CN110272761A - A kind of production method and process units of easer - Google Patents
A kind of production method and process units of easer Download PDFInfo
- Publication number
- CN110272761A CN110272761A CN201910689135.6A CN201910689135A CN110272761A CN 110272761 A CN110272761 A CN 110272761A CN 201910689135 A CN201910689135 A CN 201910689135A CN 110272761 A CN110272761 A CN 110272761A
- Authority
- CN
- China
- Prior art keywords
- pressure
- oil
- vacuum
- tower
- fractionation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- 230000008569 process Effects 0.000 title claims abstract description 19
- 239000003921 oil Substances 0.000 claims abstract description 107
- 239000007788 liquid Substances 0.000 claims abstract description 60
- 238000000926 separation method Methods 0.000 claims abstract description 42
- 238000005194 fractionation Methods 0.000 claims abstract description 33
- 238000000034 method Methods 0.000 claims abstract description 21
- 239000000047 product Substances 0.000 claims abstract description 21
- 239000000463 material Substances 0.000 claims abstract description 10
- 239000010687 lubricating oil Substances 0.000 claims abstract description 9
- 239000012264 purified product Substances 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 45
- 229910052739 hydrogen Inorganic materials 0.000 claims description 29
- 239000001257 hydrogen Substances 0.000 claims description 29
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 27
- 239000002994 raw material Substances 0.000 claims description 20
- 238000010438 heat treatment Methods 0.000 claims description 13
- 238000009826 distribution Methods 0.000 claims description 10
- 239000003054 catalyst Substances 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 5
- 230000005494 condensation Effects 0.000 claims description 5
- 230000006837 decompression Effects 0.000 claims description 5
- 239000000835 fiber Substances 0.000 claims description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 4
- 239000004809 Teflon Substances 0.000 claims description 4
- 229920006362 Teflon® Polymers 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 4
- 239000011449 brick Substances 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- 239000005864 Sulphur Substances 0.000 claims description 2
- 238000007664 blowing Methods 0.000 claims description 2
- 230000000149 penetrating effect Effects 0.000 claims 1
- 230000001105 regulatory effect Effects 0.000 claims 1
- 238000004821 distillation Methods 0.000 abstract description 15
- 238000011084 recovery Methods 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 230000008676 import Effects 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- 239000002199 base oil Substances 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 7
- 238000007670 refining Methods 0.000 description 7
- 239000000945 filler Substances 0.000 description 6
- 239000002737 fuel gas Substances 0.000 description 6
- 239000010865 sewage Substances 0.000 description 6
- 239000002904 solvent Substances 0.000 description 6
- 239000012071 phase Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000007639 printing Methods 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 239000000654 additive Substances 0.000 description 3
- 230000000996 additive effect Effects 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 230000036541 health Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000006378 damage Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000008258 liquid foam Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 241000973497 Siphonognathus argyrophanes Species 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000004042 decolorization Methods 0.000 description 1
- 238000005034 decoration Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000002761 deinking Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000009972 noncorrosive effect Effects 0.000 description 1
- 231100000956 nontoxicity Toxicity 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 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 production method of easer, the following steps are included: light lubricating oil material is successively carried out hydroisomerizing and hydrofinishing, 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, vacuum fractionation and stripping, obtains easer；The temperature of the hydroisomerizing is 330~340 DEG C, and the temperature of the hydrofinishing is 240~250 DEG C；The pressure of the high-pressure gas-liquid separation is 14~15MPa；The temperature of the normal pressure fractionation is 285~290 DEG C, and the pressure of the normal pressure fractionation is 230~240KPa；The temperature of the vacuum fractionation is 350~360 DEG C, and the pressure of the vacuum fractionation is 4~5KPa.Easer performance in the present invention is stablized, nonpollution environment, harmless, distillation recovery high income.The present invention also provides a kind of process units of easer.
Description
Technical field
The invention belongs to technical field of petrochemical industry more particularly to the production methods and production dress of a kind of easer
It sets.
Background technique
Easer is the important materials for printing, it is expressed the pattern and text on stock by printing.Oil
It include main component and auxiliary element in ink, they equably mix and form a kind of stickiness colloidal fluid through repeat-rolling.By
The composition such as link stuff (resin), pigment, filler, auxiliary agent and solvent.For books and periodicals, packing and decorating, building decoration and electronic circuit
The various printings such as plate.As social demand increases, ink variety and yield also respective extension and growth.
