CN106281462A - A kind of hydrorefining paraffin wax technique - Google Patents

A kind of hydrorefining paraffin wax technique Download PDF

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Publication number
CN106281462A
CN106281462A CN201610666590.0A CN201610666590A CN106281462A CN 106281462 A CN106281462 A CN 106281462A CN 201610666590 A CN201610666590 A CN 201610666590A CN 106281462 A CN106281462 A CN 106281462A
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fixed bed
mcm
bed reactors
molybdenum
paraffin
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朱忠良
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Xishan Lvchun Plastic Products Factory
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Xishan Lvchun Plastic Products Factory
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    • 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
    • C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
    • C10G73/42—Refining of petroleum waxes
    • C10G73/44—Refining of petroleum waxes in the presence of hydrogen or hydrogen-generating compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/03—Catalysts comprising molecular sieves not having base-exchange properties
    • B01J29/0308—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41
    • B01J29/0341—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/041—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41
    • B01J29/045—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • B01J2229/183—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself in framework positions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1081—Alkanes
    • C10G2300/1085—Solid paraffins
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Dispersion Chemistry (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention discloses a kind of hydrorefining paraffin wax technique, described technique uses fixed bed reactors, is filled with hydrogenation desulfurization and denitrogenation catalyst in fixed bed reactors, and described catalyst includes carrier and active component；Described carrier is incorporation hetero atom Cu in synthetic bone shelf structure2+MCM 41；Described active component is nitridation two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and the mixture of tungsten carbide wc；The reaction condition of described fixed bed reactors is: reaction temperature is 250 300 DEG C, and hydrogen dividing potential drop is 2.8 3.6MPa, hydrogen wax volume ratio 150 300, volume space velocity 0.6 2.0h‑1.Paraffin total sulfur content can be controlled, less than 5ppm, to control the total nitrogen content in paraffin within 10ppm by this technique simultaneously.

Description

A kind of hydrorefining paraffin wax technique
Technical field
The present invention relates to wax hydrofining desulfuration purification technique, be specifically related to a kind of paraffin using special catalyst to carry out and add Hydrogen process for refining.
Background technology
Paraffin is the one of refinery products, is through solvent refining, solvent from the lube cut of crude distillation gained Dewaxing or prepare slack wax through wax freezing and crystallizing, squeezing dewaxing, then through solvent deoiling, refined obtained by lamellar or acicular crystal.
Paraffin is divided into the big class such as food wax, paraffin wax fully refined, semi-refined paraffin wax, waxy stone, match wax and black wax.Paraffin is divided into Many grades are sold, and the main distinction is that fusing point is different.According to the difference of purposes, different to the prescription of paraffin.Due to from The waxy stone of oil contains numerous impurity such as sulfur, and therefore it can not use directly as product, needs through process for refining, to protect Holding the deep refining realizing product while the characteristic index such as the fusing point of product, oil content, needle penetration are basically unchanged, refined is deep Degree should meet following requirement: is 1. hydrogenated with by the non-hydrocarbons of sulfur, nitrogen, oxygen, removes sulfur therein, nitrogen and oxygen；2. by alkene, Aromatic hydrocarbons particularly condensed-nuclei aromatics hydrogenation is saturated；3. reduce the cracking reaction occurring C-C bond fission to generate little molecule, it is to avoid add as far as possible Hydrogen oil content in paraffin wax increases.
And in numerous paraffin process for refining, hydrorefining paraffin wax technique can keep feedstock skeleton knot due to it In the case of structure does not changes or varies less, by impurity removal, reach to change the purpose that oil product has been eaten, therefore obtain wide General application.By the end of 2005, the designed capacity of the hydrorefining paraffin wax process units of the domestic normal operation of China was close 1.3Mt/a, wherein single covering device maximum processing capacity is 150kt/a.
