CN110317639A - A kind of processing technology and processing unit (plant) of conduction oil - Google Patents
A kind of processing technology and processing unit (plant) of conduction oil Download PDFInfo
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- CN110317639A CN110317639A CN201910689144.5A CN201910689144A CN110317639A CN 110317639 A CN110317639 A CN 110317639A CN 201910689144 A CN201910689144 A CN 201910689144A CN 110317639 A CN110317639 A CN 110317639A
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- 238000012545 processing Methods 0.000 title claims abstract description 29
- 238000005516 engineering process Methods 0.000 title claims abstract description 27
- 239000007788 liquid Substances 0.000 claims abstract description 46
- 238000000926 separation method Methods 0.000 claims abstract description 44
- 238000007670 refining Methods 0.000 claims abstract description 34
- 238000005194 fractionation Methods 0.000 claims abstract description 24
- 239000000047 product Substances 0.000 claims abstract description 18
- 238000010438 heat treatment Methods 0.000 claims abstract description 17
- 239000012264 purified product Substances 0.000 claims abstract description 6
- 239000001257 hydrogen Substances 0.000 claims description 33
- 229910052739 hydrogen Inorganic materials 0.000 claims description 33
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 32
- 239000007789 gas Substances 0.000 claims description 19
- 239000003054 catalyst Substances 0.000 claims description 18
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 7
- 239000004809 Teflon Substances 0.000 claims description 4
- 229920006362 Teflon® Polymers 0.000 claims description 4
- 230000006837 decompression Effects 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims 1
- 239000003344 environmental pollutant Substances 0.000 abstract description 4
- 231100000719 pollutant Toxicity 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 86
- 230000008676 import Effects 0.000 description 10
- 238000000034 method Methods 0.000 description 9
- 239000003795 chemical substances by application Substances 0.000 description 6
- 238000004821 distillation Methods 0.000 description 5
- 238000011161 development Methods 0.000 description 4
- 230000018109 developmental process Effects 0.000 description 4
- 239000002737 fuel gas Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 230000006872 improvement Effects 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000002199 base oil Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 238000005292 vacuum distillation Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 241000772415 Neovison vison Species 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002638 heterogeneous catalyst Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
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 present invention provides a kind of processing technology of conduction oil, the following steps are included: feedstock oil is successively carried out hydroisomerizing and post-refining, obtained purified product carries out high-pressure gas-liquid separation and separates with low-pressure gas-liquid, obtain low point of oil, then low point of obtained oil product is successively subjected to normal pressure fractionation and vacuum fractionation, obtains conduction oil；The temperature of the hydroisomerizing is 310~320 DEG C；The pressure of the hydroisomerizing is 15~16MPa；The temperature of the post-refining is 200~230 DEG C；The pressure of the post-refining is 15~16MPa.The present invention reduces device heating power, power consumption, non-pollutant discharge while improving conduction oil product quality.The present invention also provides a kind of processing unit (plant)s of conduction oil.
Description
Technical field
The invention belongs to technical field of fine more particularly to the processing technologys and processing unit (plant) of a kind of conduction oil.
Background technique
The development work of the thermally conductive oil product in China starts from late 1960s, mainly synthesis type conduction oil, but develops
Slowly.The seventies, with the introduction of external novel technique and equipment, external conduction oil new technology enters domestic market, domestic
Petrochemical industry has started research and trial production to conduction oil.The 1980s to the nineties, with petrochemical industry, chemical fibre and chemistry
The rapid development of industry and industrial application technology it is increasingly mature, the demand of new process, new technology to high-temperature heating is also increasingly
Greatly, increasingly obvious the advantages of conduction oil, the application field expanded of conduction oil.Due to China's conduction oil application technology starting compared with
It is evening, smaller to application market share shared at present, so there is huge development space and vast potential for future development.
Summary of the invention
The purpose of the present invention is to provide a kind of processing technology of conduction oil and processing unit (plant), process route of the invention is closed
Reason reduces device heating power, power consumption, non-pollutant discharge while improving conduction oil product quality.
The present invention provides a kind of processing technology of conduction oil, comprising the following steps:
Feedstock oil is successively subjected to hydroisomerizing and post-refining, obtained purified product carries out high-pressure gas-liquid separation and low
Gas-liquid separation is pressed, low point of oil is obtained, low point of obtained oil product is successively then subjected to normal pressure fractionation and vacuum fractionation, is led
Hot oil；
The temperature of the hydroisomerizing is 310~320 DEG C；The pressure of the hydroisomerizing is 15~16MPa；
The temperature of the post-refining is 200~230 DEG C；The pressure of the post-refining is 15~16MPa.