In recent years, attention of the people to environmental protection and worker's occupational health and the weight to food packaging safety performance
Depending on the harm of benzene soluble ink additive is increasingly understood by people.But, today, we still saw that benzene soluble ink adds
Agent is still widely used in plastics package printing.Therefore, benzene soluble ink additive has been replaced using new environment-friendlyink ink additive
It is very urgent.But due to being limited by economic technology condition, this process can not accomplish in one move.Due to water-based ink skill
Art is also immature, therefore the task of top priority is to promote the use of the environment-friendlyink ink of technical conditions maturation.
Summary of the invention
Production the purpose of the present invention is to provide a kind of production method of easer and process units, in the present invention
The easer that method obtains is ultralow toxicity, will not be caused damages to human body and environment, meanwhile, also improve ink addition
The quality of agent.
The present invention provides a kind of production method of easer, comprising the following steps:
Light lubricating oil material is successively subjected to hydroisomerizing and hydrofinishing, obtained purified product carry 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, vacuum fractionation and vapour
It mentions, obtains easer；
The temperature of the hydroisomerizing is 330~340 DEG C, and the temperature of the hydrofinishing is 240~250 DEG C；
The pressure of the high-pressure gas-liquid separation is 14~15MPa；
The temperature of the normal pressure fractionation is 285~290 DEG C, and the pressure of the normal pressure fractionation is 230~240KPa；It is described to subtract
The temperature of pressure fractionating is 308~310 DEG C, and the pressure of the vacuum fractionation is 4~5KPa.
Preferably, the density of the light lubricating oil material is 843g/cm3, sulfur content is 3.3~3.4 μ g/g, and condensation point is 24 DEG C,
Viscosity index (VI) is 115, and flash-point is 222~226 DEG C, and initial boiling point is 360 DEG C.
Preferably, the catalyst of the hydrofinishing is the catalyst for avenging the ICR409 model that teflon company provides.
Preferably, the pressure of the low-pressure gas-liquid separation is 1.34MPa；
The temperature of the low-pressure gas-liquid separation is 40~50 DEG C.
Preferably, the low point of oily density is 847~849kg/m3, viscosity is 27~28mm2/S, viscosity index (VI) 101
~103, flash-point is 28~30 DEG C, evaporation loss 21.1.
Preferably, the air-blowing quantity of the vacuum tower is 0.25~0.3t/h.
The present invention provides a kind of process units of easer, including sequentially connected raw material surge tank plus hydrogen charging
Heating furnace, hydroisomerization reactor, hydrofining reactor, high-pressure separator, low pressure separator, atmospheric pressure kiln, atmospheric tower, decompression
Furnace, vacuum tower and stripper；
The bottom of the atmospheric pressure kiln and vacuum furnace is mounted on burner, and the burner includes shell, gas collecting tube, air gun
And altar lamp；
The side wall of outer shell is provided with air inlet, and the face plate center of the outer casing bottom is equipped with gas collecting tube；
The side wall of the gas collecting tube is provided with several connecting holes, for connecting several air guns；
The air gun is passed through and is fixed on the panel of the outer casing bottom；The altar lamp is passed through and is fixed on described outer
On the panel of shell bottom；
Fire hole and peephole are provided on the panel of the outer casing bottom；
Plug is tamped in fact using refractory fibre between refractory brick in the burner and atmospheric pressure kiln and vacuum furnace.
Preferably, the tower top of the atmospheric tower is provided with overhead air cooler device, the overhead air cooler device and the atmospheric tower
Tower top outlet is connected, and the outlet of the overhead air cooler device is provided with temperature control adjusting valve.
Preferably, it is provided with liquid distribution trough in the vacuum tower, is arranged in parallel with reflection above the liquid distribution trough
Plate.
Preferably, for several described air guns centered on gas collecting tube, radiant type is evenly distributed on the face of the outer casing bottom
On plate.
