
Coal tar isolates phenolic compound in fraction containing phenol) it is easy to isolate rudimentary phenolic product from coal tar, this method tool
There are the advantages such as phenol high income, process are simple, operating cost is low, can be used for the processes such as carbolic oil dephenolize, mixed triolein dephenolize, answer always
For in industrial production, but the disadvantage is that reluctant acid sludge, alkaline residue are generated in the process.It is increasingly tight with environmental requirement
The shortcomings that lattice, acid-base method, shows more prominent, and in order to meet current environmental requirement, it is new to start exploitation by people over the past decade
Separation phenol technology, new technology is broadly divided into both direction --- acid-base method technological improvement and non-acid-base method separation phenol technology,
In improved acid-base method be only the reduction of the discharge amount of pollutant, the discharge for not being fully solved alkaline residue and acid sludge is asked
Topic, and most of non-acid-base method separation phenol technologies do not have pollutant emission, belong to the technology of environment-friendly type.
Non- acid-base method phenol technology be can be separated according to the information having disclosed and solvent extraction, ion liquid abstraction are divided into
Method, superheated vapour abstraction technique etc..Although non-soda acid separation phenol technology solves the emission problem of pollutant, different skills
Art still has certain.Wherein solvent used in solvent extraction has glycerine, diethanol amine, small molecule organic amine
Aqueous solution and ammonium hydroxide, the aqueous solution of some inorganic salts etc., due to the limitation of selected solvent and process flow, this kind of skill
The shortcomings such as that all there is phenolic compound yields is low for art, extraction efficiency is low, and that there are also solvent losses is big, raw for some technologies
Produce the problems such as costly；Ion liquid abstraction technology can obtain relatively high phenolic compound selectivity, but due to ionic liquid
Higher cost, regeneration expense and consumption are likely to result in this kind of technology producing cost height, to influence its economy；Overheat
Water vapour abstraction technique needs to operate at a higher temperature, and one side energy consumption is higher, on the other hand since used water steams
Oil gas is mixed in vapour, water supply steam circulation use brings difficulty.
Summary of the invention
The purpose of the present invention is to provide the solvent dephenolization methods of a kind of mixed triolein or long distillate carbolic oil, have reached height
The purpose of effect, with high selectivity separating phenols compounds, and there is no pollutant emission.
To achieve the above object, the invention adopts the following technical scheme:
The present invention provides the solvent dephenolization method of a kind of mixed triolein or long distillate carbolic oil, comprising the following steps:
To contain phenol feedstock oil and extractant A heat, boost respectively after be sent into extraction tower and carry out counter-current extraction, obtain extraction phase and contain
The volume ratio of phenol solvent A and the thick dephenolize oil of raffinate phase, the extractant A and the feedstock oil containing phenol is 0.1~10:1, extraction temperature
It is 0.1~1.5MPa for 60~150 DEG C, extracting pressure, extractant A is the aqueous solution of small molecular alcohol, is contained in extractant small
The concentration of molecule alcohol is 10~90wt%；
The thick dephenolize oil of raffinate phase is flowed out from the top of extraction tower, and stripping tower I is sent into after depressurizing, is passed through in stripping tower I
The small molecular alcohol dissolved in the thick dephenolize oil of air lift removing raffinate phase obtains dephenolize oil, and the dephenolize oil flowed out from stripping tower I tower bottom is made
It sends out after the small molecular alcohol out-of-bounds, come out from stripping tower I tower top is condensed for product and is recycled for configuring extractant A；
The extraction phase solvent A containing phenol is sent into dealcoholysis tower from extraction tower bottom outflow after depressurizing, will through distillation in dealcoholysis tower
Small molecular alcohol is separated with water and phenolic compound, and the small molecular alcohol flowed out from dealcoholysis column overhead is recycled after being condensed, from
The water of dealcoholysis tower tower bottom outflow and the mixed liquor of phenolic compound, which are divided into after heat exchange is cooled to 35~40 DEG C into separator, to be contained
Phenol water and phenolic compound, phenolic compound are sent out out-of-bounds as crude phenols product, and water containing phenol is admitted to stripping column；
Water containing phenol from separator and extractant B are sent into stripping column and carry out counter-current extraction, the extractant B with contain phenol
The volume ratio of water is 5~50:100, and the dephenolize water flowed out from stripping column bottom enters stripping tower II extractant B after air lift
It is separated with water, wherein extractant B is recycled, and water is for preparing extractant A recycling；At the top of from stripping column
The B of solvent containing phenol of outflow is sent into destilling tower, and phenolic compound and extractant B after distilling in the B of solvent containing phenol are separated,
Wherein phenolic compound is sent out out-of-bounds as crude phenols product, and extractant B is recycled；The extraction temperature of stripping column be 20~