Preferably, the viscosity that the feedstock oil is 40 DEG C is 29.24mm2/s；The viscosity index (VI) of the feedstock oil is 109.
Preferably, the pressure of the high-pressure gas-liquid separation is 15.50MPa；
The temperature of the high-pressure gas-liquid separation is 40~50 DEG C.
Preferably, the pressure of the low-pressure gas-liquid separation is 1.31MPa；
The temperature of the low-pressure gas-liquid separation is 40~50 DEG C.
Preferably, catalyst used in the hydroisomerizing is the EM7611 and EM7663 that Exxon Mobil Corporation provides
The catalyst of model.
Preferably, catalyst used in the post-refining is the catalysis for avenging the ICR419 model that teflon company provides
Agent.
Preferably, the normal pressure fractionation carries out in atmospheric tower, and the normal pressure column overhead temperatures are 165~240 DEG C；
The atmospheric tower tower top pressure is 0.1~0.3MPa；The atmospheric tower tower bottom liquid level is 30~70%.
Preferably, the vacuum fractionation carries out in vacuum tower, and the decompression column overhead temperatures are 50~90 DEG C；It is described to subtract
Pressure column overhead regurgitant volume is 8~40t/h.
The present invention provides a kind of conduction oil processing unit (plant), including sequentially connected raw material surge tank plus hydrogen charging heating furnace,
Hydroisomerization reactor, hydrofining reactor, high-pressure air cooler, high-pressure separator, low pressure separation pot, atmospheric pressure kiln, atmospheric tower,
Vacuum furnace and vacuum tower；
The outlet at bottom of the high-pressure separator is connected with the low pressure separation pot, top exit successively with digester and
Recycle hydrogen liquid separation tank is connected.
The present invention provides a kind of processing technology of conduction oil, comprising the following steps: feedstock oil is successively carried out hydroisomerizing
And post-refining, obtained purified product carry out high-pressure gas-liquid separation and separate with low-pressure gas-liquid, obtain low point of oil, then will obtain
Low point of oil product successively carry out normal pressure fractionation and vacuum fractionation, obtain conduction oil；The temperature of the hydroisomerizing be 310~
320℃；The pressure of the hydroisomerizing is 15~16MPa；The temperature of the post-refining is 200~230 DEG C；The supplement essence
The pressure of system is 15~16MPa.The present invention uses high-pressure hydrogenation process technology, carries out to the technique of hydroisomerizing and post-refining
It improves, the deep refining of the isomerization-visbreaking and refining agent that cooperate isomery agent makes low point of oily pour point and coloration mention raising, simultaneously
Device fuel gas and hydrogen consumption are reduced, operation cost is saved；Low point of oil is fractionated to obtain conduction oil through mature Atmospheric vacuum.Often subtract
Pressure distillation divides normal pressure fractionation and deep vacuum distillation, and process route is reasonable, mature technology, is improving conduction oil product quality
Meanwhile reducing device heating power, power consumption, non-pollutant discharge.
Detailed description of the invention
In order to more clearly explain the embodiment of the invention or the technical proposal in the existing technology, to embodiment or will show below
There is attached drawing needed in technical description to be briefly described, it should be apparent that, the accompanying drawings in the following description is only this
The embodiment of invention for those of ordinary skill in the art without creative efforts, can also basis
The attached drawing of offer obtains other attached drawings.
Fig. 1 is the processing unit (plant) figure of conduction oil in the present invention；Wherein, 1 is raw material surge tank, and 2 is add hydrogen fine fodder heating furnace,
3 be hydroisomerization reactor, and 4 be hydrofining reactor, and 5 be high-pressure air cooler, and 6 be high-pressure separator, and 7 be digester, and 8 are
Recycle hydrogen liquid separation tank, 9 be low pressure separator, and 10 be atmospheric tower, and 11 be vacuum tower.