The present invention provides a kind of production method of easer, comprising the following steps: is successively added light lubricating oil material
Hydrogen isomery and hydrofinishing, obtained purified product carry out high-pressure gas-liquid separation and separate with low-pressure gas-liquid, obtain low point of oil, then
Low point of obtained oil product is successively subjected to normal pressure fractionation, vacuum fractionation and stripping, obtains easer；The hydroisomerizing
Temperature be 330~340 DEG C, the temperature of the hydrofinishing is 240~250 DEG C；The pressure of the high-pressure gas-liquid separation is 14
~15MPa；The temperature of the normal pressure fractionation is 285~290 DEG C, and the pressure of the normal pressure fractionation is 230~240KPa；It is described to subtract
The temperature of pressure fractionating is 350~360 DEG C, and the pressure of the vacuum fractionation is 4~5KPa.Present invention research passes through existing apparatus
Process characteristic is transformed, Optimizing Process Parameters through test, and analysis oil product composition variation adjusts operating condition, it is domestic to produce satisfaction
The novel environment friendly easer (low aromatic hydrocarbons, low-sulfur, low n-hexane content) of outer correlative link health care health standard.Its performance is stablized,
Smell is small, nonpollution environment, it is applied widely, harmless, be distilled to recover high income.The discarded ink of effective solution returns
Difficult, deinking hardly possible problem is received, and meets nontoxicity, non-corrosive, is had no irritating odor, free of contamination Environmental Safety requirement,
With biggish market competition advantage.
The present invention also provides a kind of process units of easer, the present invention has used efficiently the transformation of heating furnace
Nozzles, reduce most of energy consumption, clean energy resource efficiently produces；Atmospheric tower is transformed, increases temperature control adjusting valve in tower top,
Overhead air cooler is transformed, design atmospheric tower head temperature control effectively cuts light straight run fraction oil, meets rectifying column production
The special solvent oil of 150~190 DEG C of narrow fractions；The liquid distribution trough of vacuum tower increases reflecting plate on secondary slot, due to anti-
It penetrates the cloth liquid and guiding function of plate: uniform liquid distribution, anti-clogging and wiping 1. effectively being made to make the elastic line for realizing liquid greatly
The direct interference that shape is distributed and air-flow is prevented to spray spray apertures, reduces liquid foam entrainment；2. after transformation, the yield of product
It greatly improves, the flow of easer oil has been increased to 10t/h by original 7t/h.
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 structural schematic diagram of process units in the present invention；
Wherein, 1 is raw material surge tank, and 2 is add hydrogen to feed heating furnace, and 3 be hydroisomerization reactor, and 4 is anti-for hydrofinishing
Device is answered, 5 be high-pressure separator, and 6 be low pressure separator, and 7 be atmospheric pressure kiln, and 8 be atmospheric tower, and 9 be vacuum furnace, and 10 be vacuum tower, 10-
1 is liquid distribution trough, and 10-2 is reflecting plate, and 11 be stripper；
Fig. 2 is the structural schematic diagram that nozzles are heated in the present invention；
Fig. 3 is that nozzles A is heated in Fig. 2 of the present invention to structural schematic diagram；
Wherein, a is shell, and b is air inlet, and c is gas collecting tube, and d is air gun, and e is altar lamp, and f is refractory fibre, and g is to see
Fire hole, h are fire hole.
Specific embodiment
The present invention provides a kind of production methods of easer, comprising the following steps:
Light lubricating oil material is successively subjected to hydroisomerizing and hydrofinishing, obtained purified product carry 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, vacuum fractionation and vapour
It mentions, obtains easer；
The temperature of the hydroisomerizing is 330~340 DEG C, and the temperature of the hydrofinishing is 240~250 DEG C；
The pressure of the high-pressure gas-liquid separation is 14~15MPa；
The temperature of the normal pressure fractionation is 285~290 DEG C, and the pressure of the normal pressure fractionation is 230~240KPa；It is described to subtract
The temperature of pressure fractionating is 350~360 DEG C, and the pressure of the vacuum fractionation is 4~5KPa.
In the present invention, the light sliding oil density is 843g/cm3, sulfur content is 3.3~3.4 μ g/g, nitrogen content <
0.20 μ g/g, condensation point are that the viscosity at 24 DEG C, 40 DEG C is 27.3~27.7mm2/S, the viscosity at 100 DEG C are 5.1mm2/S, viscosity
Index is 115, and flash-point is 222~226 DEG C, and initial boiling point is 360 DEG C.Specifically, the present invention uses Sinopec Hainan oil refiningization
The light lubricating oil material that 1,200,000 tons/year of hydrocracking units of work Co., Ltd provide is raw material.
In the present invention, the light lubricating oil material preferably first carries out after being heated to certain temperature, then carries out hydroisomerizing reaction,
The hydroisomerizing can reduce the pour point of feedstock oil, improve oil low-temperature mobility.The reaction temperature of the hydroisomerizing is excellent
It is selected as 330~340 DEG C, more preferably 330~335 DEG C；The reaction pressure of the hydroisomerizing is preferably 15~16MPa, more excellent
It is selected as 15.5MPa；The present invention carries out the hydroisomerizing reaction, the hydroisomerizing reaction preferably in hydroisomerization reactor
The inlet pressure of device is preferably 15.7MPa, and bed overall presure drop is preferably 0.2MPa, and two bed inlet temperatures are preferably 333 DEG C, bed
Layer mean temperature is preferably 330 DEG C, and two bed outlet temperatures are preferably 328~329 DEG C.