50 DEG C, back extraction pressure be normal pressure.
Preferably, the volume ratio of extractant A and the feedstock oil containing phenol is 0.8~5:1 in the extraction tower, the extraction temperature
Degree is 80~130 DEG C, and extracting pressure is 0.2~0.8MPa.
Preferably, the concentration of the extractant A is 40~80wt%.
Preferably, the extractant A is methanol aqueous solution or ethanol water or methanol aqueous solution and ethanol water
Mixture.
Preferably, extractant B is Di Iso Propyl Ether or methyl iso-butyl ketone (MIBK) in the stripping column.
Preferably, the volume ratio of the extractant B and the water containing phenol is 5~20:100.
Compared with prior art, the beneficial effects of the present invention are:
The present invention uses double solvent extraction technology, develops suitable process flow, has reached efficient, has separated phenol with high selectivity
The purpose of class compound and hydrocarbon compound, and there is no pollutant emission；Solvent circulating repetition uses, and reduces operating cost；
This method suitable for high temperature coal-tar mixed triolein, naphtalene oil, washing oil and phenol generalization in coalite tar carbolic oil long distillate carbolic oil
The separation for closing object, particularly with the extraction of the rudimentary phenol such as phenol, cresols, the rate of recovery of phenolic compound is up to 90% or more.
Detailed description of the invention
Fig. 1 is the solvent dephenolization method flow diagram of a kind of mixed triolein of the present invention or long distillate carbolic oil.
It is attached marked in the figure: 1 be extraction tower, 2 be stripping tower I, 3 be dealcoholysis tower, 4 be separator, and 5 be stripping column, and 6 be gas
Stripper II, 7 be destilling tower.
Specific embodiment
The following examples are intended to illustrate the invention, but is not used to limit the scope of protection of the present invention.Unless otherwise specified, real
Apply the conventional means that technological means used in example is well known to those skilled in the art.Test method in following embodiments, such as
It is conventional method without special instruction.
The test process and test method of embodiment are as follows:
The present embodiment is respectively with low temperature coal tar in table mountain high temperature coal-tar mixed triolein (carbolic oil+naphtalene oil+washing oil) and Yulin
Oily long distillate carbolic oil (170~300 DEG C of fractions) is feedstock oil containing phenol, and composition and property are listed in Tables 1 and 2 respectively, are filling
It sets and is tested, process flow is as shown in Figure 1, i.e. respectively with methanol aqueous solution, ethanol water or methanol aqueous solution and second
The mixture of alcohol solution as extractant A, the concentration of extractant A small molecular alcohol control respectively in 50wt% and
Two levels of 75wt%, extractant A and feedstock oil containing phenol carry out counter-current extraction in extraction tower 1, and the diameter of extraction tower 1 is
100mm, height 3000mm, theoretical cam curve 15, extraction temperature are controlled respectively in 80 DEG C, 120 DEG C of two conditions, extraction tower 1
Pressure controls within the scope of 0.1~1.5MPa respectively according to the difference of solvent.