Specific embodiment
The present invention provides a kind of processing technologys of conduction oil, comprising the following steps:
Feedstock oil is successively subjected to hydroisomerizing and post-refining, obtained purified product carries out high-pressure gas-liquid separation and low
Gas-liquid separation is pressed, low point of oil is obtained, low point of obtained oil product is successively then subjected to normal pressure fractionation and vacuum fractionation, is led
Hot oil；
The temperature of the hydroisomerizing is 310~320 DEG C；The pressure of the hydroisomerizing is 15~16MPa；
The temperature of the post-refining is 200~230 DEG C；The pressure of the post-refining is 15~16MPa.
In the present invention, the viscosity of 40 DEG C of the feedstock oil is 29.24mm2/s；The viscosity index (VI) of the feedstock oil is
109.The feedstock oil is the cracking tail oil from hydrocracking unit.
The feedstock oil is preferably first heated to required reaction temperature by the present invention, and it is anti-then to carry out hydroisomerizing again
It answers；The present invention heats the feedstock oil preferably in heating furnace, in the present invention, the temperature of the hydroisomerizing
Preferably 310~320 DEG C, more preferably 315 DEG C；The pressure of the hydroisomerizing be 15~16MPa, more preferably 15.5~
15.6MPa, the reaction velocity of the hydroisomerizing are preferably 1~2h-1, more preferably 1.5h-1.Present invention preferably employs Essens
The hydroisomerisation catalysts for the EM7611 and EM7663 model that gram Mobil provides, the dosage of the hydroisomerisation catalysts are
12.521 tons.
After completing the hydroisomerizing, obtained isomate is subjected to post-refining, the post-refining preferably exists
It being carried out in hydrofining reactor, the reaction temperature of post-refining reaction is 200~230 DEG C, more preferably 210~220
DEG C, the pressure of the post-refining is 15~16MPa, more preferably 15.1~15.5MPa, and the post-refining reaction velocity is excellent
It is selected as 1~2h-1, more preferably 1.2~1.5h-1.Present invention preferably employs the purifications of the ICR419 model of snow teflon offer to urge
Agent, the dosage of the catalyst for refining are preferably 13.393 tons.
After obtaining the product of hydrofinishing, the product of hydrofinishing is carried out gas-liquid point by the present invention in high-pressure separator
From the hydrogen-rich gas isolated enters digester at the top of the high-pressure separator, removes H2After S, into circulation hydrogen compressed
Machine liquid separation tank liquid separation finally enters circulating hydrogen compressor recycling.
The liquid of the high-pressure separator bottom carries out gas-liquid separation after depressurizing, into low pressure separator, isolated
Low point of gas and low point of oil.The pressure of the low-pressure gas-liquid separation is preferably 1.3MPa；The temperature of the low-pressure gas-liquid separation is preferred
It is 43 DEG C.Obtained low point of oily pour point preferably≤- 27 DEG C.
After completing the low-pressure gas-liquid separation, low point of obtained oil enters atmospheric tower and vacuum tower and successively carries out normal pressure fractionation
And vacuum fractionation.
In the present invention, the low point of oil, which is preferably introduced into atmospheric pressure kiln, to be heated, needed for the low point of oil is heated to
It after temperature, is fractionated into atmospheric tower, the normal pressure heater outlet temperature is preferably 260~340 DEG C, more preferably 280~300
℃；The atmospheric pressure kiln fire box temperature is preferably 650~750 DEG C；The atmospheric pressure kiln oxygen content of smoke gas is preferably 4~6%；It is described normal
The tower top temperature for pressing tower is preferably 165~240 DEG C；The tower top pressure of the atmospheric tower is preferably 0.1~0.3MPa；The normal pressure
Tower tower bottom is also preferably 30~70%.
After frequent pressure fractionating, obtained tower bottom product enters vacuum furnace, carries out vacuum fractionation subsequently into vacuum tower, described
Vacuum furnace branch outlet temperature is preferably 330~355 DEG C, and more preferably 340~350 DEG C；The vacuum furnace oxygen content of smoke gas is excellent
4~6% are selected as, the vacuum tower tower top pressure is preferably 3.0KPa~6.0KPa；The decompression column overhead temperatures are preferably 50
~90 DEG C；The vacuum tower top pumparound amount is preferably 8~40t/h, more preferably 10~30t/h, most preferably 20~
25t/h；The vacuum tower tower bottom liquid level is preferably 30~70%；The washing flow is preferably 1.2~8t/h, the washing master
If being segregated into the mink cell focus of entrained in distillation stage gas phase, oil product fractionating effect is improved.