The product that hydroisomerizing obtains, which enters, carries out hydrofinishing in hydrofining reactor, the hydrofinishing is for taking off
The impurity such as sulphur removal nitrogen, aromatic hydrocarbons improve oxidation stability.The inlet temperature of the hydrofining reactor is preferably 244~246
DEG C, more preferably 245 DEG C；One bed inlet temperatures are preferably 250~252 DEG C, and more preferably 251 DEG C, inlet pressure is preferably
15.4MPa, the stagnation pressure in hydrofining reactor are reduced to 0.08MPa, and the bed mean temperature of the hydrofining reactor is
243 DEG C, the inlet temperature of two beds is 243 DEG C, outlet pressure 15.3MPa.
In the present invention, the catalysis for the ICR409 model that the hydrofining reaction is provided it is preferable to use snow teflon company
Agent.
Obtained purified product carries out high-pressure gas-liquid separation, and after high-pressure gas-liquid separates, the hydrogen-rich gas isolated is smart
After desulfurization adsorbing and removing H2S, circulating hydrogen compressor liquid separation is gone to be recycled, the product liquid at high-pressure gas-liquid separation, after
It is continuous to carry out low-pressure gas-liquid separation.The pressure of the high-pressure gas-liquid separation is preferably 14~15MPa, and hydrogen discharge amount of giving up is preferably 237
~247Nm3/ h, the high-pressure gas-liquid separation carry out in high-pressure separator, and the liquid level in the high-pressure separator is preferably 54
~55%.
Product liquid after high-pressure gas-liquid separation enters low pressure separator and carries out low-pressure gas-liquid separation, by low-pressure gas-liquid point
Low point of gas and low point of oil are obtained from after, the pressure of the low-pressure gas-liquid separation is 1.3~1.4MPa, preferably 1.34MPa, institute
The discharge amount for stating low point of gas is preferably 350~363Nm3/ h, the liquid level in the low pressure separator is preferably 41~42%.
Low point of isolated oil density of low-pressure gas-liquid is 847~849kg/m3, viscosity is 27~28mm at 40 DEG C2/S,
Viscosity is 4.6~4.9mm at 100 DEG C2/S, viscosity index (VI) are 101~103, and flash-point is 28~30 DEG C, and evaporation loss 21.1 is inclined
Point is -27~-28 DEG C.
Low point of obtained oil enters atmospheric tower and carries out normal pressure fractionation, and the normal pressure column overhead temperatures are 175~185 DEG C, often
Pressure column overhead pressure is preferably 230~240KPa, and it is preferably 293~296 DEG C that atmospheric tower tower bottom, which extracts temperature out, the charging of atmospheric tower
Temperature is 285~290 DEG C.
Atmospheric tower base oil after normal pressure is fractionated enters vacuum tower and carries out vacuum fractionation, and the temperature of the vacuum fractionation is excellent
308~310 DEG C are selected as, the tower top pressure of the vacuum tower is preferably 4~5KPa, and the flow of the vacuum fractionation product is preferably
12t/h。
Product after vacuum fractionation enters stripper and is purified, and obtains easer solvent naphtha.
The present invention also provides a kind of easer, the density of obtained easer solvent naphtha is 852kg/m3,
Viscosity at 40 DEG C is 41~42mm2/S, the viscosity at 100 DEG C are 6.5mm2/S, viscosity index (VI) are 106~107, flash-point 241
~243 DEG C, pour point is -18~-22 DEG C.
The present invention also provides a kind of process units of easer, including sequentially connected raw material surge tank plus hydrogen
Feed heating furnace, hydroisomerization reactor, hydrofining reactor, high-pressure air cooler, high-pressure separator, low pressure separation pot, often
Press furnace, atmospheric tower, vacuum furnace and vacuum tower；
The bottom of the atmospheric pressure kiln and vacuum furnace is provided with heating nozzles, is equipped with burner, and the burner includes
Shell, gas collecting tube, air gun and altar lamp；
The side wall of outer shell is provided with air inlet, and the face plate center of the outer casing bottom is equipped with gas collecting tube；
The side wall of the gas collecting tube is provided with several connecting holes, for connecting several air guns；
The air gun is passed through and is fixed on the panel of the outer casing bottom；The altar lamp is passed through and is fixed on described outer
On the panel of shell bottom；
Fire hole and peephole are provided on the panel of the outer casing bottom；
Plug is tamped in fact using refractory fibre between refractory brick in the burner and atmospheric pressure kiln and vacuum furnace.
