CN104611006A - Equipment and method for improving gassing resistance of transformer oil - Google Patents
Equipment and method for improving gassing resistance of transformer oil Download PDFInfo
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- CN104611006A CN104611006A CN201510024719.3A CN201510024719A CN104611006A CN 104611006 A CN104611006 A CN 104611006A CN 201510024719 A CN201510024719 A CN 201510024719A CN 104611006 A CN104611006 A CN 104611006A
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- raffinate
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- 238000000034 method Methods 0.000 title claims abstract description 50
- 239000000284 extract Substances 0.000 claims abstract description 212
- 238000000605 extraction Methods 0.000 claims abstract description 142
- 239000002904 solvent Substances 0.000 claims abstract description 135
- 238000007670 refining Methods 0.000 claims abstract description 101
- 238000001704 evaporation Methods 0.000 claims description 54
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical group O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 claims description 54
- 230000008020 evaporation Effects 0.000 claims description 41
- 235000011194 food seasoning agent Nutrition 0.000 claims description 28
- 125000000753 cycloalkyl group Chemical group 0.000 claims description 21
- 238000005984 hydrogenation reaction Methods 0.000 claims description 19
- 238000001035 drying Methods 0.000 claims description 10
- 238000002156 mixing Methods 0.000 claims description 9
- 238000004807 desolvation Methods 0.000 claims description 8
- 239000011259 mixed solution Substances 0.000 claims description 7
- 239000003610 charcoal Substances 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 238000005373 pervaporation Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 abstract description 7
- 239000003921 oil Substances 0.000 description 342
- 239000002994 raw material Substances 0.000 description 17
- 238000004519 manufacturing process Methods 0.000 description 12
- 230000003078 antioxidant effect Effects 0.000 description 11
- 238000007872 degassing Methods 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 10
- 239000000047 product Substances 0.000 description 10
- 239000007791 liquid phase Substances 0.000 description 9
- 238000000638 solvent extraction Methods 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 229930195733 hydrocarbon Natural products 0.000 description 8
- 150000002430 hydrocarbons Chemical class 0.000 description 8
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 8
- 238000000746 purification Methods 0.000 description 8
- 239000004215 Carbon black (E152) Substances 0.000 description 6
- 239000003963 antioxidant agent Substances 0.000 description 6
- 239000003348 petrochemical agent Substances 0.000 description 6
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 4
- 239000002199 base oil Substances 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000010779 crude oil Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000012188 paraffin wax Substances 0.000 description 3
- 150000004996 alkyl benzenes Chemical class 0.000 description 2
- 125000003118 aryl group Chemical group 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 230000005685 electric field effect Effects 0.000 description 2
- 238000009413 insulation Methods 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 1
- 241001494479 Pecora Species 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000004020 conductor Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003989 dielectric material Substances 0.000 description 1
- 230000005684 electric field Effects 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
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
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/12—Electrical isolation oil
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)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses equipment and a method for improving the gassing resistance of transformer oil, wherein the equipment comprises an extraction tower, an extracted oil refining tank, a raffinate stripping tower and a transformer oil tank, wherein the extraction tower comprises a raw oil inlet, a solvent inlet, a primary extracted liquid outlet and a raffinate outlet; the extracted oil refining tank comprises a primary extract inlet connected with the primary extract inlet; the raffinate stripping tower comprises a refined oil outlet connected with a raffinate outlet of a raffinate inlet and a refined oil outlet connected with a transformer oil tank, an extract oil raffinate pipeline is arranged between the extract oil refining tank and the extraction tower and comprises an extract oil raffinate outlet and an extract oil raffinate inlet which are arranged at the top of the extract oil refining tank, and the extract oil raffinate inlet is arranged on the extraction tower and is positioned at the position of a raw oil inlet or below the raw oil inlet. The invention can improve the gassing property of the naphthenic transformer oil and achieve the purpose of improving the quality of the transformer oil or producing the ultrahigh voltage transformer oil.
Description
Technical field
The invention belongs to technical field of petrochemical industry, relate in particular to a kind of apparatus and method for improving transformer oil anti-gassing performance.
Background technology
Along with the development of electric utility and the raising of power transmission and transforming equipment voltage range, constantly increase the demand of transformer oil, specification of quality also improves constantly simultaneously.Transformer oil plays a clasp Y insulation Y dielectric material of the effects such as insulation, cooling and arc extinguishing in the electrical apparatus.Transformer oil is the liquid dielectric thermally conductive material that electric utility uses, and its performance is relevant with contained hydrocarbon composition.Such as, straight-chain paraffin pour point is high, and low-temperature fluidity is poor, anti-gassing property is poor, is the undesirable components in transformer oil, and the anti-gassing property of aromatic hydrocarbons is good, but the anti-oxidative stability of polycyclic aromatic hydrocarbons is poor; Anti-gassing property can be the important indicator of transformer oil particularly ultrahigh voltage transformer oil, hydro carbons anti-gassing property can by weak order being by force, aromatic hydrocarbons > naphthenic hydrocarbon > isoparaffin > straight-chain paraffin, therefore the hydrocarbon composition that transformer oil is desirable is: relatively large naphthenic hydrocarbon, appropriate few Polycyclic aromatic hydrocarbons (in ultrahigh voltage transformer oil, content is slightly high), a small amount of isoparaffin, hardly containing straight-chain paraffin.
