CN103436289A - Method for producing naphthenic base transformer oil base oil by using coal tar oil - Google Patents
Method for producing naphthenic base transformer oil base oil by using coal tar oil Download PDFInfo
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Abstract
The invention relates to a method for producing naphthenic base transformer oil base oil by using coal tar oil. The method is characterized in that high-additional value products such as naphtha oil, diesel oil and transformer oil base oil are obtained by adopting the steps of hydrotreating of the coal tar oil, the fractional distillation of hydrogenated products, solvent refining of transformer distillate oil and clay refining of the transformer distillate oil. The method has the advantages that the hydrogenation industrial chain of the coal tar oil is extended, the coal tar oil resource is reasonably utilized, the utilization value of the coal tar oil is increased, meanwhile, the density of the coal tar oil hydrogenated diesel oil can be reduced, the cycloparaffin distillate oil (300-360 DEG C) with high content can be obtained, the quality of the transformer oil base oil is ensured, and the obtained transformer oil base oil has high quality and high yield and is in line with the standards on the transformer oil No. 45 in national GB2536-1990 transformer oil.
Description
Technical field
The invention belongs to the coal tar production technical field, particularly a kind of method with coal tar production cycloalkyl transformer oil base oil.
Background technology
The main application of transformer oil is by transformer insulated and cooling.Since transmitting transformer invention, people are just striving to find a kind of insulation that can meet transformer, the performance requriements such as cooling always, again can long-term stable operation, low-cost medium.Through long-term actual use, naphthenic base oils is acknowledged as a kind of selection of the best, is also safe, the most most economical selection.At present, global transformer manufacturers, the transformer that particularly large multinational company such as ABB, Alstom produces, adopt the transformer oil of producing with naphthenic base oils bar none.
Naphthenic base oils at high temperature viscosity is low, and the dissolving power under extremely low temperature is good, and has very high oxidation stability, fabulous electrical specification and good heat-transfer medium characteristic, thus oil for the best that makes it become transformer.But the reserves of naphthenic base crude only account for 2%～3% of crude oil total reserves, due to the shortage of naphthenic base crude resource, in China, still have a considerable amount of transformer oil by non-cycloalkyl crude production.
There is at present the kinds of processes method to produce transformer oil both at home and abroad.
The people such as Guo Huai disclose a kind ofly take atmospheric distillate as raw material, (Guo Huai etc., face No. 25 ultrahigh voltage transformer oils of hydrogen explained hereafter, refining of petroleum and chemical industry to the method for adopt that alkali cleaning is refining, ultrahigh voltage transformer oil is produced in furfural treatment, hydrofining technology, the 2nd phase in 1999,56-57).But the alkali washing process of the method can bring certain pollution, and the standard that product yield is low, condensation point does not reach No. 45 transformer oil.
U.S. Pat 5167847 be take paraffinic crude as raw material, by hydrocracking, solvent dewaxing process, produces transformer oil; It is raw material that U.S. Pat 4018666 be take the cut of 310-400 ℃ of paraffinic crude, by solvent treatment Arene removal and polar material, produces transformer oil; CN1110709 discloses a kind of method with production of transformer oil with hydrocracking tail oil, the method is by adding aromatic hydrocarbon (alkylbenzene, refining heavy alkyl benzene or alkylnaphthalene) and naphthene base crude oil to improve its light stability in hydrocracking tail oil, all contain aliphatic hydrocarbon in raw material in these methods and product, so quality product does not have the cycloalkyl transformer oil good.
Chinese patent CN100537722 discloses a kind of production method of ultrahigh voltage transformer oil, it is raw material that the method adopts the atmospheric distillate of naphthenic base crude and one or more of vacuum distillate, and it is carried out to hydrotreatment and hydrofining obtains ultrahigh voltage transformer oil.This method is raw materials used is fraction oil of petroleum, and the raw material of present method is more unmanageable coal tar, so also there are larger difference in processing method and correlation parameter.
The raw material of the Technology of above these reports is fraction oil of petroleum, still not take coal tar or its derived product to prepare the technique report of whiteruss as raw material.The contriver is further finding to have a large amount of naphthenic hydrocarbon and aromatic hydrocarbons in the coal tar hydrogenating product in R&D process, can be used as the raw material of preparation cycloalkyl transformer oil.