Subtract top through fractionating out of coming out of vacuum tower and follow that oil, first vacuum side stream, second line of distillation are oily, subtract third fractional oil, subtract base oil, wherein
Subtract one, two wires miscella is required product conduction oil in the present invention.40 DEG C of viscosity of conduction oil in the present invention are 28~
35.2mm2/s；Flash-point >=200 DEG C of the conduction oil；Pour point≤- 20 DEG C of the conduction oil.
The present invention is by screening catalyst, and by hydroisomerizing, hydrofinishing is fractionated with normal pressure and vacuum fractionation combines, and
Corresponding technological improvement has been carried out to processing technology relevant parameter, has improved thermally conductive oil quality, while reducing plant energy consumption.
The present invention also provides a kind of processing unit (plant)s of conduction oil, including sequentially connected raw material surge tank plus hydrogen charging
Heating furnace, hydroisomerization reactor, hydrofining reactor, high-pressure air cooler, high-pressure separator, low pressure separation pot, atmospheric pressure kiln,
Atmospheric tower, vacuum furnace and vacuum tower；
The outlet at bottom of the high-pressure separator is connected with the low pressure separation pot, top exit successively with digester and
Recycle hydrogen liquid separation tank is connected
In the present invention, the raw material surge tank be used for feedstock oil charging, the outlet of the raw material surge tank with it is described
Add and is connected between the import of hydrogen charging heating furnace using pipeline, the former described plus hydrogen charging heating in the outlet of the raw material surge tank
Hydrogen inlet is provided in the connecting pipe of the import of furnace, hydrogen enters from hydrogen inlet, after mixing in pipeline with feedstock oil
Enter jointly plus hydrogen feeds heating furnace.
Described plus hydrogen charging heating furnace is used to be heated to feedstock oil the reaction temperature of hydroisomerizing, and the present invention adds to described
Hydrogen charging heating furnace does not have special limitation.
The outlet of described plus hydrogen charging heating furnace is connected with the import of hydroisomerization reactor, the hydroisomerizing reaction
It is mounted with hydroisomerization catalyst in device, provides place for the hydroisomerizing reaction for feedstock oil.
The import of the hydrofining reactor is connected with the outlet of the hydroisomerization reactor, the hydrofinishing
It is mounted with catalyst for refining in reactor, provides the place of hydrofinishing for the feedstock oil for isomerization.The hydrofinishing
The outlet of reactor is connected with the import of high-pressure air cooler, and the feedstock oil after hydrofinishing enters high pressure separation after carrying out cooling
Device carries out gas-liquid separation.
The high-pressure separator is separated oil, oily wastewater, recycle hydrogen by the density of oil-water-gas.The high pressure point
From outlet is provided at the top of device, for separating hydrogen-rich gas；The outlet at the top is connected with the import of digester, is used for
H in hydrogen-rich gas2The outlet of the removing of S, the digester is connected with the import of circulating hydrogen compressor liquid separation tank, the circulation
The outlet of hydrogen compressor liquid separation tank is connected with the circulating hydrogen compressor.Circulation is arranged in the present invention before the recycle compressor
Compressor liquid separation tank can reduce entrained liquid, reduce liquid phase and enter in compressor.
The bottom of the high-pressure separator is provided with outlet, and for separating liquid phase, the outlet of the bottom is separated with low pressure
The import of tank is connected.
The low pressure separation pot is knockout drum, and main function is to carry out gas liquid separation, and isolated substance is low point
Gas, low point of oil.The low pressure separation pot is provided with low point of gas outlet, low point of oil export and oily wastewater outlet, the low point of oil
Outlet is connected with the import of atmospheric tower.
The atmospheric tower normal pressure fractionation oily for low point, atmospheric pressure kiln, low point of oil is preferably arranged in the present invention before atmospheric tower
It is first heated to required temperature in atmospheric pressure kiln, then enters back into atmospheric tower and carries out normal pressure fractionation.
The tower top outlet of the atmospheric tower is preferably connected with air cooler, water cooler in turn and often pushes up return tank, and being used for will be normal
The Oil-gas Separation for pressing column overhead, isolated normal top oil removes tank field, Chang Dingqi to fuel system or fire in often top return tank
Torch emptying.