Naphthenic base crude is the preferred raw materials of the production transformer oil of generally acknowledging in the world, and domestic and international high-quality transformer oil mostly uses naphthenic base crude to produce.Its reason is mainly because paraffinic hydrocarbons, naphthenic hydrocarbon and aromatic hydrocarbon in naphthenic base crude have relatively reasonable ratio.It needs to carry out degree of depth dewaxing unlike paraffinic based oil, also a large amount of polynuclear aromaticss to be removed unlike Heavy aromatic base crude oil, and cycloalkyl crude oil of low-coagulation wax content is very low, generally all below 3%, can without the dewaxing just good transformer oil of energy production low-temperature performance.But naphthenic base crude is also the resource of a kind of rareness in the world, about 2.2% of Jin Zhan world crude oil reserves, only have Venezuela, the U.S., Canada and a few countries such as Chinese to have naphthenic base crude resource at present in the world.The naphthenic base crude of China is also comparatively rare.Along with the develop rapidly of hydrogen addition technology, utilize isomerization dewaxing hydrogen addition technology both at home and abroad at present, be that the output of the transformer oil of raw material production constantly increases with paraffinic base, although it is low that this kind of transformer has pour point, low temperature viscosity is little, the advantages such as anti-oxidative stability is good, but because its naphthene content is low, almost aromatic free, isoparaffin content is high, cause the anti-gassing property extreme difference of this kind of transformer oil, therefore generally the way concocted of good component transformer oil can be produced with this kind of transformer oil and the anti-gassing property such as cycloalkyl transformer oil or alkylbenzene, if produce ultrahigh voltage transformer oil, just need to add more alkylbenzene or anti-gassing property component, the transformer oil base oil that cycloalkyl anti-gassing property is good is just seemed precious especially, is therefore badly in need of the method that exploitation improves cycloalkyl transformer oil anti-gassing.
In the prior art, with the appropriate fractions of naphthenic base crude for transformer oil produced by stock oil.Such as, hydrofining-furfural treatment-clay-filtered explained hereafter 45 is adopted
#(Li Huixin etc. utilize the wooden low-sulfur naphthenic base crude of huge port sheep three to produce 45 to transformer oil
#transformer oil, lubricating oil, the 18th volume the 4th phase, 2003,60 to 62), but this method can not be prepared qualified ultrahigh voltage transformer oil or improve the degassing property of transformer oil further.
The patent No. be 201110056086.6 Chinese invention patent disclose a kind of method improving transformer oil anti-gassing performance and the equipment producing transformer oil, but the method limits by stock oil, the method do not illustrate how produce anti-gassing property for raw material by solvent treatment with naphthenic base crude transformer oil cut fraction hydrogenation depickling oil can good transformer oil base oil or ultrahigh voltage transformer oil.
The object of the invention is with naphthenic base crude transformer oil cut fraction hydrogenation depickling oil for raw material comes the direct production anti-gassing property good transformer oil of energy or ultrahigh voltage transformer oil by solvent treatment, post-refining etc.
Summary of the invention
For overcoming the shortcoming of prior art, the invention provides a kind of Apparatus and method for improving transformer oil anti-gassing performance.By the present invention, without the need to adopting harsh hydrogenation technique, the ultrahigh voltage transformer oil or better than the anti-gassing property of the transformer oil of usual vehicle process for purification production of SH0040-91 technical requirements just can be met.
For achieving the above object, the invention provides a kind of equipment improving transformer oil anti-gassing performance, comprise extraction tower, extract oil refining tank, raffinate stripping tower and transformer oil tank out, described extraction tower comprises the stock oil entrance being arranged at its underpart, the colvent inlet being arranged at its top, the raffinate outlet that is arranged at an Extract outlet bottom it, is arranged at its top; Described extraction oil refining tank comprises an Extract entrance in portion disposed therein, and described Extract outlet is connected with a described Extract entrance; Described raffinate stripping tower comprises the raffinate entrance being arranged at its underpart and the treated oil outlet be arranged at bottom it, and described raffinate outlet is connected with described raffinate entrance; Described transformer oil tank exports with described treated oil and is connected, wherein, there is between described extraction oil refining tank and described extraction tower an extraction oil raffinate pipeline, described extraction oily raffinate pipeline comprises to be extracted the outlet of oily raffinate out and extracts oily raffinate entrance out, the outlet of described extraction oily raffinate is arranged at the top of described extraction oil refining tank, and described extraction oil raffinate entrance to be arranged on described extraction tower and to be positioned at the position of below the position at described stock oil entrance place or described stock oil entrance.
The equipment of above-mentioned raising transformer oil anti-gassing performance, wherein, is also connected with post-refining unit in turn between described treated oil outlet and described transformer oil tank and concocts unit.
The equipment of above-mentioned raising transformer oil anti-gassing performance, wherein, also comprise solvent seasoning tower, wet solvent entrance and solvent outlet after being arranged at bottom it drying after described solvent seasoning tower comprises the stripping being arranged at its top, described raffinate stripping tower also comprises the first wet solvent outlet being arranged at its top, described first wet solvent outlet is connected with wet solvent entrance after described stripping, and after described drying, solvent outlet is connected with described colvent inlet.
The equipment of above-mentioned raising transformer oil anti-gassing performance, wherein, also comprise secondary Extract evaporator tower, described secondary Extract evaporator tower comprises the secondary Extract entrance being arranged at its underpart, solvent outlet and secondary Extract outlet after being arranged at bottom it evaporation after being arranged at the evaporation at its top, described solvent seasoning tower comprises colvent inlet after the evaporation in portion disposed therein, described extraction oil refining tank also comprises the secondary Extract outlet be arranged at bottom it, described secondary Extract outlet is connected with described secondary Extract entrance, after described evaporation, the outlet of secondary Extract is connected with a described Extract entrance, after described evaporation, solvent outlet is connected with colvent inlet after described evaporation.
The equipment of above-mentioned raising transformer oil anti-gassing performance, wherein, also comprise secondary extract stripper and secondary extraction oil tank, after described secondary extract stripper comprises the evaporation being arranged at its underpart, secondary Extract entrance and the secondary be arranged at bottom it extract oil export out, after described evaporation, the outlet of secondary Extract is connected with secondary Extract entrance after described evaporation, and described secondary extraction oil export is extracted oil tank out with described secondary and is connected.
The equipment of above-mentioned raising transformer oil anti-gassing performance, wherein, described secondary extract stripper also comprises the second wet solvent outlet being arranged at its top, and described second wet solvent outlet is connected with wet solvent entrance after described stripping.
The equipment of above-mentioned raising transformer oil anti-gassing performance, wherein, described secondary is extracted oil export out and is connected with a described Extract entrance.