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 bottom of the atmospheric pressure kiln is equipped with burner, and the burner includes shell, gas collecting tube, air gun and altar lamp；
The side wall of outer shell is provided with air inlet, and the face plate center of the outer casing bottom is equipped with gas collecting tube, the gas collection
Pipe is for for air gun providing fuel gas, therefore, the gas collecting tube be mounted on the bottom panel still with the shell not
Connection；The side wall of the gas collecting tube is provided with several connecting holes, for connecting several air guns；It opens one end of the gas collecting tube
Mouth is for being passed through fuel gas.
The air gun is passed through and is fixed on the panel of the outer casing bottom, during several described air guns with gas collecting tube are
The heart, radiant type are distributed on the panel of the outer casing bottom；The air gun preferably uses hose, one embodiment of the present of invention
In, the number of the air gun is 8, and the angle between two neighboring air gun is 45 °.
The altar lamp is passed through and is fixed on the panel of the outer casing bottom；It is provided on the panel of the outer casing bottom
Fire hole and peephole；Plug is tamped in fact using refractory fibre between refractory brick in the burner and atmospheric pressure kiln.
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 overhead air cooler device is provided with temperature control adjusting valve, can effectively control atmospheric tower head temperature, effectively cut
It takes light straight run fraction oily, meets the special solvent oil that rectifying column produces 150~190 DEG C of narrow fractions.
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 decompression furnace bottom is also equipped with burner, the decompression
The burner of furnace bottom is identical as the above burner structure of normal pressure furnace bottom, and details are not described herein.The vacuum tower setting
Have subtract top 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 being discharged not
Same fraction.What the second line of distillation oil export was discharged is the easer in the present invention.
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.
The vacuum tower is internally provided with liquid distribution trough, increases reflecting plate on the secondary slot of the liquid distribution trough,
Due to the cloth liquid and guiding function of reflecting plate, realizes the linear distribution of liquid and to prevent air-flow to spray spray apertures direct
Interference, reduces liquid foam entrainment, improves yield and product quality.
In conjunction with the process units in the present invention, the production technology in the present invention is as follows:
Feedstock oil from raw material tank field is subtracted top and follows/raw material oil heat exchanger → second line of distillation/raw material oil heat exchanger → raw material
Oil strainer → feedstock oil surge tank.Raw material mixes → bis- anti-productions with new hydrogen, recycle hydrogen after raw material pump boosting in surge tank
Object/mixed raw material heat exchange → mono- anti-product/mixed raw material heat exchange → reaction heating furnace (after the reaction temperature required by being heated to →
Into hydroisomerization reactor；The anti-product of reaction product → mono-/mixed raw material heat exchanger exchanges heat → enters post-refining reactor
Carry out aromatic hydrogenation saturation.The anti-product of effluent → bis- of post-refining reactor/mixed raw material heat exchanger and two anti-products/low
After dividing oil heat exchanger heat exchange → reaction product air cooler to condense → high-pressure separator progress gas liquid separation.At the top of high-pressure separator
The hydrogen-rich gas isolated is through digester adsorbing and removing H2After S, enter recycle hydrogen pressure after going circulating hydrogen compressor liquid separation tank liquid separation
Contracting machine is recycled.The product liquid of high-pressure separator bottom carries out after fluid level control valve depressurizes into low pressure separator
Gas liquid separation.The low point of gas that low pressure separator is isolated is discharged into fuel gas pipe network, and low point of oil and two anti-products/low point of oil exchange heat
After device heat exchange, product cutting separation is carried out to fractionating section.
Low point of oil → low point of oil/first vacuum side stream heat exchanger → low point of oil that low pressure separator bottom comes out/second line of distillation heat exchange
→/→ low point of oil/subtracts base oil heat exchanger → low point of oil/to subtract low point of oil device → low point of oil/vacuum 1st side cut heat exchanger for the line heat exchanger that subtracts three
Heat exchanger → atmospheric pressure kiln → atmospheric tower in one.