Along with heaviness, the in poor quality of world's crude oil are deepened day by day, crude oil sulfur content is more and more higher, and the lightweight of high-quality is former Oil is constantly reducing.The crude oil of refinery's processing in recent years mostly is imported crude oil, and relative density increases year by year, in several years of the beginning of this century The average density of whole world refinery processing crude oil rises to about 0.8633.The problem that sulfur content is high is the most extremely serious, the current world The yield of upper sour crude oil and sour crude accounts for more than the 75% of world's crude oil total output.20th century the mid-90 whole world refinery The crude oil average sulfur content of processing is 0.9%, and the beginning of this century has increased to 1.6%.
Current hydrorefining paraffin wax technique, similar with fraction oil hydrogenation refining, generally comprise pretreatment of raw material, hydrogenation instead Answer and product post processing three parts.Paraffin typically through pretreatment such as filtration, degassings, the impurity that carries in removing raw material, The gaseous oxygen etc. of minor amount of water, solvent and dissolving, then mix with hydrogen, heat entrance reactor, carry out hydrofining reaction.Reaction Product carries out gas-liquid separation respectively in high pressure and low pressure separator, then through stripping, being dried and be filtrated to get finished product wax.
But existing hydrorefining paraffin wax technique is all to arrange for former high-quality edible vegetable oil.For current high-sulfur The paraffin that content crude oil production obtains, owing to its high sulfur content, its catalyst used and hydroconversion condition are all difficult to be suitable for.
The most how paraffin process for refining is provided, can effectively the sulfur content in the starting paraffin of high sulfur content be controlled Below 10ppm, to meet standard, is a difficult problem facing of this area.
Summary of the invention
It is an object of the invention to propose a kind of wax hydrofining desulfuration purification technique, this technique can be by the total sulfur in paraffin Content is reduced to below 10ppm, with satisfied discharge and Corrosion standards.
For reaching this purpose, the present invention by the following technical solutions:
A kind of hydrorefining paraffin wax technique, described technique uses fixed bed reactors, is filled with and adds in fixed bed reactors Hydrogen catalyst, described catalyst includes carrier and active component.
Described carrier is incorporation hetero atom Cu in synthetic bone shelf structure2+MCM-41.
Described active component is nitridation two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and the mixture of tungsten carbide wc.
The reaction condition of described fixed bed reactors is: reaction temperature is 250-300 DEG C, and hydrogen dividing potential drop is 2.8-3.6MPa, Hydrogen wax volume ratio 150-300, volume space velocity 0.6-2.0h-1。
MCM-41 is ordered into mesoporous material, and its duct is that six side's ordered arrangement, size are uniform, aperture size can with synthesis time The difference adding directed agents and synthetic parts changes between 1.5～10nm, lattice parameter about 4.5nm, specific pore volume about 1mL/g, MCM-41 uniform pore diameter, has higher specific surface area (1000m2/ g) and big adsorption capacity (0.7mL/g), the most organic The free diffusing of molecule.The present invention through in numerous mesoporous materials, such as MCM-22, MCM-36, MCM-48, MCM-49, MCM56, carries out contrast test selection, finds that only MCM-41 can reach the goal of the invention of the present invention, and other mesoporous materials are all Having such-and-such defect, there is the technical difficulty being difficult to overcome when being applied in the present invention, therefore the present invention selects to use MCM-41 is as carrier basis.
The acidity of silica MCM-41 own is the most weak, is directly used as catalyst activity relatively low.Therefore, it is changed by the present invention Property, to increase its catalysis activity.The approach that MCM-41 mesopore molecular sieve is modified is by the present invention: be situated between to the Siliceous MCM-41 of finished product Porous molecular sieve inner surfaces of pores introduces Cu2+, this approach can be exchanged Cu by ion2+It is supported on the inner surface of MCM-41, Thus improve catalysis activity, absorption and the Thermodynamically stable performance etc. of MCM-41 mesopore molecular sieve on the whole.