Summary of the invention
The object of the invention is in order to realize that coal tar prepares as stock oil that naphthenic hydrocarbon distillate content is high, the measured cycloalkyl transformer oil of matter, provide that a kind of technique is simple, cost is low and rationally utilized the method for the coal tar production cycloalkyl transformer oil base oil of tar resource.
The present invention realizes that the technical scheme that above-mentioned purpose adopts is comprised of following steps:
(1) coal tar hydrogenating is processed
Coal tar is mixed with hydrogen, carry out hydrotreatment under the katalysis of Hydrobon catalyst and catalytic dewaxing catalyst in hydrogenator, temperature of reaction is 300～400 ℃, pressure is 10～15MPa, hydrogen to oil volume ratio is 800～1500:1, with respect to the liquid volume air speed of Hydrobon catalyst, is 0.3～0.6h
-1, with respect to the liquid volume air speed of catalytic dewaxing catalyst, be 0.6～1.0h
-1, obtain hydrogenated oil;
(2) fractionation of hydrogenation products
Hydrogenated oil is sent into to fractionation in separation column, obtain being less than 180 ℃ naphtha fraction, 180～300 ℃ diesel oil distillate, 300～360 ℃ the transformer oil cut and be greater than the residue fraction of 360 ℃;
(3) solvent treatment of transformer distillate
With selective solvent, transformer oil cut countercurrent mass transfer in extraction tower is conducted heat and extracts, transformer oil after extraction carries out underpressure distillation and removes residual solvent in solvent recovery unit, the volume ratio of transformer oil cut and selective solvent is 1:1～2, the extraction tower tower top temperature is that 80～90 ℃, column bottom temperature are 40～50 ℃, completes solvent treatment;
Above-mentioned selectivity volume is phenol or N-first class pyrrolidone or furfural;
(4) the transformer distillate is clay-filtered
Under nitrogen protection, the transformer oil cut after solvent treatment to be mixed with carclazyte, the carclazyte add-on is 7～10% of transformer oil cut quality after solvent treatment, stirs, 130～150 ℃ of reaction 40～50min, cooling, filter, obtain transformer oil base oil.
Above-mentioned Hydrobon catalyst is to take the molybdenum-nickel type catalyzer that aluminium sesquioxide is carrier, and in its catalytically-active metals, molybdic oxide content is at least 21wt%, and nickel oxide content is at least 6wt%, and total pore volume is at least 0.3mL/g, and specific surface area is at least 150m
2/ g;
The ZSM-5 zeolite catalytic dewaxing catalyst that above-mentioned catalytic dewaxing catalyst is nickel-loaded, in catalytically-active metals, nickel oxide content is 1～3wt%, and total pore volume is at least 0.1mL/g, and specific surface area is at least 200m
2/ g.
Above-mentioned steps (1) is mixed coal tar with hydrogen, carry out hydrotreatment under the katalysis of Hydrobon catalyst and catalytic dewaxing catalyst in hydrogenator, preferably 350～380 ℃ of temperature of reaction, be preferably 380 ℃, pressure is 12～14MPa preferably, is preferably 14MPa, and hydrogen to oil volume ratio is 900～1200:1 preferably, be preferably 1000:1, with respect to the preferred 0.4～0.5h of the liquid volume air speed of Hydrobon catalyst
-1, be preferably 0.4h
-1, with respect to the preferred 0.8～0.9h of the liquid volume air speed of catalytic dewaxing catalyst
-1, be preferably 0.8h
-1, obtain hydrogenated oil.
Above-mentioned steps (3) in solvent recovery unit is carried out underpressure distillation after countercurrent mass transfer heat transfer extraction to the transformer oil cut with selective solvent and is removed residual solvent in extraction tower, the volume ratio of transformer oil cut and selective solvent is preferably 1:1.2～1.8, be preferably 1:1.2, the extraction tower tower top temperature is that 85～90 ℃, column bottom temperature are 45 ℃, better tower top temperature is that 90 ℃, column bottom temperature are 45 ℃, completes solvent treatment.
Above-mentioned steps (4), under nitrogen protection, is mixed the transformer oil cut after solvent treatment and carclazyte, and the better add-on of carclazyte is 8% of transformer oil cut quality after solvent treatment; stir, 140 ℃ of reaction 40min, cooling; filter, obtain transformer oil base oil.