Atmospheric Tower oil gas → overhead air cooler device → often pushing up water cooler → often pushes up return tank, bottom sewage → subtract top sewage pump
→ Sewage Disposal；Divide two-way after often pushing up oil → often top reflux pump extraction: a part of often top oil returns Atmospheric Tower and makees withdrawing oil
Tower top temperature is controlled, a part is sent as pure white oil plant to tank field.Normal top return tank top fixed gas → fuel gas system (or fire
Torch emptying).
Normal base oil → normal bottom pumps → removes vacuum furnace → vacuum tower.Top of Vacuum Tower oil gas → subtracting top level-one evacuation → subtracts top one
Grade evacuation condenser → subtract top water distributing can；It is cold to subtract top second level evacuation for the fixed gas phase → subtracting top second level evacuation → of level-one evacuation
Condenser condenses → subtracts top water distributing can；The fixed gas phase → subtracting top three-level evacuation → of second level evacuation subtracts top three-level and evacuates condenser
→ subtract top water distributing can；Fixed gas mutually goes after low pressure gas tank liquid separation to remove vacuum furnace low pressure fire nozzle as fuel gas.Subtract top oil → subtract
Top oil pump → subtract top tank farm.Bottom sewage → subtract top sewage pump → Sewage Disposal.
Following oil from the top that subtracts of vacuum tower, → subtract top follow oil pump → feedstock oil/subtract top follow oil heat exchanger → subtracts top and follows oily air cooler
→ subtract top and follow after grease cooler is cooled to 50 DEG C and be divided into two-way；Subtract top all the way and follow oil → vacuum tower and do top and walk around to stream, another way goes out
Device → 10# white oil tank.
II section filler oil sump tank extraction → vacuum 1st side cut stripper (upper section) of the first vacuum side stream from vacuum tower.Tower bottom is passed through stripping
Steam, gas phase return to vacuum tower.First vacuum side stream → vacuum 1st side cut oil pump → low point of oil/first vacuum side stream heat exchanger in stripper → low point
Oil/first vacuum side stream heat exchanger → vacuum 1st side cut air cooler → go out device to 32# white oil tank.
III section filler oil sump tank extraction → second line of distillation stripper (middle section) of the second line of distillation oil from vacuum tower.Tower bottom is passed through stripping
Steam, gas phase return to vacuum tower.Second line of distillation oil → second line of distillation oil pump → low point of oil/second line of distillation oil heat exchanger → raw material in stripper
Oil/second line of distillation oil heat exchanger → second line of distillation water cooler → second line of distillation water cooler (or sending to second line of distillation oil decolorization tank post-refining) →
It send to 46# white oil tank (product is easer oil).
Subtract third fractional oil and extract → line the stripper (lower section) that subtracts three from V section of filler oil sump tank of vacuum tower out, tower bottom is passed through stripping
Steam, gas phase return to vacuum tower.The third fractional oil that subtracts after stripping → subtracts third fractional oil pump →/to subtract third fractional oil heat exchanger → through low point of oil to subtract
Three line water coolers are cooling, and → the line water cooler that subtracts three (or send to subtract three line bleacher post-refining) → is sent to 68# white oil tank.
Subtract base oil → subtract bottom pump → low point/subtract base oil heat exchanger → subtracting base oil water cooler → subtract base oil water cooler (or send to
Subtract base oil bleacher post-refining) → give to 100# white oil tank.
Vacuum tower is equipped with a middle section reflux and a washing reflux.IV section filler oil sump tank of the oil from vacuum tower in subtracting one
→ subtract one in oil pump → low point of oil/oil heat exchanger → vacuum tower in subtracting one.The oily V section of filler oil sump tank from vacuum tower of washing →
Decompression washing oil pump → vacuum tower.
In order to further illustrate the present invention, with reference to embodiments to a kind of production of easer provided by the invention
Technique and process units are described in detail, but cannot be understood as limiting the scope of the present invention.
Using process units shown in Fig. 1~3, easer is produced according to the parameter in table 1.
Hydrobon catalyst is the catalyst for refining for avenging the ICR409 model that teflon provides.
The density of obtained easer solvent naphtha is 852.4kg/m3, the viscosity at 40 DEG C is 41.69mm2/S, 100
Viscosity at DEG C is 6.51mm2/S, viscosity index (VI) 106, flash-point are 242 DEG C, and pour point is -21 DEG C.