The present invention also provides a kind of method improving transformer oil anti-gassing performance, wherein, adopts the equipment of above-mentioned raising transformer oil anti-gassing performance to refine, comprises the steps:
Solvent enters described extraction tower from the top of described extraction tower, stock oil enters described extraction tower from the bottom of described extraction tower and carries out extracting, the Extract that extracting obtains enters described extraction oil refining tank and refines, the refining extraction oil raffinate obtained is back to described extraction tower by described extraction oily raffinate pipeline, the raffinate that in described extraction tower, extracting obtains enters described raffinate stripping tower, and the treated oil that raffinate obtains after carrying out stripping desolvation enters described transformer oil tank.
The method of above-mentioned raising transformer oil anti-gassing performance, wherein, treated oil obtains transformer oil after post-refining and blending, and transformer oil enters described transformer oil tank.
The method of above-mentioned raising transformer oil anti-gassing performance, wherein, the wet solvent that described raffinate stripping tower stripping goes out enters described solvent seasoning tower through condensation and carries out drying, and the dried described solvent of described solvent seasoning tower bottom enters described extraction tower and recycles.
The method of above-mentioned raising transformer oil anti-gassing performance, wherein, in described extraction oil refining tank, the refining secondary Extract obtained obtains the secondary Extract containing a small amount of solvent after pervaporation, and the secondary Extract containing a small amount of solvent obtains secondary and extracts oil out after stripping.
The method of above-mentioned raising transformer oil anti-gassing performance, wherein, part secondary extracts oil out or part mixes with the Extract that described extraction tower extracting obtains through the secondary Extract of evaporation containing a small amount of solvent, enters described extraction oil refining tank and refines.
The method of above-mentioned raising transformer oil anti-gassing performance, wherein, the solvent removed during the evaporation of secondary Extract and the wet solvent removed when evaporation contains the secondary Extract stripping of a small amount of solvent enter described solvent seasoning tower respectively and carry out drying.
The method of above-mentioned raising transformer oil anti-gassing performance, wherein, the operational condition of described extraction oil refining tank is: secondary extracts oil out or the mass ratio of the amount that mixes with Extract through the secondary Extract of evaporation containing a small amount of solvent and stock oil is 0.1-1.0:1, the temperature of extracting oil refining tank out is 30 DEG C-40 DEG C, and the residence time that Extract stays in described extraction oil refining tank is 50-100 minutes; The residence time that the mixed solution that part secondary extraction oil or part obtain after the secondary Extract of evaporation containing a small amount of solvent mixes with an Extract stays in described extraction oil refining tank is 50-100 minutes.
The method of above-mentioned raising transformer oil anti-gassing performance, wherein, described stock oil is cycloalkyl transformer oil cut fraction hydrogenation depickling oil, and described solvent is furfural.
The method of above-mentioned raising transformer oil anti-gassing performance, wherein, described cycloalkyl transformer oil cut fraction hydrogenation depickling oil fraction scope is 280 DEG C-360 DEG C, close flash point ≮ 135 DEG C, fragrant charcoal (C
a) content ≮ 10%.
The method of above-mentioned raising transformer oil anti-gassing performance, wherein, described furfural extraction condition is, described extraction tower tower top temperature 60 DEG C-80 DEG C, described extraction tower column bottom temperature is 30 DEG C-50 DEG C, and the mass ratio of described furfural and described cycloalkyl transformer oil cut fraction hydrogenation depickling oil is 1.5-2.5:1.
The present invention can improve the degassing property of cycloalkyl transformer oil, reaches the object improved transformer oil quality or produce ultrahigh voltage transformer oil.
Describe the present invention below in conjunction with the drawings and specific embodiments, but not as a limitation of the invention.
Accompanying drawing explanation
Fig. 1 is the structure diagram of the equipment of raising transformer oil anti-gassing performance of the present invention;
Fig. 2 is the process flow sheet of the method for raising transformer oil anti-gassing performance of the present invention.
Wherein, Reference numeral
100 extraction towers
110 stock oil entrances
120 colvent inlets
130 Extract outlets
140 raffinate outlets
200 extract oil refining tank out
210 Extract entrances
220 2 Extract outlets
300 raffinate stripping towers
310 raffinate entrances
320 treated oil outlets
330 first wet solvent outlets
400 transformer oil tanks
500 extract oily raffinate pipeline out
510 extract the outlet of oily raffinate out
520 extract oily raffinate entrance out
600 solvent seasoning towers
Wet solvent entrance after 610 strippings
620 dry rear solvent outlet
Colvent inlet after 630 evaporations
700 2 Extract evaporator towers
710 2 Extract entrances
Solvent outlet after 720 evaporations
Secondary Extract outlet after 730 evaporations
800 2 extract strippers
Secondary Extract entrance after 810 evaporations
Extract oil export out 820 2 times
830 second wet solvent outlets
Extract oil tank out 900 2 times
1000 post-refining unit
1100 blending unit
4 raffinates
5 Extracts
7 extract oily raffinate out
8 two Extracts
10 solvents removed
11,12,13 containing the secondary Extract of a small amount of solvent
14, oil is extracted out 16,17 2 times
15, the wet solvent that goes out of 18 strippings
20 treated oils
23 transformer oil
Embodiment
Below in conjunction with the drawings and specific embodiments, technical solution of the present invention is described in detail, further to understand object of the present invention, scheme and effect, but not as the restriction of claims protection domain of the present invention.
The method of raising transformer oil anti-gassing performance of the present invention is: with cycloalkyl transformer oil cut fraction hydrogenation depickling oil for stock oil, in counter-current extraction tower, take furfural as solvent, solvent enters extraction tower from the top of extraction tower, stock oil enters extraction tower from the bottom of extraction tower, the raffinate extracting oil out enters extraction tower from the stock oil entrance of extraction tower or stock oil entrance bottom, an Extract is flowed out bottom extraction tower, the raffinate that extraction tower top is flowed out enters raffinate stripping tower, treated oil is obtained after desolvation, again through post-refining, blending obtains the transformer oil that ultrahigh voltage transformer oil or anti-gassing property can be good.