The method of a kind of coal tar production cycloalkyl transformer oil base oil provided by the present invention, by coal tar hydrogenating and distillate solvent treatment, clay-filtered technique has been carried out rational coupling, take full advantage of its adsorptive power to impurity positively charged in transformer oil of ability that atlapulgite has adsorpting pigment and organic molecule and remove residual solvent and colloid in oil product, the objectionable impuritiess such as basic nitrogen, improve the anti-oxidative stability and the color of improving oil product of oil product, and then obtained petroleum naphtha, the high value added product such as diesel oil and transformer oil base oil, extended the coal tar hydrogenating industrial chain, rationally utilized tar resource, improved the utility value of coal tar, can reduce the density of coal tar hydrogenating diesel oil simultaneously, obtain the naphthenic hydrocarbon distillate (300～360 ℃) of high-content, guaranteed the quality of transformer oil base oil, the acquisition transformer oil base oil is of fine quality, yield is high and meet the standard of No. 45 transformer oil in national GB2536-1990 " transformer oil ".
The accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
Embodiment
Now in conjunction with the accompanying drawings and embodiments technical scheme of the present invention is further described, but the present invention is not limited only to following enforcement situation.
Embodiment 1
500～700 ℃ of coalite tars that produce of take in the coal pyrolysis process are raw material, and the method for production cycloalkyl transformer oil base oil realizes by following steps, referring to Fig. 1:
(1) coal tar hydrogenating is processed
Coal tar is mixed and sends in hydrogenator with hydrogen, carry out hydrotreatment take under molybdenum-nickel type Hydrobon catalyst that aluminium sesquioxide is carrier and the katalysis with the ZSM-5 zeolite catalytic dewaxing catalyst of nickel-loaded successively, temperature of reaction is 380 ℃, pressure is 14MPa, hydrogen to oil volume ratio is 1000:1, with respect to the liquid volume air speed of Hydrobon catalyst, is 0.4h
-1, with respect to the liquid volume air speed of catalytic dewaxing catalyst, be 0.8h
-1, obtain hydrogenated oil;
The molybdenum-nickel type Hydrobon catalyst that above-mentioned aluminium sesquioxide is carrier is the TK-561 type catalyzer (http://www.topsoe.com/products/CatalystPortfolio.aspx) that adopts the exploitation of TOPSOE company, in its catalytically-active metals, molybdic oxide content is at least 21wt%, nickel oxide content is at least 6wt%, total pore volume is at least 0.3mL/g, and specific surface area is at least 150m
2/ g; The ZSM-5 zeolite catalytic dewaxing catalyst of above-mentioned nickel-loaded adopts the FDW-3 type catalyzer (http://sinopec-catalyst.com/product/detail/id/31.html) of catalyzer branch office of Sinopec Group, its catalyst activity Oxygen in Metals nickel content is 1～3wt%, total pore volume is at least 0.1mL/g, and specific surface area is at least 200m
2/ g.
(2) fractionation of hydrogenation products
Hydrogenated oil is sent into to fractionation in separation column, obtain being less than 180 ℃ naphtha fraction, 180～300 ℃ diesel oil distillate, 300～360 ℃ the transformer oil cut and be greater than the residue fraction of 360 ℃;
(3) solvent treatment of transformer distillate
With N-first class pyrrolidone, transformer oil cut countercurrent mass transfer in extraction tower is conducted heat and extracts, be that N-first class pyrrolidone is squeezed in extraction tower from tower top by pump after preheating, the transformer oil cut is squeezed in extraction tower at the bottom of tower, carry out the countercurrent mass transfer heat transfer, transformer oil after extraction enters in solvent recovery unit and carries out underpressure distillation and remove remaining N-first class pyrrolidone, the volume ratio of transformer oil cut and N-first class pyrrolidone is 1:1.2, the extraction tower tower top temperature is 90 ℃, column bottom temperature is 45 ℃, complete solvent treatment, obtain the transformer oil cut after solvent treatment,
(4) the transformer distillate is clay-filtered
Under nitrogen protection; transformer oil cut after solvent treatment is mixed with carclazyte; the mass percent that carclazyte accounts for the transformer oil cut is 8%; stir; 140 ℃ of reaction 40min, cooling, filter; obtain transformer oil base oil, yield is that the transformer distillate of 300～360 ℃ that 78.5wt%(be take after hydrotreatment is 100%).
The yield of the naphtha fraction of the present embodiment gained, diesel oil distillate and transformer oil cut and the character of product transformer oil base oil see the following form respectively 1～4.