The outlet of the atmospheric tower is connected with the import of the vacuum tower, and the present invention is preferably arranged before the vacuum tower
Vacuum furnace is heated for low point of oil after being fractionated to normal pressure, and the vacuum tower, which is provided with, to be subtracted top and follow oil export, first vacuum side stream
Outlet, second line of distillation oil export subtract third fractional oil outlet and subtract base oil outlet.For different fractions to be discharged.
The vacuum tower tower top outlet is connected with three-level vacuum evacuation device, condenser and separator in turn, for that will depressurize
The oil gas of column overhead is separated, and isolated subtracts top oil to tank field, and obtained top gas to the fuel gas system or torch that subtract is put
It is empty.
Specifically, the conduction oil in the present invention is processed to obtain according to following below scheme:
Feedstock oil from tank field is heated after exchanging heat to reaction heating furnace, after being heated to required reaction temperature
Into hydroisomerization reactor, hydroisomerizing reaction is carried out under the action of hydroisomerization catalyst, reaction product is from adding hydrogen different
The bottom of structure reactor is discharged, and post-refining reactor is entered after exchanging heat, and virtue is carried out under the action of Hydrobon catalyst
Hydrocarbon adds hydrogen to be saturated, and the bottoms effluent of post-refining reactor enters high-pressure separator after being exchanged heat, being cooled down and carries out gas/liquid point
From.The hydrogen-rich gas isolated at the top of high-pressure separator is through digester adsorbing and removing H2After S, circulating hydrogen compressor liquid separation tank point is removed
Enter circulating hydrogen compressor after liquid to be recycled.The product liquid of high-pressure separator bottom enters after fluid level control valve depressurizes
Low pressure separator carries out gas liquid separation.The low point of gas that low pressure separator is isolated is discharged into fuel gas pipe network, after low point of oil heat exchange,
It is fractionated to atmospheric tower and vacuum tower, carries out product segmentation.
The present invention provides a kind of processing technology of conduction oil, comprising the following steps: feedstock oil is successively carried out hydroisomerizing
And post-refining, obtained purified product carry out high-pressure gas-liquid separation and separate with low-pressure gas-liquid, obtain low point of oil, then will obtain
Low point of oil product successively carry out normal pressure fractionation and vacuum fractionation, obtain conduction oil；The temperature of the hydroisomerizing be 310~
320℃；The pressure of the hydroisomerizing is 15~16MPa；The temperature of the post-refining is 200~230 DEG C；The supplement essence
The pressure of system is 15~16MPa.The present invention uses high-pressure hydrogenation process technology, carries out to the technique of hydroisomerizing and post-refining
It improves, the deep refining of the isomerization-visbreaking and refining agent that cooperate isomery agent makes low point of oily pour point and coloration mention raising, simultaneously
Device fuel gas and hydrogen consumption are reduced, operation cost is saved；Low point of oil is fractionated to obtain conduction oil through mature Atmospheric vacuum.Often subtract
Pressure distillation divides normal pressure fractionation and deep vacuum distillation, while improving conduction oil product quality, reduce device heating power, power consumption,
Non-pollutant discharge.
In order to further illustrate the present invention, with reference to embodiments to a kind of processing technology of conduction oil provided by the invention
And processing unit (plant) is described in detail, but cannot be understood as limiting the scope of the present invention.
Embodiment 1
Using the device in Fig. 1, conduction oil is processed according to the technological parameter in following table.
Hydroisomerization catalyst is the heterogeneous catalyst for EM7611, EM763 model that Essen gram Mobil provides, hydrofinishing
Catalyst is the catalyst for refining for avenging the ICR419 model that teflon provides.
40 DEG C of viscosity of obtained conduction oil are 30.97mm2/ s, viscosity index (VI) 104, flash-point are 232 DEG C, and pour point is -26
DEG C, coloration is+30.
Comparative example 1
It processes to obtain conduction oil according to the method in embodiment 1, unlike, the temperature of hydroisomerizing is in this comparative example
329℃。
40 DEG C of viscosity of obtained conduction oil are 29.97mm2/ s, viscosity index (VI) 98, flash-point are 220 DEG C, and pour point is -32
DEG C, coloration is+30.
The above is only a preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
For member, various improvements and modifications may be made without departing from the principle of the present invention, these improvements and modifications are also answered
It is considered as protection scope of the present invention.