Although the method being modified MCM-41 mesopore molecular sieve or approach are a lot, inventor finds, the present invention urges Agent can only use doping Cu2+MCM-41 could realize sulfur content control and denitrification effect as carrier, inventor attempts MCM-41 adulterates: Al3+、Fe3+、Zn2+、Ga3+In the ion at generation anionic surface center, discovery all can not realize described Effect.Although described mechanism is current and unclear, but this has no effect on the enforcement of the present invention, and inventor is according to well-known theory and reality Checking is real, there is cooperative effect between itself and the active component of the present invention.
Described Cu2+Doping in MCM-41 must control within specific content range, and its doping is with weight Meter, for the 0.56%-0.75% of MCM-41 weight, such as 0.57%, 0.58%, 0.59%, 0.6%, 0.61%, 0.62%, 0.63%, 0.64%, 0.65%, 0.66%, 0.67%, 0.68%, 0.69%, 0.7%, 0.71%, 0.72%, 0.73%, 0.74 etc..
Inventor finds, outside this range, can cause drastically reducing of paraffin desulfurized effect.It is more pleasurable, Work as Cu2+When doping in MCM-41 controls in the range of 0.63%-0.72%, its desulphurizing ability is the strongest, when drawing with Cu2 +Doping is transverse axis, and during curve chart with target desulfurized effect as the longitudinal axis, in this content range, sulfur content can control extremely low Within the scope of, its desulfurized effect produced, far beyond expection, belongs to unforeseeable technique effect.
The total content of described active component is the 1%-15% of carrier MCM-41 weight, preferably 3-12%, further preferably 5-10%.Such as, described content can be 2%, 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, 5.5%, 6%, 6.5%, 7%, 7.5%, 8%, 8.5%, 9%, 9.5%, 10%, 10.5%, 11%, 11.5%, 12%, 12.5%, 13%, 13.5%, 14%, 14.5% etc..
In the present invention, it is particularly limited to active component for nitridation two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide wc Mixed proportion, inventor find, the effect that different mixed proportions reaches is entirely different.Inventor finds, nitrogenizes two molybdenums MO2N, tungsten nitride W2N, molybdenum carbide Mo2The mixed proportion (mol ratio) of C and tungsten carbide wc is 1:(0.4-0.6): (0.28- 0.45): (0.8-1.2), nitridation two molybdenum MO are only controlled2N, tungsten nitride W2N, molybdenum carbide Mo2The mol ratio of C and tungsten carbide wc exists In the range of Gai, sulfur content in paraffin can be realized and control at below 10ppm and denitrification ability notable.It is to say, the present invention Four kinds of active components be only 1:(0.4-0.6 in mol ratio): (0.28-0.45): time (0.8-1.2), just possess collaborative effect Should.Outside this molar ratio range, or omit or replace any one component, all can not realize cooperative effect.
Preferably, two molybdenum MO are nitrogenized2N, tungsten nitride W2N, molybdenum carbide Mo2The mol ratio of C and tungsten carbide wc is 1:(0.45- 0.5): (0.35-0.45): (0.8-1.0), more preferably 1:(0.45-0.48): (0.4-0.45): (0.9-1.0), Preferably 1:0.48:0.42:0.95.
The preparation method of described catalyst can take infusion process and other alternative methods, the people in the art of routine The prior art unrestricted choice that member can grasp according to it, the present invention repeats no more.