The yield of table 1 embodiment 1 resulting various products
Annotate: with feed coal tar 100%, calculate.
The naphtha fraction character that table 2 embodiment 1 obtains
As shown in Table 2, the sulphur of this naphtha fraction, nitrogen, olefin(e) centent are very low, and aromaticity content is less than 40%.Research octane number (RON) 72.1 is less than 90, all reaches motor spirit GB17930-2006 standard, can be used as premium blend component or solvent oil.
The character of resulting 180～300 ℃ of diesel oil distillates of table 3 embodiment 1
As shown in Table 3, the sulphur of this diesel oil distillate, nitrogen content are very low, and condensation point has reached-20 ℃, and each index has all reached the regulation of standard GB/T 252-2000, can be used as fine-quality diesel oil blending component.
Table 4 embodiment 1 obtains the transformer foundation oil properties
As shown in Table 4, resulting transformer foundation oil indices all meets the regulation of GB GB2536-1990.
Embodiment 2
In the present embodiment, step (1) is mixed coal tar to send in hydrogenator with hydrogen, carry out hydrotreatment take under molybdenum-nickel type Hydrobon catalyst that aluminium sesquioxide is carrier and the katalysis with the ZSM-5 zeolite catalytic dewaxing catalyst of nickel-loaded successively, temperature of reaction is 350 ℃, pressure is 13MPa, hydrogen to oil volume ratio is 900:1, with respect to the liquid volume air speed of Hydrobon catalyst, is 0.5h
-1, with respect to the liquid volume air speed of catalytic dewaxing catalyst, be 0.9h
-1, obtain hydrogenated oil.Step (3) is conducted heat and is extracted transformer oil cut countercurrent mass transfer in extraction tower with N-first class pyrrolidone, transformer oil after extraction enters in solvent recovery unit and carries out underpressure distillation and remove remaining N-first class pyrrolidone, the volume ratio of transformer oil cut and N-first class pyrrolidone is 1:1.6, the extraction tower tower top temperature is that 88 ℃, column bottom temperature are 45 ℃, completes solvent treatment.Other step is identical with embodiment 1.
Embodiment 3
In the present embodiment, step (1) is mixed coal tar to send in hydrogenator with hydrogen, carry out hydrotreatment take under molybdenum-nickel type Hydrobon catalyst that aluminium sesquioxide is carrier and the katalysis with the ZSM-5 zeolite catalytic dewaxing catalyst of nickel-loaded successively, temperature of reaction is 360 ℃, pressure is 12MPa, hydrogen to oil volume ratio is 1200:1, with respect to the liquid volume air speed of Hydrobon catalyst, is 0.45h
-1, with respect to the liquid volume air speed of catalytic dewaxing catalyst, be 0.85h
-1, obtain hydrogenated oil.The present embodiment is used, and to take the molybdenum-nickel type Hydrobon catalyst that aluminium sesquioxide is carrier be the FZC-41A type catalyzer (http://www.gqcat.com.cn/Chinese/ProductList.asp PID=25) that adopts Shandong Gong Quan chemical inc to produce, ZSM-5 zeolite catalytic dewaxing catalyst with nickel-loaded is the MLDW-3 type catalyzer (http://www.exxonmobil.com/Apps/RefiningTechnologies/files/sells heet_mldw.pdf) that adopts EXXON MOBIL company, step (3) is conducted heat and is extracted transformer oil cut countercurrent mass transfer in extraction tower with N-first class pyrrolidone, transformer oil after extraction enters in solvent recovery unit and carries out underpressure distillation and remove remaining N-first class pyrrolidone, the volume ratio of transformer oil cut and N-first class pyrrolidone is 1:1.8, the extraction tower tower top temperature is 85 ℃, column bottom temperature is 40 ℃, complete solvent treatment.Other step is identical with embodiment 1.
Embodiment 4
In the present embodiment, step (1) is mixed coal tar to send in hydrogenator with hydrogen, carry out hydrotreatment take under molybdenum-nickel type Hydrobon catalyst that aluminium sesquioxide is carrier and the katalysis with the ZSM-5 zeolite catalytic dewaxing catalyst of nickel-loaded successively, temperature of reaction is 300 ℃, pressure is 10MPa, hydrogen to oil volume ratio is 800:1, with respect to the liquid volume air speed of Hydrobon catalyst, is 0.3h
-1, with respect to the liquid volume air speed of catalytic dewaxing catalyst, be 0.6h
-1, obtain hydrogenated oil.Step (3) is conducted heat and is extracted transformer oil cut countercurrent mass transfer in extraction tower with N-first class pyrrolidone, transformer oil after extraction enters in solvent recovery unit and carries out underpressure distillation and remove remaining N-first class pyrrolidone, the volume ratio of transformer oil cut and N-first class pyrrolidone is 1:1, the extraction tower tower top temperature is that 80 ℃, column bottom temperature are 40 ℃, completes solvent treatment.Step (4), under nitrogen protection, is mixed the transformer oil cut after solvent treatment and carclazyte, and the carclazyte add-on is 7% of transformer oil cut quality after solvent treatment, stir, and 130 ℃ of reaction 50min, cooling, filter, obtain transformer oil base oil.Other step is identical with embodiment 1.
Embodiment 5
In the present embodiment, step (1) is mixed coal tar to send in hydrogenator with hydrogen, carry out hydrotreatment take under molybdenum-nickel type Hydrobon catalyst that aluminium sesquioxide is carrier and the katalysis with the ZSM-5 zeolite catalytic dewaxing catalyst of nickel-loaded successively, temperature of reaction is 400 ℃, pressure is 15MPa, hydrogen to oil volume ratio is 1500:1, with respect to the liquid volume air speed of Hydrobon catalyst, is 0.6h
-1, with respect to the liquid volume air speed of catalytic dewaxing catalyst, be 1.0h
-1, obtain hydrogenated oil.Step (3) is conducted heat and is extracted transformer oil cut countercurrent mass transfer in extraction tower with N-first class pyrrolidone, transformer oil after extraction enters in solvent recovery unit and carries out underpressure distillation and remove remaining N-first class pyrrolidone, the volume ratio of transformer oil cut and N-first class pyrrolidone is 1:2, the extraction tower tower top temperature is that 90 ℃, column bottom temperature are 50 ℃, completes solvent treatment.Step (4), under nitrogen protection, is mixed the transformer oil cut after solvent treatment and carclazyte, and the carclazyte add-on is 10% of transformer oil cut quality after solvent treatment, stir, and 150 ℃ of reaction 40min, cooling, filter, obtain transformer oil base oil.Other step is identical with embodiment 1.
Embodiment 6
In above-described embodiment 1～5, step (3) selective solvent N-used first class pyrrolidone is replaced with furfural or the phenol of equivalent, and other step is identical with corresponding embodiment.
Embodiment 7
In above-described embodiment 1～6, the raw materials used coalite tar of step (1) is replaced with the coal-tar middle oil of equivalent, with 700～900 ℃ of coal-tar middle oils that produce in the coal pyrolysis process, is raw material production cycloalkyl transformer oil base oil.Other step is identical with corresponding embodiment.
In order to verify the effect of having a mind to of the present invention, the contriver is through a large amount of test and research, now take following Comparative Examples and describes as example:
(1) change hydrogenation conditions
Hydrobon catalyst and catalytic dewaxing catalyst are identical with embodiment 1, the reaction conditions of the hydrotreatment in this Comparative Examples is as follows: temperature of reaction is 420 ℃, reaction pressure is 16MPa, and hydrogen to oil volume ratio is 1800:1, with respect to the liquid volume air speed of Hydrobon catalyst, is 0.4h
-1, with respect to the liquid volume air speed of catalytic dewaxing catalyst, be 0.8h
-1.The liquid product under these processing condition, coal tar hydrogenating obtained enters separation column and carries out fractionation, and after fractionation, the yield of each component is in Table 5.
The yield of the various products that 1 hydrotreatment of table 5 Comparative Examples obtains
Annotate: with feed coal tar 100%, calculate.
From table 5 and table 1 contrast, along with the severity increase of hydroconversion condition, the hydrogenation reaction degree of depth increases, the yield of light ends oil significantly increases, but the yield of transformer distillate significantly reduces, and is unfavorable for preparing transformer oil base oil.