An Extract and secondary are extracted oil out or are extracted secondary Extract that oil refining pot bottom flows out and be mixed into and extract oil refining tank through evaporating the secondary Extract containing a small amount of solvent out and refine, extract oil refining tank top out and flow out the oily raffinate of extraction, extract oil refining pot bottom out and flow out secondary Extract, secondary Extract enters secondary Extract evaporator tower, the secondary Extract containing a small amount of solvent is flowed out bottom secondary Extract evaporator tower, when adopting the secondary Extract containing a small amount of solvent to mix with an Extract, this secondary Extract is divided into two portions, the Extract that a part goes out with extraction tower underflow is mixed into be extracted oil refining tank out and refines further, another part enters secondary extract stripper, obtain secondary after desolvation and extract oil out, when adopting secondary extraction oil to mix with an Extract, bottom secondary Extract evaporator tower, the secondary Extract flowed out containing a small amount of solvent enters secondary extract stripper, obtain secondary after desolvation and extract oil out, part secondary is extracted oily being mixed into an Extract out and is extracted oil refining tank out, and remaining secondary is extracted oil out and entered products pot as byproduct.
Particularly, consult Fig. 1, the equipment of raising transformer oil anti-gassing performance of the present invention comprises extraction tower 100, extracts oil refining tank 200, raffinate stripping tower 300, transformer oil tank 400 out and extract oily raffinate pipeline 500 out.Extraction tower 100 comprises: be arranged at the stock oil entrance 110 of the bottom of extraction tower 100, be arranged at the colvent inlet 120 on extraction tower 100 top, be arranged at an Extract outlet 130 bottom extraction tower 100 and be arranged at the raffinate outlet 140 at extraction tower 100 top.Extract oil refining tank 200 out to comprise: be arranged at the Extract entrance 210 extracted out in the middle part of oil refining tank 200, wherein, an Extract outlet 130 on extraction tower 100 is connected with the Extract entrance 210 extracted out on oil refining tank 200.Raffinate stripping tower 300 comprises: the raffinate entrance 310 being arranged at raffinate stripping tower 300 bottom and the treated oil outlet 320 be arranged at bottom raffinate stripping tower 300, wherein, the raffinate outlet 140 on extraction tower 100 is connected with the raffinate entrance 310 on raffinate stripping tower 300; Transformer oil tank 400 and the treated oil on raffinate stripping tower 300 export 320 and are connected.Extract oily raffinate pipeline 500 out to be arranged between extraction oil refining tank 200 and extraction tower 100, the setting of extracting oily raffinate pipeline 500 out can improve the content of few Polycyclic aromatic hydrocarbons in treated oil, improves yield and the quality of product.
Extract oily raffinate pipeline 500 out comprise the oily raffinate outlet 510 of extraction and extract oily raffinate entrance 520 out, extract oily raffinate outlet 510 out and be arranged at the top of extracting oil refining tank 200 out, extract oily raffinate entrance 520 out to be arranged on extraction tower 100 and the position being positioned at stock oil entrance less than 110, comprise the position at stock oil entrance 110 place.
As shown in Figure 1, the equipment of raising transformer oil anti-gassing performance of the present invention also comprises solvent seasoning tower 600, secondary Extract evaporator tower 700, secondary extract stripper 800 and secondary and extracts oil tank 900 out, is also connected with post-refining unit 1000 in turn and concocts unit 1100 between treated oil outlet 320 and transformer oil tank 400.Post-refining unit 1000 is for carrying out post-refining to treated oil, and blending unit 1100 is for concocting treated oil.
Solvent seasoning tower 600 comprises: wet solvent entrance 610 and solvent outlet 620 after being arranged at bottom solvent seasoning tower 600 drying after being arranged at the stripping on solvent seasoning tower 600 top.Raffinate stripping tower 300 also comprises: the first wet solvent outlet 330 being arranged at raffinate stripping tower 300 top, the first wet solvent outlet 330 on raffinate stripping tower 300 is connected with wet solvent entrance 610 after the stripping on solvent seasoning tower 600, and after the drying on solvent seasoning tower 600, solvent outlet 620 is connected with the colvent inlet 120 on extraction tower 100.
Secondary Extract evaporator tower 700 comprises: the secondary Extract entrance 710 being arranged at secondary Extract evaporator tower 700 bottom, be arranged at secondary Extract evaporator tower 700 top evaporation after solvent outlet 720 and secondary Extract outlet 730 after being arranged at bottom secondary Extract evaporator tower 700 evaporation.Solvent seasoning tower 600 also comprises: be arranged at colvent inlet 630 after the evaporation in the middle part of solvent seasoning tower 600.Extract oil refining tank 200 out also to comprise: be arranged at the secondary Extract outlet 220 of extracting out bottom oil refining tank 200, the secondary Extract outlet 220 of extracting out on oil refining tank 200 is connected with the secondary Extract entrance 710 on secondary Extract evaporator tower 700, after evaporation on secondary Extract evaporator tower 700, secondary Extract outlet 730 is connected with the Extract entrance 210 extracted out on oil refining tank 200, and after the evaporation on secondary Extract evaporator tower 700, solvent outlet 720 is connected with colvent inlet 630 after the evaporation on solvent seasoning tower 600.
Secondary extract stripper 800 comprises: after being arranged at the evaporation of secondary extract stripper 800 bottom, secondary Extract entrance 810 and the secondary be arranged at bottom secondary extract stripper 800 extract oil export 820 out, after evaporation on secondary Extract evaporator tower 700, secondary Extract outlet 730 is connected with secondary Extract entrance 810 after the evaporation on secondary extract stripper 800, and the secondary extraction oil export 820 on secondary extract stripper 800 is extracted oil tank 900 out with secondary and is connected.
Secondary extract stripper 800 also comprises: the second wet solvent outlet 830 being arranged at secondary extract stripper 800 top, and the second wet solvent outlet 830 on secondary extract stripper 800 is connected with wet solvent entrance 610 after the stripping on solvent seasoning tower 600.
Secondary on secondary extract stripper 800 is extracted oil export 820 out and is connected with the Extract entrance 210 extracted out on oil refining tank 200.