Claims (9)
1. a kind of processing technology of conduction oil, comprising the following steps:
Feedstock oil is successively subjected to hydroisomerizing and post-refining, obtained purified product carries out high-pressure gas-liquid separation and low pressure gas
Liquid separation, obtains low point of oil, low point of obtained oil product is successively then carried out normal pressure fractionation and vacuum fractionation, is obtained thermally conductive
Oil；
The temperature of the hydroisomerizing is 310~320 DEG C；The pressure of the hydroisomerizing is 15~16MPa；
The temperature of the post-refining is 200~230 DEG C；The pressure of the post-refining is 15~16MPa.
2. conduction oil processing technology according to claim 1, which is characterized in that the feedstock oil is that 40 DEG C of viscosity is
29.24mm2/s；The viscosity index (VI) of the feedstock oil is 109.
3. conduction oil processing technology according to claim 1, which is characterized in that the pressure of high-pressure gas-liquid separation is
15.50MPa；
The temperature of the high-pressure gas-liquid separation is 40~50 DEG C.
4. conduction oil processing technology according to claim 1, which is characterized in that the pressure of low-pressure gas-liquid separation is
1.31MPa；
The temperature of the low-pressure gas-liquid separation is 40~50 DEG C.
5. conduction oil processing technology according to claim 1, which is characterized in that catalyst used in the hydroisomerizing
For the catalyst for the EM7611 and EM7663 model that Exxon Mobil Corporation provides.
6. conduction oil processing technology according to claim 1, which is characterized in that catalyst used in the post-refining
For the catalyst for the ICR419 model that snow teflon company provides.
7. conduction oil processing technology according to claim 1, which is characterized in that normal pressure fractionation in atmospheric tower into
Row, the normal pressure column overhead temperatures are 165~240 DEG C；
The atmospheric tower tower top pressure is 0.1~0.3MPa；The atmospheric tower tower bottom liquid level is 30~70%.
8. conduction oil processing technology according to claim 1, which is characterized in that the vacuum fractionation in vacuum tower into
Row, the decompression column overhead temperatures are 50~90 DEG C；The vacuum tower overhead reflux amount is 8~40t/h.
9. a kind of conduction oil processing unit (plant), including sequentially connected raw material surge tank plus hydrogen charging heating furnace, hydroisomerizing reaction
Device, hydrofining reactor, high-pressure air cooler, high-pressure separator, low pressure separation pot, atmospheric pressure kiln, atmospheric tower, vacuum furnace and decompression
Tower；
The outlet at bottom of the high-pressure separator is connected with the low pressure separation pot, top exit successively with digester and circulation
Hydrogen liquid separation tank is connected.
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| CN201910689144.5A CN110317639A (en) | 2019-07-29 | 2019-07-29 | A kind of processing technology and processing unit (plant) of conduction oil |
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| CN201910689144.5A CN110317639A (en) | 2019-07-29 | 2019-07-29 | A kind of processing technology and processing unit (plant) of conduction oil |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115261069A (en) * | 2022-06-29 | 2022-11-01 | 海南汉地阳光石油化工有限公司 | Preparation method of novel coastal anticorrosive paint blender |
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| US20080073248A1 (en) * | 2006-09-26 | 2008-03-27 | Chevron U.S.A. Inc. | Heat transfer oil with high auto ignition temperature |
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| US20080073248A1 (en) * | 2006-09-26 | 2008-03-27 | Chevron U.S.A. Inc. | Heat transfer oil with high auto ignition temperature |
| CN109181767A (en) * | 2018-09-26 | 2019-01-11 | 海南汉地阳光石油化工有限公司 | A kind of preparation method of high speed engine base oil |
| CN109181768A (en) * | 2018-09-26 | 2019-01-11 | 海南汉地阳光石油化工有限公司 | A kind of preparation method of low temp area motor-car transmission oil |
| CN109722304A (en) * | 2019-01-28 | 2019-05-07 | 海南汉地阳光石油化工有限公司 | A kind of production method of hydraulic oil |
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| CN115261069A (en) * | 2022-06-29 | 2022-11-01 | 海南汉地阳光石油化工有限公司 | Preparation method of novel coastal anticorrosive paint blender |
| CN115261069B (en) * | 2022-06-29 | 2024-02-20 | 海南汉地阳光石油化工有限公司 | Preparation method of novel coastal anti-corrosion coating blending agent |
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