Preferably, the reaction condition of described fixed bed reactors is: reaction temperature is 260-280 DEG C, and hydrogen dividing potential drop is 2.8- 3.0MPa, hydrogen wax volume ratio 150-200, volume space velocity 1.0-1.5h-1。
Preferably, described technological process includes, raw material, after filter, surge tank, is pumped into heat exchanger by feed pump and become Product heat exchange, is mixed to form hydrogen wax mixture, again enters heating furnace with after product heat exchange with recycle hydrogen and new hydrogen after heat exchange, Being heated to reaction temperature and enter hydrofining reactor (fixed bed reactors), hydrogen wax mixture is made at catalyst in the reactor Under with, the reaction such as carry out that hydrodesulfurization, denitrogenation, deoxidation, alkene is saturated and aromatic hydrocarbons is saturated, product is through heat exchange more water cooled To predetermined temperature, entering high-pressure separator, high-pressure separator top gas phase returns recycle hydrogen surge tank as recycle hydrogen, and oil phase enters Entering low pressure separator, the generation oil drawn bottom low pressure separator enters stripper, tower top oil gas warp after product heat exchange Entering separatory tank after air cooling, water-cooled and obtain Petroleum, stripping tower bottom obtains paraffin.
Preferably, described fixed bed reactors include 1-5 beds, further preferred 2-3 beds.
The hydrofining technology of the present invention is by choosing specific catalyst, and described catalyst is by mixing hetero atom Cu2+ MCM-41 as carrier, and choose the nitridation two molybdenum MO of special ratios2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide wc As active component so that this catalyst produces cooperative effect, and the hydrodesulfurization to paraffin can control to be less than at total sulfur content 5ppm, controls within 10ppm the total nitrogen content in paraffin simultaneously.
Detailed description of the invention
The hydrofining technology of the present invention is illustrated by the present invention by following embodiment.
Embodiment 1
Preparing catalyst by infusion process, carrier is doping Cu2+MCM-41, Cu2+Doping in MCM-41 Control at the 0.65% of carrier quality.Described active component nitrogenizes two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide wc Total content is carrier quality 10%, its mol ratio is 1:0.4:0.3:0.8.
Described Catalyst packing enters fixed bed reactors, and the reaction tube of described reactor is by the stainless steel of internal diameter 50mm Becoming, beds is set to 3 layers, and reaction bed temperature UGU808 type temp controlled meter is measured, and raw material paraffin is by Bei Jingwei The double plunger micro pump of star maker manufacture carries continuously, and hydrogen is supplied and use Beijing Sevenstar-HC D07-11A/ by gas cylinder ZM mass-flow gas meter coutroi velocity, loaded catalyst is 2kg.Reacted product cools down laggard circulation of qi promoting through water-bath room temperature Liquid separates.
Raw materials used for paraffin, its total sulfur content 561ppm, basic n content is 258ppm.
Controlling reaction condition is: temperature 270 DEG C, hydrogen dividing potential drop 3.0MPa, hydrogen wax volume ratio 200, volume space velocity 1.5h-1。
Testing final product, total sulfur content is reduced to 5ppm, and total alkaline nitrogen content is reduced to 9ppm.
Embodiment 2
Preparing catalyst by infusion process, carrier is doping Cu2+MCM-41, Cu2+Doping in MCM-41 Control at the 0.7% of carrier quality.Described active component nitrogenizes two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide wc Total content is carrier quality 10%, its mol ratio is 1:0.6:0.45): 1.2.
Remaining condition is same as in Example 1.
Testing final product, total sulfur content is reduced to 4ppm, and total alkaline nitrogen content is reduced to 9ppm.
Comparative example 1
The carrier of embodiment 1 is replaced with γ-Al2O3, remaining condition is constant.
Testing final product, total sulfur content is reduced to 36ppm, and total alkaline nitrogen content is reduced to 31ppm.
Comparative example 2
The carrier of embodiment 1 is replaced with unadulterated MCM-41, and remaining condition is constant.
Testing final product, total sulfur content is reduced to 31ppm, and total alkaline nitrogen content is reduced to 20ppm.
Comparative example 3
Cu by embodiment 12+Replace with Zn2+, remaining condition is constant.
Testing final product, total sulfur content is reduced to 37ppm, and total alkaline nitrogen content is reduced to 25ppm.
Comparative example 4
By the Cu in embodiment 12+Doping in MCM-41 controls at the 0.5% of carrier quality, and remaining condition is constant.