The operation of the method for raising transformer oil anti-gassing performance of the present invention is as shown in Figure 2: stock oil adopts cycloalkyl transformer oil cut fraction hydrogenation depickling oil also to enter extraction tower 100 from the stock oil entrance 110 of extraction tower 100 bottom, solvent adopts furfural and enters extraction tower 100 from the colvent inlet 120 on extraction tower 100 top, stock oil in extraction tower 100 after solvent treatment, the Extract 5 flowed out bottom extraction tower 100, extract the secondary Extract 8 flowed out bottom oil refining tank 200 out and remove most of solvent through secondary Extract evaporator tower 700, the solvent 10 removed enters the middle part of solvent seasoning tower 600, the secondary Extract 11 containing a small amount of solvent flowed out bottom secondary Extract evaporator tower 700 is divided into two portions 12 and 13, the Extract 5 flowed out bottom the secondary Extract 12 of a part containing a small amount of solvent and extraction tower 100 is mixed into extracts oil refining tank 200 out, the extraction oil raffinate 7 that flows out of the top of extracting oil refining tank 200 out enters extraction tower 100 by extracting oily raffinate pipeline 500 out from the bottom of the stock oil entrance 100 of extraction tower 100 or stock oil entrance 110, the secondary Extract 13 containing a small amount of solvent flowed out bottom secondary Extract evaporator tower 700 enters secondary extract stripper 800, the wet solvent 15 that stripping goes out enters solvent seasoning tower 600 top through condensation removes moisture as top backflow, dry solvent bottom solvent seasoning tower 600 enters extraction tower 100 to recycle.The raffinate 4 at extraction tower 100 top enters raffinate stripping tower 300, the wet solvent 18 that stripping goes out enters solvent seasoning tower 600 top through condensation removes moisture as pushing up back to heat up in a steamer, dry solvent bottom solvent seasoning tower 600 recycles, treated oil 20 is flowed out bottom raffinate stripping tower 300, treated oil 20 enters post-refining unit 1000 and obtains transformer oil base oil, and transformer oil base oil enters blending unit 1100 and obtains transformer oil finished product 23; The secondary containing a small amount of solvent flowed out bottom secondary Extract evaporator tower 800 is extracted oil 14 out and is divided into two portions 16 and 17, part secondary is extracted oil 16 out and is entered secondary as byproduct and extract oil tank 900 out, and a part of secondary is extracted oil 17 out and once extracted oily 5 and be mixed into and extract oil refining tank 200 out.
This invention takes and secondary refining is carried out to extraction oil, the raffinate of the extraction oil obtained is returned the way of extraction tower, solvent extraction with routine is compared, be equivalent to anti-gassing property energy in extraction oil, few Polycyclic aromatic hydrocarbons of good security reclaims, simultaneously owing to extracting the special composition of oily raffinate out, it returns in extraction tower and makes the extracting of extraction tower inside create useful effect, few cyclic aromatics content that secondary is extracted out in oil is lower, polycyclic aromatic hydrocarbon content is higher, namely the anti-gassing property in raw material good component can obtain sufficient recovery (this component enters in treated oil mostly), adopt the method to compare with Conventional solvents is refining, under the condition ensureing transformer oil qualified, in transformer oil, the content of aromatic hydrocarbons is improved largely, and anti-gassing property can improve, namely adopt the efficiency the method increasing solvent extraction, be equivalent to the selectivity that improve solvent.
It is more high better that the present invention mainly meets aromaticity content in treated oil, but polycyclic aromatic hydrocarbon content and the foreign matter content such as sulphur, nitrogen more low better, otherwise the requirement of transformer oil anti-oxidative stability can not be met, therefore the position range that the oily raffinate of the extraction of the best of the present invention returns extraction tower is, the region of extraction tower feed(raw material)inlet and bottom, feed(raw material)inlet.
The opening for feed extracting oil refining tank 200 out can establish feed distributor, extracting out in oil refining tank 200 can be that component is not established in slack tank and inside, or inside increases by one to three layers of sieve plate for preventing back-mixing, extract oil refining tank 200 preferably sleeping tank out, it is 50-100 minutes that the volume extracting oil refining tank 200 out meets the mixed solution residence time wherein that an Extract and secondary extract oil out, time is separated not exclusively lower than extracting oily raffinate when 50 minutes out with Extract, time more than 100 minutes under identical purification condition, the yield of raffinate no longer increases, illustrate that extracting oily raffinate out is fully separated with Extract.
Described cycloalkyl transformer oil cut fraction hydrogenation depickling oil, cut scope is 280 DEG C-360 DEG C, close flash point ≮ 135 DEG C, fragrant charcoal (CA) content ≮ 10%; Furfural extraction condition is the tower top temperature 50 DEG C-80 DEG C of extraction tower 100, and column bottom temperature is 30 DEG C-45 DEG C, and solvent ratio is 1.5-2.5:1; The operational condition of extracting oil refining tank 200 out is: secondary mix with Extract is extracted oily or secondary Extract and contained the secondary Extract of a small amount of solvent and the mass ratio of stock oil is 0.1-1.0:1 through evaporating, and mixing temperature is 30 DEG C-40 DEG C; Above-mentioned post-refining can be clay-filtered or liquid phase denitrogenation-and clay-filtered; Blending mainly adds appropriate oxidation inhibitor etc.
Embodiment 1: with cycloalkyl atmosphere 3rd side cut hydrogenation deacidification oil (raw material 1) for stock oil, carry out solvent extraction sepn process, the purification condition of extraction tower 100 is: tower top temperature is 80 DEG C, and column bottom temperature is 45 DEG C, and the mass ratio of solvent furfural and stock oil is 2.5:1.The operational condition of extracting oil refining tank 200 out is: temperature is 30 DEG C, being mixed into Extract the secondary extracting oil refining tank 200 out, to extract oil out with the mass ratio of stock oil be 0.1:1, mixed solution is 50 minutes extracting the residence time in oil refining tank 200 out, the extraction oil raffinate that the top of extracting oil refining tank 200 out is flowed out enters extraction tower 100 from the stock oil entrance 110 of extraction tower 100, obtain treated oil after the raffinate 4 that extraction tower 100 top is flowed out enters raffinate stripping tower 300 desolvation, secondary Extract obtains secondary and extracts oil out after evaporating solvent.
Treated oil carries out clay-filtered, and clay-filtered condition is: the mass percent of carclazyte (production of Jinxi atlapulgite factory) add-on and treated oil is 8%, temperature of reaction is 140 DEG C, and the residence time is 60 minutes, obtains clay-filtered oil.Add in this clay-filtered oil with the mass percent of clay-filtered oil be 0.50% antioxidant (T501, Liaohe Oil Field general petrochemicals factory energetically Industrial Group Corporation produce), the degassing property obtaining transformer oil is+10.6 μ l/min.
Comparative example 1: with cycloalkyl atmosphere 3rd side cut hydrogenation deacidification oil (raw material 1) for stock oil, carry out solvent extraction sepn process, the purification condition of extraction tower is: tower top temperature is 80 DEG C, column bottom temperature is 45 DEG C, the mass ratio of solvent furfural and stock oil is 2.5:1, and the Extract at the bottom of tower obtains extracting oil out after evaporating solvent; The refined liquid that tower top obtains obtains furfural refining oil after evaporating solvent, this treated oil is through clay-filtered, clay-filtered condition is: the mass percent of carclazyte (production of Jinxi atlapulgite factory) add-on and furfural refining oil is 5%, temperature of reaction is 140 DEG C, the residence time is 60 minutes, obtains clay-filtered oil.Add in this clay-filtered oil with the mass percent of clay-filtered oil be 0.50% antioxidant (T501, Liaohe Oil Field general petrochemicals factory energetically Industrial Group Corporation produce), the degassing property obtaining transformer oil is+13.5 μ l/min.
Embodiment 2 with cycloalkyl normal two wires hydrogenation deacidification oil (raw material 2) for stock oil, carry out solvent extraction sepn process, the purification condition of extraction tower 100 is: tower top temperature is 70 DEG C, and column bottom temperature is 40 DEG C, and the mass ratio of solvent furfural and stock oil is 2.0:1.The operational condition of extracting oil refining tank 200 out is: temperature is 40 DEG C, being mixed into what extract oil refining tank 200 out with Extract is 1.0:1 through evaporating containing the secondary Extract of a small amount of solvent and the mass ratio of stock oil, mixed solution is 100 minutes extracting the residence time in oil refining tank 200 out, the extraction oil refining liquid that the top of extracting oil refining tank 200 out is flowed out enters extraction tower 100 from the entrance of stock oil entrance 110 bottom of extraction tower 100, treated oil is obtained after the raffinate 4 that extraction tower 100 top is flowed out enters raffinate stripping tower 300 desolvation, secondary Extract obtains secondary and extracts oil out after evaporating solvent.
Treated oil carries out liquid phase denitrogenation, clay-filtered, liquid phase denitrification process condition is: denitrfying agent (WSQ-2, Hubei Jin He Chemical Co., Ltd. produces) mass percent of add-on and furfural refining oil is 0.4%, temperature of reaction is 90 DEG C, clay-filtered condition is: the mass percent of carclazyte (production of Jinxi atlapulgite factory) add-on and furfural refining oil is 5%, temperature of reaction is 140 DEG C, the residence time is 60 minutes, obtains clay-filtered oil.Add in this clay-filtered oil relative to the mass percent of clay-filtered oil be 0.50% antioxidant (T501, Liaohe Oil Field general petrochemicals factory energetically Industrial Group Corporation produces), obtain common 45# transformer oil, wherein the degassing property of transformer oil is-1.5 μ l/min
Comparative example 2: with cycloalkyl normal two wires hydrogenation deacidification oil (raw material 2) for stock oil, carry out solvent extraction sepn process, the purification condition of extraction tower is: tower top temperature is 70 DEG C, column bottom temperature is 40 DEG C, the mass ratio of solvent furfural and stock oil is 2.0:1, and the Extract at the bottom of tower obtains extracting oil out after evaporating solvent; The refined liquid that tower top obtains obtains furfural refining oil after evaporating solvent, this treated oil is through liquid phase denitrogenation, clay-filtered, liquid phase denitrification process condition is: denitrfying agent (WSQ-2, Hubei Jin He Chemical Co., Ltd. produces) mass percent of add-on and furfural refining oil is 0.25%, temperature of reaction is 90 DEG C, clay-filtered condition is: the mass percent of carclazyte (production of Jinxi atlapulgite factory) add-on and furfural refining oil is 2%, temperature of reaction is 140 DEG C, the residence time is 60 minutes, obtains clay-filtered oil.Add in this clay-filtered oil relative to the mass percent of clay-filtered oil be 0.50% antioxidant (T501, Liaohe Oil Field general petrochemicals factory energetically Industrial Group Corporation produce), the degassing property obtaining transformer oil is+7.2 μ l/min.
Embodiment 3 with cycloalkyl normal two wires hydrogenation deacidification oil (raw material 2) for stock oil, carry out solvent extraction sepn process, the purification condition of extraction tower 100 is: tower top temperature is 60 DEG C, and column bottom temperature is 30 DEG C, and the mass ratio of solvent furfural and stock oil is 1.5:1.The operational condition of extracting oil refining tank 200 out is: temperature is 30 DEG C, being mixed into what extract oil refining tank 200 out with Extract is 0.5:1 through evaporating containing the secondary Extract of a small amount of solvent and the mass ratio of stock oil, mixed solution is 70 minutes extracting the residence time in oil refining tank 200 out, mixed solution is 90 minutes extracting the residence time in oil refining tank 200 out, the extraction oil refining liquid that the top of extracting oil refining tank 200 out is flowed out enters extraction tower 100 from the entrance of stock oil entrance 110 bottom of extraction tower 100, treated oil is obtained after the raffinate 4 that extraction tower 100 top is flowed out enters raffinate stripping tower 300 desolvation, secondary Extract obtains secondary and extracts oil out after evaporating solvent.
Treated oil carries out liquid phase denitrogenation, clay-filtered, liquid phase denitrification process condition is: denitrfying agent (WSQ-2, Hubei Jin He Chemical Co., Ltd. produces) mass percent of add-on and furfural refining oil is 0.5%, temperature of reaction is 90 DEG C, clay-filtered condition is: the mass percent of carclazyte (production of Jinxi atlapulgite factory) add-on and furfural refining oil is 5%, temperature of reaction is 140 DEG C, the residence time is 60 minutes, obtains clay-filtered oil.Add in this clay-filtered oil relative to the mass percent of clay-filtered oil be 0.50% antioxidant (T501, Liaohe Oil Field general petrochemicals factory energetically Industrial Group Corporation produces), be met the 45# ultrahigh voltage transformer oil of SH0040-91 quality index, wherein the anti-gassing property of transformer oil is+1.7 μ l/min.