The thick dephenolize oil of raffinate phase is flowed out from the top of extraction tower 1, and stripping tower I2 is sent into after being depressured, and (stripping tower I is filler
Tower, internal diameter 150mm, height 1500mm), the small molecule in stripping tower I2 by being dissolved in the thick dephenolize oil of air lift removing raffinate phase
Alcohol obtains dephenolize oil, and when methanol aqueous solution is as extractant A, stripping tower I2 pushes up temperature and controls at 60~70 DEG C, stripping tower
I2 tower top methanol send to solvent circulating tank through condensation and is recycled for preparing extractant A, and stripping tower I2 tower bottom dephenolize oil is made
Go out device for product；When ethanol water is as extractant A, the control of stripping tower I2 tower top temperature is at 75~85 DEG C, air lift
Ethyl alcohol is obtained after the condensation of tower I2 overhead gas to send to solvent circulating tank for preparing extractant A recycling, stripping tower I2 tower
Bottom dephenolize oil goes out device as product；When the mixture of methanol aqueous solution and ethanol water is as extractant A, stripping tower
The control of I2 tower top temperature obtains the mixture and a small amount of water of methanol, ethyl alcohol after 75~85 DEG C, the condensation of stripping tower I2 overhead gas,
It send to solvent circulating tank and is recycled for preparing extractant A, stripping tower I2 tower bottom dephenolize oil goes out device as product.
Extraction phase solvent A containing phenol is sent into dealcoholysis tower 3 after being depressured, being exchanged heat, and in dealcoholysis tower 3, (dealcoholysis tower 3 is packed tower, interior
Diameter 150mm, height 1600mm) in small molecular alcohol and water and phenolic compound are separated through distilling, from 3 tower top of dealcoholysis tower outflow
Small molecular alcohol be condensed after be recycled.When methanol aqueous solution is as extractant A, the control of 3 tower top temperature of dealcoholysis tower exists
65~75 DEG C, the methanol of removing is flowed out from tower top, and being sent after condensing to solvent circulating tank makes for preparing extractant A circulation
With the mixed liquor of tower bottom water and phenolic compound is sent after heat exchange is cooled to 35~40 DEG C to separator, is divided into the separator
Water containing phenol (water phase) and phenolic compound (phenol phase), wherein phenol is mutually used as product carrying device, and water phase is sent (anti-to stripping column 5
Extraction tower 5 internal diameter 100mm, height 3000mm, theoretical cam curve 15, extraction temperature are controlled respectively in 20 DEG C, 50 DEG C of two items
Part, pressure are normal pressure)；When ethanol water is as extractant A, the control of 3 tower top temperature of dealcoholysis tower is at 80~90 DEG C, tower top
Hydrous ethanol (concentration of alcohol about 95w%) is obtained after gas condensation to send to solvent circulating tank for preparing extractant A circulation
It uses, the mixed liquor of tower bottom water and phenolic compound is sent after heat exchange is cooled to 35~40 DEG C to separator 4, in separator 4
It is divided into water containing phenol (water phase) and phenolic compound (phenol phase), wherein phenol is mutually used as product carrying device, and water phase is sent to stripping column
5；When the mixture of methanol aqueous solution and ethanol water is as extractant A, 3 tower top temperature of dealcoholysis tower is controlled 80~90
DEG C, the mixture and a small amount of water of methanol, ethyl alcohol are obtained after overhead gas condensation, is sent to solvent circulating tank for preparing extractant
A is recycled, and the mixed liquor of tower bottom water and phenolic compound is sent after heat exchange is cooled to 35~40 DEG C to separator 4, is separating
It is divided into water containing phenol (water phase) and phenolic compound (phenol phase) in device 4, wherein phenol is mutually used as product carrying device, and water phase is sent to back extraction
Take tower 5.
Enter the top of stripping column from the water containing phenol of separator 4, extractant B enters the lower part of stripping column 5, contains
The volume flow control of phenol water and extractant B in two levels of 100:5 and 100:20, after counter-current extraction the B of solvent containing phenol from
It is flowed out at the top of stripping column 5, send to destilling tower 7 (destilling tower 7 is packed tower, internal diameter 100mm, height 1600mm) and obtained after distilling
To phenolic compound and extractant B, wherein extractant B is recycled, and phenolic compound goes out device as crude phenols product；From anti-
The dephenolize water of 5 bottom of extraction tower outflow, into stripping tower II6, (stripping tower II6 is packed tower, internal diameter 150mm, height
1500mm), through extractant B a small amount of in air lift removing water, extractant B, which is used as, to be recycled, and water circulation is for preparing extraction
Take solvent A.When diisopropyl ether is as extractant B, stripping tower II6 head temperature and the control of 7 tower top temperature of destilling tower are 55
Within the scope of~65 DEG C；When methyl iso-butyl ketone (MIBK) is as extractant B, 7 tower top temperature of stripping tower II6 head temperature and destilling tower
Control is within the scope of 80~90 DEG C.
The composition and property of 1 table mountain high temperature coal-tar mixed triolein of table
The composition and property of coalite tar long distillate carbolic oil in 2 Yulin of table
| Project | Index |
| Density (20 DEG C), kg/m3 | 992.6 |
| Acidity, mg (KOH)/100mL | 36.7 |
| Rudimentary phenol content, m% | 14.6 |
| Elemental analysis, % | |
| H | 8.95 |
| C | 79.81 |
| N | 0.65 |
| S | 0.24 |
| O | 10.35 |
| It is total | 100.00 |
| Boiling range, C | |
| IBP | 197 |
| 10% recovered (distilled) temperature | 212 |
| 30% recovered (distilled) temperature | 227 |
| 50% recovered (distilled) temperature | 244 |
| 70% recovered (distilled) temperature | 268 |
| 90% recovered (distilled) temperature | 293 |
| 95% recovered (distilled) temperature | 304 |
Embodiment 1-5
According to above-mentioned test process and test method, table is listed in using table mountain high temperature coal-tar mixed triolein as the test result of raw material
3。
Test result of the table 3 using table mountain high temperature coal-tar mixed triolein as raw material at different conditions
Note: phenol in the sum of phenol, cresols, xylenol amount/feedstock oil containing phenol in the rudimentary phenol rate of recovery=crude phenols product, cresols,
The sum of xylenol amount * 100；The sum of phenol, cresols, concentration of xylenol in rudimentary phenol selectivity=crude phenols product.
Embodiment 6-10
According to above-mentioned test process and test method, using coalite tar long distillate carbolic oil in Yulin as the test of raw material
As a result it is listed in table 4.
Table 4 is using test result of the coalite tar long distillate carbolic oil as raw material at different conditions in Yulin
Note: phenol, cresols in the sum of phenol, cresols and xylenol amount/feedstock oil containing phenol in the rudimentary phenol rate of recovery=crude phenols product
With the sum of xylenol amount * 100；The sum of phenol, cresols and concentration of xylenol in rudimentary phenol selectivity=crude phenols product.
The embodiment of the above, only presently preferred embodiments of the present invention, is only used to explain the present invention, not limit
The scope of the present invention processed to those of ordinary skill in the art certainly can be according to skill disclosed in this specification
Art content makes other embodiments easily by way of replacing or changing, therefore all made in the principle of the present invention
Changes and improvements etc., should be included in scope of the present invention patent.
Claims (6)
1. the solvent dephenolization method of a kind of mixed triolein or long distillate carbolic oil, which comprises the following steps:
Phenol feedstock oil will be contained and extractant A distinguishes feeding extraction tower progress counter-current extraction after heated, boosting, obtain extraction phase
The volume ratio of solvent A containing phenol and the thick dephenolize oil of raffinate phase, the extractant A and the feedstock oil containing phenol is 0.1 ~ 10:1, extraction temperature
Degree is 60 ~ 150 DEG C, extracting pressure is 0.1 ~ 1.5MPa, and extractant A is the aqueous solution of small molecular alcohol, is contained in extractant small
The concentration of molecule alcohol is 10 ~ 90wt%；The feedstock oil containing phenol is that high temperature coal-tar mixed triolein or middle coalite tar long distillate contain
Carbolic oil；
The thick dephenolize oil of raffinate phase is flowed out from the top of extraction tower, and stripping tower I is sent into after depressurizing, is passed through in stripping tower I
The small molecular alcohol dissolved in the thick dephenolize oil of air lift removing raffinate phase obtains dephenolize oil, and the dephenolize oil flowed out from stripping tower I tower bottom is made
It sends out after the small molecular alcohol out-of-bounds, come out from stripping tower I tower top is condensed for product and is recycled for configuring extractant A；
The extraction phase solvent A containing phenol is sent into dealcoholysis tower from extraction tower bottom outflow after depressurizing, will through distillation in dealcoholysis tower
Small molecular alcohol is separated with water and phenolic compound, and the small molecular alcohol flowed out from dealcoholysis column overhead is recycled after being condensed, from
The water of dealcoholysis tower tower bottom outflow and the mixed liquor of phenolic compound enter separator after heat exchange is cooled to 35 ~ 40 DEG C and are divided into containing phenol
Water and phenolic compound, phenolic compound are sent out out-of-bounds as crude phenols product, and water containing phenol is admitted to stripping column；
Water containing phenol from separator and extractant B are sent into stripping column and carry out counter-current extraction, the extractant B with contain phenol
The volume ratio of water is 5 ~ 50:100, and the dephenolize water flowed out from stripping column bottom enters stripping tower II extractant B after air lift
It is separated with water, wherein extractant B is recycled, and water is for preparing extractant A；What is flowed out at the top of from stripping column contains
Phenol solvent B is sent into destilling tower, and phenolic compound and extractant B after distilling in the B of solvent containing phenol are separated, wherein phenols
Compound is sent out out-of-bounds as crude phenols product, and extractant B is recycled；The extraction temperature of stripping column is 20 ~ 50 DEG C, is stripped
Taking pressure tower is normal pressure.
2. the solvent dephenolization method of a kind of mixed triolein according to claim 1 or long distillate carbolic oil, which is characterized in that institute
The volume ratio for stating extractant A and the feedstock oil containing phenol is 0.8 ~ 5:1, and the extraction temperature is 80 ~ 130 DEG C, extracting pressure 0.2
~0.8MPa。
3. the solvent dephenolization method of a kind of mixed triolein according to claim 1 or long distillate carbolic oil, which is characterized in that institute
The concentration for stating extractant A is 40 ~ 80wt%.
4. the solvent dephenolization method of a kind of mixed triolein according to claim 1 or long distillate carbolic oil, which is characterized in that institute
State the mixture that extractant A is methanol aqueous solution or ethanol water or methanol aqueous solution and ethanol water.
5. the solvent dephenolization method of a kind of mixed triolein according to claim 1 or long distillate carbolic oil, which is characterized in that institute
Stating extractant B is Di Iso Propyl Ether or methyl iso-butyl ketone (MIBK).
6. the solvent dephenolization method of a kind of mixed triolein according to claim 1 or long distillate carbolic oil, which is characterized in that institute
Stating the volume ratio of extractant B and the water containing phenol in stripping column is 5 ~ 20:100.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910362937.6A CN110003941A (en) | 2019-04-30 | 2019-04-30 | A kind of solvent dephenolization method of mixed triolein or long distillate carbolic oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910362937.6A CN110003941A (en) | 2019-04-30 | 2019-04-30 | A kind of solvent dephenolization method of mixed triolein or long distillate carbolic oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110003941A true CN110003941A (en) | 2019-07-12 |
Family
ID=67175313
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910362937.6A Pending CN110003941A (en) | 2019-04-30 | 2019-04-30 | A kind of solvent dephenolization method of mixed triolein or long distillate carbolic oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110003941A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114832436A (en) * | 2022-06-20 | 2022-08-02 | 运城市盐湖区禾呈信息技术有限公司 | Process for extracting crude phenol from phenol oil by secondary extraction of composite extracting agent |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000044699A1 (en) * | 1999-01-29 | 2000-08-03 | Ecovac Pyrocycling Technologies Inc. | Process for the production of phenolic-rich pyrolysis oils for use in making phenol-formaldehyde resol resins |
| JP2002047226A (en) * | 2000-07-26 | 2002-02-12 | National Institute Of Advanced Industrial & Technology | Method for separating and recovering phenol compound and hydrocarbon oil from mixture containing the components |
| CN102219649A (en) * | 2011-04-22 | 2011-10-19 | 煤炭科学研究总院 | Method of extracting phenolic compound from coal liquefied oil or coal tar |
| CN106278827A (en) * | 2016-07-22 | 2017-01-04 | 煤炭科学技术研究院有限公司 | A kind of method and device of extract and separate phenolic compound from coal derived oils |
-
2019
- 2019-04-30 CN CN201910362937.6A patent/CN110003941A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000044699A1 (en) * | 1999-01-29 | 2000-08-03 | Ecovac Pyrocycling Technologies Inc. | Process for the production of phenolic-rich pyrolysis oils for use in making phenol-formaldehyde resol resins |
| JP2002047226A (en) * | 2000-07-26 | 2002-02-12 | National Institute Of Advanced Industrial & Technology | Method for separating and recovering phenol compound and hydrocarbon oil from mixture containing the components |
| CN102219649A (en) * | 2011-04-22 | 2011-10-19 | 煤炭科学研究总院 | Method of extracting phenolic compound from coal liquefied oil or coal tar |
| CN106278827A (en) * | 2016-07-22 | 2017-01-04 | 煤炭科学技术研究院有限公司 | A kind of method and device of extract and separate phenolic compound from coal derived oils |
Non-Patent Citations (3)
| Title |
|---|
| 中国化工防治污染技术协会: "《化工废水处理技术》", 28 April 2000, 化学工业出版社 * |
| 尚建选等: "《低阶煤分质转化多联产技术》", 30 May 2013, 煤炭工业出版社 * |
| 张明等: "《煤制合成天然气技术与应用》", 31 October 2017, 化学工业出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114832436A (en) * | 2022-06-20 | 2022-08-02 | 运城市盐湖区禾呈信息技术有限公司 | Process for extracting crude phenol from phenol oil by secondary extraction of composite extracting agent |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106588579B (en) | A method of extracting phenolic compound from carbolic oil | |
| CN106145426B (en) | Carbolic oil joint removing system and treatment process in a kind of coal chemical industrial waste water | |
| CN103420442B (en) | Method for extracting high-concentration phenol-containing coal chemical industry wastewater at high temperature by using methyl isobuthyl ketone | |
| CN103695036B (en) | Middle coalite tar processing and treating method | |
| CN102219649A (en) | Method of extracting phenolic compound from coal liquefied oil or coal tar | |
| CN101143805B (en) | Method for separating phenols compounds from phenol-containing raw material oil | |
| CN101913718A (en) | Method for extracting and dephenolizing coal chemical industry wastewater | |
| CN105296135B (en) | A kind of regeneration method of waste lubricating oil | |
| CN105016554A (en) | Semi-coke wastewater treatment process | |
| CN102153449A (en) | Continuous refining separation device and method for coal gasification crude phenol | |
| CN102021010A (en) | Processing method of middle and low temperature coal tar | |
| CN102633597B (en) | Process of recovering ethanol, propyl alcohol and isobutyl alcohol from polyalcohol-water mixture | |
| CN105198711A (en) | Coked crude phenol refining device and method | |
| CN103896739A (en) | Method for extracting phenol compounds from direct coal liquefied oil through extractive distillation | |
| CN109825322B (en) | Method for extracting phenolic substances from coal tar or direct coal liquefaction oil | |
| CN110015949A (en) | A method of from extraction phenolic substances in feedstock oil containing phenol | |
| CN110003939A (en) | A kind of efficient carbolic oil dephenolization method | |
| CN110003941A (en) | A kind of solvent dephenolization method of mixed triolein or long distillate carbolic oil | |
| CN107446606A (en) | The technique and device of a kind of coal tar production modified coal tar pitch, aliphatic hydrocarbon and aromatic hydrocarbon | |
| CN108395367B (en) | Method for separating phenolic compounds from coal tar | |
| CN101974345A (en) | Method for processing low-temperature pyrolyzed coal tar | |
| CN103923690A (en) | Method for extracting FCC oil slurry aromatic hydrocarbons | |
| CN102351358B (en) | Method and system for treating phenol-containing acidic water by direct liquefaction with coal | |
| CN101619230A (en) | Method for recycling organic compounds from caustic sludge generated in coal tar oil light end alkali cleaning | |
| CN106866382A (en) | The extracting method of aldehydes matter in a kind of catalytic lignin depolymerization product liquid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190712 |
|
| RJ01 | Rejection of invention patent application after publication |