(2) change the hydrogenation reaction air speed
Hydrobon catalyst and catalytic dewaxing catalyst are identical with embodiment 1, the reaction conditions of the hydrotreatment of this Comparative Examples is as follows: temperature of reaction is 350 ℃, reaction pressure is 14MPa, and hydrogen to oil volume ratio is 800:1, with respect to the liquid volume air speed of Hydrobon catalyst, is 0.8h
-1, with respect to the liquid volume air speed of catalytic dewaxing catalyst, be 1.2h
-1.The liquid product under these processing condition, coal tar hydrogenating obtained enters separation column and carries out fractionation, after fractionation, the yield of each component is in Table 6, adopt the processing method of embodiment 1 to carry out solvent treatment and clay-filtered the transformer distillate obtained, obtain transformer oil base oil, character is in Table 7.
The yield of the various products that 2 hydrotreatments of table 6 Comparative Examples obtain
From the contrast of table 6 and table 1, along with the increase of the reaction velocity of hydroconversion condition, the yield of all light ends oil all decreases, and the residual oil ratio significantly increases, and illustrates that the hydrogenation degree of depth is inadequate, is unfavorable for preparing light-weight fuel oil and transformer oil base oil.
Table 7 Comparative Examples 2 obtains the transformer foundation oil properties
As shown in Table 7, resulting transformer foundation oil many index can not reach the regulation of GB GB2536-1990.
Claims (7)
1. the method for a coal tar production cycloalkyl transformer oil base oil is characterized in that being comprised of following steps:
(1) coal tar hydrogenating is processed
Coal tar is mixed with hydrogen, carry out hydrotreatment under the katalysis of Hydrobon catalyst and catalytic dewaxing catalyst in hydrogenator, temperature of reaction is 300～400 ℃, pressure is 10～15MPa, hydrogen to oil volume ratio is 800～1500:1, with respect to the liquid volume air speed of Hydrobon catalyst, is 0.3～0.6h
-1, with respect to the liquid volume air speed of catalytic dewaxing catalyst, be 0.6～1.0h
-1, obtain hydrogenated oil;
(2) fractionation of hydrogenation products
Hydrogenated oil is sent into to fractionation in separation column, obtain being less than 180 ℃ naphtha fraction, 180～300 ℃ diesel oil distillate, 300～360 ℃ the transformer oil cut and be greater than the residue fraction of 360 ℃;
(3) solvent treatment of transformer distillate
With selective solvent, transformer oil cut countercurrent mass transfer in extraction tower is conducted heat and extracts, transformer oil after extraction carries out underpressure distillation and removes residual solvent in solvent recovery unit, the volume ratio of transformer oil cut and selective solvent is 1:1～2, the extraction tower tower top temperature is that 80～90 ℃, column bottom temperature are 40～50 ℃, completes solvent treatment;
Above-mentioned selectivity volume is phenol or N-first class pyrrolidone or furfural;
(4) the transformer distillate is clay-filtered
Under nitrogen protection, the transformer oil cut after solvent treatment to be mixed with carclazyte, the carclazyte add-on is 7～10% of transformer oil cut quality after solvent treatment, stirs, 130～150 ℃ of reaction 40～50min, cooling, filter, obtain transformer oil base oil.
2. the method for coal tar production cycloalkyl transformer oil base oil according to claim 1, it is characterized in that: described Hydrobon catalyst is to take the molybdenum-nickel type catalyzer that aluminium sesquioxide is carrier, in its catalytically-active metals, molybdic oxide content is at least 21wt%, nickel oxide content is at least 6wt%, total pore volume is at least 0.3mL/g, and specific surface area is at least 150m
2/ g;
The ZSM-5 zeolite catalytic dewaxing catalyst that described catalytic dewaxing catalyst is nickel-loaded, in catalytically-active metals, nickel oxide content is 1～3wt%, and total pore volume is at least 0.1mL/g, and specific surface area is at least 200m
2/ g.
3. the method for coal tar production cycloalkyl transformer oil base oil according to claim 1, it is characterized in that: described step (1) is mixed coal tar with hydrogen, carry out hydrotreatment under the katalysis of Hydrobon catalyst and catalytic dewaxing catalyst in hydrogenator, temperature of reaction is 350～380 ℃, pressure is 12～14MPa, hydrogen to oil volume ratio is 900～1200:1, with respect to the liquid volume air speed of Hydrobon catalyst, is 0.4～0.5h
-1, with respect to the liquid volume air speed of catalytic dewaxing catalyst, be 0.8～0.9h
-1, obtain hydrogenated oil.