Testing final product, total sulfur content is reduced to 27ppm, and total alkaline nitrogen content is reduced to 32ppm.
Comparative example 5
By the Cu in embodiment 12+Doping in MCM-41 controls at the 0.8% of carrier quality, and remaining condition is constant.
Testing final product, total sulfur content is reduced to 26ppm, and total alkaline nitrogen content is reduced to 24ppm.
Embodiment 1 shows with comparative example 1-5, certain content scope that the application uses and certain loads metal ion MCM-41 carrier, when replacing with other known carriers of this area, or carrier is identical but Cu2+During doping difference, all reach Less than the technique effect of the present invention, the therefore Cu of the certain content scope of the present invention2+Doping MCM-41 carrier and catalyst other Possessing cooperative effect between component, described hydrofining technology creates unforeseeable technique effect.
Comparative example 6
Omit the MO in embodiment 12N, remaining condition is constant.
Testing final product, total sulfur content is reduced to 34ppm, and total alkaline nitrogen content is reduced to 41ppm.
Comparative example 7
Omitting the WC in embodiment 1, remaining condition is constant.
Testing final product, total sulfur content is reduced to 33ppm, and total alkaline nitrogen content is reduced to 22ppm.
Above-described embodiment and comparative example 6-7 explanation, several active component of catalyst of the hydrofining technology of the present invention it Between there is specific contact, be omitted or substituted one of which or several, all can not reach the certain effects of the application, it was demonstrated that it produces Give birth to cooperative effect.
Applicant states, the present invention illustrates the technique of the present invention by above-described embodiment, but the invention is not limited in Above-mentioned technique, does not i.e. mean that the present invention has to rely on above-mentioned detailed catalysts and could implement.Those of skill in the art Member is it will be clearly understood that any improvement in the present invention, and the equivalence of raw material each to product of the present invention is replaced and the interpolation of auxiliary element, tool Body way choice etc., within the scope of all falling within protection scope of the present invention and disclosure.

Claims (6)

1. a hydrorefining paraffin wax technique, described technique uses fixed bed reactors, is filled with hydrogenation in fixed bed reactors Catalyst, described catalyst includes carrier and active component, it is characterised in that
Described carrier is incorporation hetero atom Cu in synthetic bone shelf structure2+MCM-41,
Described active component is nitridation two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and the mixture of tungsten carbide wc,
The reaction condition of described fixed bed reactors is: reaction temperature is 250-300 DEG C, and hydrogen dividing potential drop is 2.8-3.6MPa, hydrogen wax Volume ratio 150-300, volume space velocity 0.6-2.0h-1。
2. hydrofining technology as claimed in claim 1, it is characterised in that hetero atom Cu2+Doping be MCM-41 weight 0.63%-0.72%.
3. hydrofining technology as claimed in claim 1, it is characterised in that the total content of described active component is carrier MCM- The 3-12% of 41 weight, preferably 5-10%.
4. hydrofining technology as claimed in claim 1, it is characterised in that nitrogenize two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2The mol ratio of C and tungsten carbide wc is 1:(0.45-0.5): (0.35-0.45): (0.8-1.0), more preferably 1: (0.45-0.48): (0.4-0.45): (0.9-1.0), most preferably 1:0.48:0.42:0.95.
5. hydrofining technology as claimed in claim 1, it is characterised in that the reaction condition of described fixed bed reactors is: Reaction temperature is that reaction temperature is 260-280 DEG C, and hydrogen dividing potential drop is 2.8-3.0MPa, hydrogen wax volume ratio 150-200, volume space velocity 1.0-1.5h-1。
6. hydrofining technology as claimed in claim 1, it is characterised in that described fixed bed reactors include 1-5 catalysis Agent bed, preferably includes 2-3 beds.
CN201610666590.0A 2016-08-12 2016-08-12 A kind of hydrorefining paraffin wax technique Pending CN106281462A (en)

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