As can be seen from the above data,
1) comparative example and embodiment feedstock oil change of properties are more apparent, density by comparative example 849kg/m3It drops to
843kg/m3, the initial boiling point of feedstock oil has been increased to 360 DEG C than 330 DEG C of comparative example, and condensation point has been increased to+23 DEG C by+12 DEG C,
Viscous refer to has been increased to 115 by 108.And reaction bed is kept at 330 DEG C during calibration, illustrates that the technique in the present invention is more suitable
It closes and processes high condensation point feedstock oil；
2) compared with comparative example, low point of oily flash-point has been increased to 40 DEG C by 25 DEG C in the present embodiment, evaporation loss also by
22.7% has decreased to 21%, and illustrating in low point of oil that light component compares comparative example reduces much；
3) easer oil is in addition to density is by 859kg/m3It mentions and falls below 852kg/m3Outside, flash-point, pour point, analysis of distillation process
Xiang Jun take a favorable turn.102 before especially viscosity index (VI) has have been increased to 107；
4) energy consumption data is compared, device comprehensive energy consumption is down to the present embodiment by 33.35 kilograms of mark coal/ton raw materials of comparative example
31.46 kilograms of mark coal/tons；
5) low point of throughput of the present embodiment is about 390Nm3/ h, and low point of throughput of comparative example is 410Nm3/h。
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 (10)
1. a kind of production method of easer, comprising the following steps:
Light lubricating oil material is successively subjected to hydroisomerizing and hydrofinishing, obtained purified product carries out high-pressure gas-liquid separation and low pressure
Gas-liquid separation obtains low point of oil, and low point of obtained oil product is successively then carried out normal pressure fractionation, vacuum fractionation and stripping, is obtained
To easer；
The temperature of the hydroisomerizing is 330~340 DEG C, and the temperature of the hydrofinishing is 240~250 DEG C；
The pressure of the high-pressure gas-liquid separation is 14~15MPa；
The temperature of the normal pressure fractionation is 285~290 DEG C, and the pressure of the normal pressure fractionation is 230~240KPa；The decompression point
The temperature evaporated is 308~310 DEG C, and the pressure of the vacuum fractionation is 4~5KPa.
2. production method according to claim 1, which is characterized in that the density of the light lubricating oil material is 843g/cm3, sulphur contains
Amount is 3.3~3.4 μ g/g, and condensation point is 24 DEG C, and viscosity index (VI) 115, flash-point is 222~226 DEG C, and initial boiling point is 360 DEG C.
3. production method according to claim 1, which is characterized in that the catalyst of the hydrofinishing is snow teflon company
The catalyst of the ICR409 model of offer.
4. production method according to claim 1, which is characterized in that the pressure of the low-pressure gas-liquid separation is 1.34MPa；
The temperature of the low-pressure gas-liquid separation is 40~50 DEG C.
5. production method according to claim 1, which is characterized in that the low point of oily density is 847~849kg/m3,
Viscosity is 27~28mm2/S, viscosity index (VI) are 101~103, and flash-point is 28~30 DEG C, evaporation loss 21.1.
6. production method according to claim 1, which is characterized in that the air-blowing quantity of the vacuum tower is 0.25~0.3t/
h。
7. a kind of process units of easer, including sequentially connected raw material surge tank plus hydrogen feed heating furnace plus hydrogen is different
Structure reactor, hydrofining reactor, high-pressure separator, low pressure separator, atmospheric pressure kiln, atmospheric tower, vacuum furnace, vacuum tower and vapour
Stripper；
The bottom of the atmospheric pressure kiln and vacuum furnace is mounted on burner, and the burner includes shell, gas collecting tube, air gun and length
Bright lamp；
The side wall of outer shell is provided with air inlet, and the face plate center of the outer casing bottom is equipped with gas collecting tube；
The side wall of the gas collecting tube is provided with several connecting holes, for connecting several air guns；
The air gun is passed through and is fixed on the panel of the outer casing bottom；The altar lamp passes through and is fixed on the shell bottom
On the panel in portion；
Fire hole and peephole are provided on the panel of the outer casing bottom；
Plug is tamped in fact using refractory fibre between refractory brick in the burner and atmospheric pressure kiln and vacuum furnace.
8. process units according to claim 7, which is characterized in that the tower top of the atmospheric tower is provided with overhead air cooler
Device, the overhead air cooler device are connected with the tower top outlet of the atmospheric tower, and the outlet of the overhead air cooler device is provided with temperature control
Regulating valve.
9. process units according to claim 7, which is characterized in that be provided with liquid distribution trough, institute in the vacuum tower
It states and is arranged in parallel with reflecting plate above liquid distribution trough.