4. the method for coal tar production cycloalkyl transformer oil base oil according to claim 1, it is characterized in that: described step (1) is mixed coal tar with hydrogen, carry out hydrotreatment under the katalysis of Hydrobon catalyst and catalytic dewaxing catalyst in hydrogenator, temperature of reaction is 380 ℃, pressure is 14MPa, hydrogen to oil volume ratio is 1000:1, with respect to the liquid volume air speed of Hydrobon catalyst, is 0.4h
-1, with respect to the liquid volume air speed of catalytic dewaxing catalyst, be 0.8h
-1, obtain hydrogenated oil.
5. the method for coal tar production cycloalkyl transformer oil base oil according to claim 1, it is characterized in that: described step (3) in solvent recovery unit is carried out underpressure distillation after countercurrent mass transfer heat transfer extraction to the transformer oil cut with selective solvent and is removed residual solvent in extraction tower, the volume ratio of transformer oil cut and selective solvent is 1:1.2～1.8, the extraction tower tower top temperature is that 85～90 ℃, column bottom temperature are 45 ℃, completes solvent treatment.
6. the method for coal tar production cycloalkyl transformer oil base oil according to claim 1, it is characterized in that: described step (3) in solvent recovery unit is carried out underpressure distillation after countercurrent mass transfer heat transfer extraction to the transformer oil cut with selective solvent and is removed residual solvent in extraction tower, the volume ratio of transformer oil cut and selective solvent is 1:1.2, the extraction tower tower top temperature is that 90 ℃, column bottom temperature are 45 ℃, completes solvent treatment.
7. the method for coal tar production cycloalkyl transformer oil base oil according to claim 1; it is characterized in that: described step (4) is under nitrogen protection; transformer oil cut after solvent treatment and carclazyte are mixed; the carclazyte add-on is 8% of transformer oil cut quality after solvent treatment; stir, 140 ℃ of reaction 40min, cooling; filter, obtain transformer oil base oil.
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| CN106433777A (en) * | 2016-08-25 | 2017-02-22 | 王树宽 | Method for preparing monomer naphthenic hydrocarbon and megilp by using coal cornerstone cerebral |
| CN107903945A (en) * | 2017-11-23 | 2018-04-13 | 海南汉地阳光石油化工有限公司 | A kind of fractionating system for producing lube base oil |
| CN108977224A (en) * | 2018-08-01 | 2018-12-11 | 国家能源投资集团有限责任公司 | Transformer oil base oil and preparation method thereof |
| CN111534317A (en) * | 2020-04-10 | 2020-08-14 | 圣德光科技发展(北京)有限公司 | Preparation method of refined asphalt |
| CN112280612A (en) * | 2020-11-08 | 2021-01-29 | 盘锦北方沥青股份有限公司 | High-performance transformer oil and preparation method thereof |
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| CN106433777A (en) * | 2016-08-25 | 2017-02-22 | 王树宽 | Method for preparing monomer naphthenic hydrocarbon and megilp by using coal cornerstone cerebral |
| CN106433777B (en) * | 2016-08-25 | 2017-12-26 | 王树宽 | A kind of method that coal based naphtha prepares monomer cycloalkane and solvent naphtha |
| CN107903945A (en) * | 2017-11-23 | 2018-04-13 | 海南汉地阳光石油化工有限公司 | A kind of fractionating system for producing lube base oil |
| CN108977224A (en) * | 2018-08-01 | 2018-12-11 | 国家能源投资集团有限责任公司 | Transformer oil base oil and preparation method thereof |
| CN111534317A (en) * | 2020-04-10 | 2020-08-14 | 圣德光科技发展(北京)有限公司 | Preparation method of refined asphalt |
| CN111534317B (en) * | 2020-04-10 | 2021-09-03 | 圣德光科技发展(北京)有限公司 | Preparation method of refined asphalt |
| CN112280612A (en) * | 2020-11-08 | 2021-01-29 | 盘锦北方沥青股份有限公司 | High-performance transformer oil and preparation method thereof |
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| CN103436289B (en) | 2015-06-17 |
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Effective date of registration: 20200422 Address after: 719319 Jinyuan South Road, Jinjie Industrial Park, Shenmu City, Yulin City, Shaanxi Province Patentee after: SHENMUFUYOU ENERGY TECHNOLOGY Co.,Ltd. Address before: 719319 Shenmu oil rich energy technology Co., Ltd., Shenmu Industrial Zone, Shenmu, Shaanxi, Yulin Patentee before: Wang Shukuan |
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