Comparative example 3: with cycloalkyl normal two wires hydrogenation deacidification oil (raw material 2) for stock oil, carry out solvent extraction sepn process, the purification condition of extraction tower is: tower top temperature is 60 DEG C, column bottom temperature is 30 DEG C, the mass ratio of solvent furfural and stock oil is 1.5:1, and the Extract at the bottom of tower obtains extracting oil out after evaporating solvent; The refined liquid that tower top obtains obtains furfural refining oil after evaporating solvent, this treated oil is through liquid phase denitrogenation, clay-filtered, liquid phase denitrification process condition is: denitrfying agent (WSQ-2, Hubei Jin He Chemical Co., Ltd. produces) mass percent of add-on and furfural refining oil is 0.25%, temperature of reaction is 90 DEG C, clay-filtered condition is: the mass percent of carclazyte (production of Jinxi atlapulgite factory) add-on and furfural refining oil is 2%, temperature of reaction is 140 DEG C, the residence time is 60 minutes, obtains clay-filtered oil.Add in this clay-filtered oil relative to the mass percent of clay-filtered oil be 0.30% antioxidant (T501, Liaohe Oil Field general petrochemicals factory energetically Industrial Group Corporation produces), obtain 45# common transformer oil, its degassing property is+5.7 μ l/min by analysis.
Table 1 embodiment raw material oil properties
Table 2 embodiment 1 finished product oil properties (raw material 1)
Table 3 example 2 finished product oil properties (raw material 2)
Table 4 example 3 finished product oil properties (raw material 2)
Oil product is under the effect of high-voltage electric field, and the descending order of degassing property is: alkane, naphthenic hydrocarbon, aromatic hydrocarbon.Transformer oil, under high-voltage electric field effect, owing to sparking or marginal discharge, makes oil product generation dehydrogenation, produce hydrogen, the hydrogen deviate from can all or part ofly be absorbed by oil product again, and this trend absorbing under high-voltage electric field effect or release gas of oil product, is called degassing property.It is an important indicator of evaluation ultrahigh voltage transformer oil performance.The ultrahigh voltage transformer oil standard that current China measures is not more than+5uL/min to degassing property index clear stipulaties.
The good transformer oil of anti-gassing property energy is produced for the solvent-refined method of employing, it is more high better that treated oil will meet aromaticity content, few Polycyclic aromatic hydrocarbons is The more the better, but the foreign matter content such as sulphur, nitrogen and polycyclic aromatic hydrocarbon content are more low better, meet the requirements such as transformer oil anti-oxidative stability, when requiring more than meeting, the yield of treated oil is more high better, the yield extracting oil out is more low better, and the foreign matter content such as sulphur, nitrogen extracting oil out is more high better.Due to extract oily secondary refining out raffinate in aromaticity content relatively high, wherein containing many rings of some amount and the compound such as sulphur, nitrogen of high level, therefore this component returns the position difference of extraction tower, different impacts can be produced to the treated oil quality of solvent extraction, test-results shows: return the opening for feed or following that tower position is extraction tower, only in this way just can reach the transformer oil produced not only anti-gassing property well but also can meet the requirements such as anti-oxidative stability.
Method and apparatus of the present invention is applicable to the hydrogenation deacidification of transformer oil cut oil for stock oil, the transformer oil that production ultrahigh voltage transformer oil or anti-gassing can be good.The present invention, by improving the degassing property of cycloalkyl transformer oil, reaches the object improved transformer oil quality or produce ultrahigh voltage transformer oil, therefore has a extensive future.
Certainly; the present invention also can have other various embodiments; when not deviating from the present invention's spirit and essence thereof; those of ordinary skill in the art are when making various corresponding change and distortion according to the present invention, but these change accordingly and are out of shape the protection domain that all should belong to the claim appended by the present invention.
Claims (17)
1. one kind is improved the equipment of transformer oil anti-gassing performance, comprise extraction tower, extract oil refining tank, raffinate stripping tower and transformer oil tank out, described extraction tower comprises the stock oil entrance being arranged at its underpart, the colvent inlet being arranged at its top, the raffinate outlet that is arranged at an Extract outlet bottom it, is arranged at its top; Described extraction oil refining tank comprises an Extract entrance in portion disposed therein, and described Extract outlet is connected with a described Extract entrance; Described raffinate stripping tower comprises the raffinate entrance being arranged at its underpart and the treated oil outlet be arranged at bottom it, and described raffinate outlet is connected with described raffinate entrance; Described transformer oil tank exports with described treated oil and is connected, it is characterized in that, there is between described extraction oil refining tank and described extraction tower an extraction oil raffinate pipeline, described extraction oily raffinate pipeline comprises to be extracted the outlet of oily raffinate out and extracts oily raffinate entrance out, the outlet of described extraction oily raffinate is arranged at the top of described extraction oil refining tank, and described extraction oil raffinate entrance to be arranged on described extraction tower and to be positioned at the position of below the position at described stock oil entrance place or described stock oil entrance.
2. the equipment of raising transformer oil anti-gassing performance according to claim 1, is characterized in that, is also connected with post-refining unit in turn and concocts unit between described treated oil outlet and described transformer oil tank.
3. the equipment of raising transformer oil anti-gassing performance according to claim 1, it is characterized in that, also comprise solvent seasoning tower, wet solvent entrance and solvent outlet after being arranged at bottom it drying after described solvent seasoning tower comprises the stripping being arranged at its top, described raffinate stripping tower also comprises the first wet solvent outlet being arranged at its top, described first wet solvent outlet is connected with wet solvent entrance after described stripping, and after described drying, solvent outlet is connected with described colvent inlet.
4. the equipment of raising transformer oil anti-gassing performance according to claim 3, it is characterized in that, also comprise secondary Extract evaporator tower, described secondary Extract evaporator tower comprises the secondary Extract entrance being arranged at its underpart, solvent outlet and secondary Extract outlet after being arranged at bottom it evaporation after being arranged at the evaporation at its top, described solvent seasoning tower comprises colvent inlet after the evaporation in portion disposed therein, described extraction oil refining tank also comprises the secondary Extract outlet be arranged at bottom it, described secondary Extract outlet is connected with described secondary Extract entrance, after described evaporation, the outlet of secondary Extract is connected with a described Extract entrance, after described evaporation, solvent outlet is connected with colvent inlet after described evaporation.
5. the equipment of raising transformer oil anti-gassing performance according to claim 4, it is characterized in that, also comprise secondary extract stripper and secondary extraction oil tank, after described secondary extract stripper comprises the evaporation being arranged at its underpart, secondary Extract entrance and the secondary be arranged at bottom it extract oil export out, after described evaporation, the outlet of secondary Extract is connected with secondary Extract entrance after described evaporation, and described secondary extraction oil export is extracted oil tank out with described secondary and is connected.
6. the equipment of raising transformer oil anti-gassing performance according to claim 5, it is characterized in that, described secondary extract stripper also comprises the second wet solvent outlet being arranged at its top, and described second wet solvent outlet is connected with wet solvent entrance after described stripping.
7. the equipment of raising transformer oil anti-gassing performance according to claim 5, is characterized in that, described secondary is extracted oil export out and is connected with a described Extract entrance.
8. improve a method for transformer oil anti-gassing performance, it is characterized in that, adopt the equipment of raising transformer oil anti-gassing performance according to claim 1 to refine, comprise the steps:
Solvent enters described extraction tower from the top of described extraction tower, stock oil enters described extraction tower from the bottom of described extraction tower and carries out extracting, the Extract that extracting obtains enters described extraction oil refining tank and refines, the refining extraction oil raffinate obtained is back to described extraction tower by described extraction oily raffinate pipeline, the raffinate that in described extraction tower, extracting obtains enters described raffinate stripping tower, and the treated oil that raffinate obtains after carrying out stripping desolvation enters described transformer oil tank.
9. the method for raising transformer oil anti-gassing performance according to claim 8, is characterized in that, treated oil obtains transformer oil after post-refining and blending, and transformer oil enters described transformer oil tank.
10. the method for raising transformer oil anti-gassing performance according to claim 8, it is characterized in that, the wet solvent that described raffinate stripping tower stripping goes out enters described solvent seasoning tower through condensation and carries out drying, and the dried described solvent of described solvent seasoning tower bottom enters described extraction tower and recycles.
The method of 11. raising transformer oil anti-gassing performances according to claim 10, it is characterized in that, in described extraction oil refining tank, the refining secondary Extract obtained obtains the secondary Extract containing a small amount of solvent after pervaporation, and the secondary Extract containing a small amount of solvent obtains secondary and extracts oil out after stripping.
The method of 12. raising transformer oil anti-gassing performances according to claim 11, it is characterized in that, part secondary extracts oil out or part mixes with the Extract that described extraction tower extracting obtains through the secondary Extract of evaporation containing a small amount of solvent, enters described extraction oil refining tank and refines.
The method of 13. raising transformer oil anti-gassing performances according to claim 11, it is characterized in that, the solvent removed during the evaporation of secondary Extract and the wet solvent removed when evaporation contains the secondary Extract stripping of a small amount of solvent enter described solvent seasoning tower respectively and carry out drying.
The method of 14. raising transformer oil anti-gassing performances according to claim 12, it is characterized in that, the operational condition of described extraction oil refining tank is: secondary extracts oil out or the mass ratio of the amount that mixes with Extract through the secondary Extract of evaporation containing a small amount of solvent and stock oil is 0.1-1.0:1, the temperature of extracting oil refining tank out is 30 DEG C-40 DEG C, and the residence time that Extract stays in described extraction oil refining tank is 50-100 minutes; The residence time that the mixed solution that part secondary extraction oil or part obtain after the secondary Extract of evaporation containing a small amount of solvent mixes with an Extract stays in described extraction oil refining tank is 50-100 minutes.
The method of 15. raising transformer oil anti-gassing performances according to claim 8, is characterized in that, described stock oil is cycloalkyl transformer oil cut fraction hydrogenation depickling oil, and described solvent is furfural.
The method of 16. raising transformer oil anti-gassing performances according to claim 15, is characterized in that, described cycloalkyl transformer oil cut fraction hydrogenation depickling oil fraction scope is 280 DEG C-360 DEG C, close flash point ≮ 135 DEG C, fragrant charcoal (C
a) content ≮ 10%.
The method of 17. raising transformer oil anti-gassing performances according to claim 15, it is characterized in that, described furfural extraction condition is, described extraction tower tower top temperature 60 DEG C-80 DEG C, described extraction tower column bottom temperature is 30 DEG C-50 DEG C, and the mass ratio of described furfural and described cycloalkyl transformer oil cut fraction hydrogenation depickling oil is 1.5-2.5:1.
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| CN102676215A (en) * | 2011-03-08 | 2012-09-19 | 中国石油天然气股份有限公司 | Method for improving gassing resistance of transformer oil and equipment for producing transformer oil |
| CN202595050U (en) * | 2012-05-28 | 2012-12-12 | 中国石油天然气股份有限公司 | Production device of high-performance environment-friendly rubber oil |
| CN104212479A (en) * | 2013-06-05 | 2014-12-17 | 中国石油天然气股份有限公司 | Solvent refining method for producing rubber filling oil or lubricating oil |
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| CN102676215A (en) * | 2011-03-08 | 2012-09-19 | 中国石油天然气股份有限公司 | Method for improving gassing resistance of transformer oil and equipment for producing transformer oil |
| CN202595050U (en) * | 2012-05-28 | 2012-12-12 | 中国石油天然气股份有限公司 | Production device of high-performance environment-friendly rubber oil |
| CN104212479A (en) * | 2013-06-05 | 2014-12-17 | 中国石油天然气股份有限公司 | Solvent refining method for producing rubber filling oil or lubricating oil |
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