10. process units according to claim 7, which is characterized in that several described air guns are centered on gas collecting tube, spoke
The formula of penetrating is evenly distributed on the panel of the outer casing bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910689135.6A CN110272761A (en) | 2019-07-29 | 2019-07-29 | A kind of production method and process units of easer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910689135.6A CN110272761A (en) | 2019-07-29 | 2019-07-29 | A kind of production method and process units of easer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110272761A true CN110272761A (en) | 2019-09-24 |
Family
ID=67965517
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910689135.6A Pending CN110272761A (en) | 2019-07-29 | 2019-07-29 | A kind of production method and process units of easer |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110272761A (en) |
Cited By (2)
| 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 |
| CN115558522A (en) * | 2022-09-29 | 2023-01-03 | 盘锦北方沥青股份有限公司 | Operation method of reduced pressure fractionation system in naphthenic base crude oil processing |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106382629A (en) * | 2016-11-18 | 2017-02-08 | 岳阳钟鼎热工电磁科技有限公司 | Oil and gas combustor capable of realizing combustion of high-purity hydrogen fuel gas, flat flame and ultra-low NOx emission |
| 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 |
| CN210595941U (en) * | 2019-07-29 | 2020-05-22 | 海南汉地阳光石油化工有限公司 | Production device of printing ink additive |
-
2019
- 2019-07-29 CN CN201910689135.6A patent/CN110272761A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106382629A (en) * | 2016-11-18 | 2017-02-08 | 岳阳钟鼎热工电磁科技有限公司 | Oil and gas combustor capable of realizing combustion of high-purity hydrogen fuel gas, flat flame and ultra-low NOx emission |
| 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 |
| CN210595941U (en) * | 2019-07-29 | 2020-05-22 | 海南汉地阳光石油化工有限公司 | Production device of printing ink additive |
Non-Patent Citations (4)
| Title |
|---|
| 刘武辉: "现代印刷材料", 30 September 2007, pages: 149 * |
| 张剑波等: "清洗技术基础教程", 31 July 2004, pages: 86 - 87 * |
| 董大清等: "加氢裂化尾油生产食品级白油的研究", pages 197 - 199 * |
| 邓勇等: "工业装备学", 30 June 2017, pages: 128 - 136 * |
Cited By (3)
| 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 |
| 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 |
| CN115558522A (en) * | 2022-09-29 | 2023-01-03 | 盘锦北方沥青股份有限公司 | Operation method of reduced pressure fractionation system in naphthenic base crude oil processing |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU762235B2 (en) | Intergrated deethanizer/ethylene fractionation column | |
| CN101475819B (en) | Two-tower type pressure reducing coke tar distillation process and apparatus therefor | |
| CN101376068A (en) | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer | |
| CN102351627A (en) | Process method for extracting normal hexane and isohexane from crude hexane | |
| CN102234541B (en) | Energy-saving pyrolysis gasoline full-cut hydrogenation method and device | |
| CN107177373B (en) | A kind of overcritical residual oil and/or catalytic slurry processing system and processing method | |
| CN110272761A (en) | A kind of production method and process units of easer | |
| CN112410068A (en) | Wax oil hydrocracking device and method for producing 5# industrial white oil by using same | |
| CN101020846A (en) | Coal tar hydrogenating process with high diesel oil output | |
| CN109762590B (en) | Fractionation system and fractionation method | |
| CN101575533A (en) | Improved method for preparing fuel oil by coal tar hydrogenation | |
| CN103484159B (en) | Matching technology method for optimizing feeding of coal tar suspended bed hydrocracker | |
| CN109022032B (en) | Method for recovering waste mineral oil by hydrogenation | |
| CN214088414U (en) | Wax oil hydrocracking unit | |
| CN202246472U (en) | Device for extracting normal hexane and isohexane from crude hexane | |
| CN201686667U (en) | Cracking gasoline full-fraction hydrogenation device | |
| CN210595941U (en) | Production device of printing ink additive | |
| CN107177372A (en) | The suspended bed hydrogenation method and hydrogenation system of heavy oil feedstock | |
| CN101294104B (en) | Hydrocracking recycle hydrogen deoiling, dewatering separation method and apparatus | |
| CN103608430B (en) | Prepare the technique of diesel oil distillate | |
| CN202576341U (en) | Three-tower atmospheric and vacuum tar distillation unit | |
| CN111377801A (en) | Method and system for refining low carbon alcohol | |
| CN107794076B (en) | Method and device for separating refined mixed aromatic hydrocarbon containing hydrogen sulfide | |
| CN210595940U (en) | Heat conduction oil processing device | |
| SU1648961A1 (en) | Process for petroleum refining |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |