CN107304376A - A kind of reformed oil liquid-phase hydrogenatin processing method - Google Patents
A kind of reformed oil liquid-phase hydrogenatin processing method Download PDFInfo
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- CN107304376A CN107304376A CN201610252807.3A CN201610252807A CN107304376A CN 107304376 A CN107304376 A CN 107304376A CN 201610252807 A CN201610252807 A CN 201610252807A CN 107304376 A CN107304376 A CN 107304376A
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- depentanizer
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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
- 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
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
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- Oil, Petroleum & Natural Gas (AREA)
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- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of reformed oil liquid-phase hydrogenatin processing method, reformed oil is subjected to hydrotreating before depentanizer is entered, hydrotreating uses liquid-phase hydrogenatin treatment technology, when setting cross-line is isolated for hydrotreating systems with reformer system, reformed oil is introduced directly into depentanizer；Leakproof pipeline is set, and leakproof pipeline one end is connected with cross-line, and the other end is connected with depentanizer bottoming cycle pump discharge pipeline.The inventive method can effectively solve that product that cross-line valves leakage causes is unqualified or the problem of device shortens service cycle.
Description
Technical field
The present invention relates to a kind of reformed oil liquid-phase hydrogenatin processing method, specifically reformed oil is post-processed
Unit is incorporated into reformer, is particularly suitable for producing the reformer of aromatic hydrocarbons.
Background technology
Catalytic reforming（Catalytic Reforming）It is one of petroleum refining significant process.It is in higher temperature, low
Press and face under hydrogen state, in the presence of noble metal catalyst, naphtha is transformed into the reformed oil rich in aromatic hydrocarbons
Process.Reformed oil can be directly used as the blend component of motor petrol, and benzene, toluene and diformazan can be also produced through Aromatics Extractive Project
Benzene, while the hydrogen of by-product.
Since being gone into operation from first set hydroforming process device in 1940, catalytic reforming process is so far after nearly more than 70 years
Development course, with the demand of market and human lives to fuel and aromatic hydrocarbons, many countries are all continuous to catalytic reforming process
R and D are carried out.
In recent years, continuing to develop with reforming catalyst and catalytic reforming process, in addition new-type heat exchanger, many streams connection
The introducing of the high-efficiency appliance such as heating furnace is closed, technological process is improved, reduce the pressure drop for facing hydrogen system, catalytic reforming faces hydrogen
Pressure is greatly reduced；In reduction energy consumption simultaneously, product yield has also obtained further raising.But because reformer is anti-
The reduction of pressure is answered, reaction severity is further improved, causes ethylenic unsaturation hydrocarbon content in reformed oil to increase, sternly
Ghost image rings follow-up aromatic extraction unit stable operation and product quality.Therefore, reformed oil is before Aromatics Extractive Project part is entered
Need to be pre-processed, to ensure that olefin(e) centent therein meets requirement of the extraction unit to raw material.At this stage, reformed oil
Deolefination mainly has two methods, clay-filtered technique and hydrofining technology.Due to there is refining effect in clay-filtered technique
The problems such as difference, fast deactivation rate and serious environmental pollution, process for refining it has been hydrogenated gradually and has been replaced.
In recent years, the related of technology of alkene is reported in external existing selective hydrogenation and removing reformed oil（Method
State IFP Arofining techniques）.Using the benzene fraction of reformed oil as raw material, using noble metal catalyst, comparing mitigation
Under conditions of removing raw material in alkene.The domestic oily selective hydrogenation and olefin hydrocarbon removal technology of catalytic reforming generation is also opened in oil refining enterprise
Beginning is progressively applied.
China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute develops to be carried out using noble metal catalyst
The oily selective hydrogenation and olefin hydrocarbon removal technology of catalytic reforming generation（FHDO）.The technology is from 2003 first in Maoming Petrochemical branch company
Since being applied successfully on benzene fraction hydrogenation and olefin hydrocarbon removal device, realized in succession in the BTX cuts of Yanshan Mountain branch company, Chang Ling branch company
Commercial Application, also successfully realizes commercial Application in 2009 on the full cut of Zhenghai refinery reformed oil.Current reformation generation
Oily selective hydrogenation and olefin hydrocarbon removal commercial plant, provided with the dynamic equipment such as raw material pump, make-up hydrogen compressor, circulating hydrogen compressor, device hydrogen
Gas circulate operation, is a set of independent unit, and it is higher to there is energy consumption, and the problem of investment and operating cost are higher have impact on enterprise
Economic benefit.
CN103666544A discloses a kind of recapitalization generating oil hydrogenation processing method.This method is in liquid-phase hydrogenatin treatment conditions
Under, reformed oil is contacted with the catalyst with catalytic hydrogenation in hydrogenation reactor, weight is taken full advantage of
Alkene in dissolved hydrogen in whole generation oil, removing reformed oil, while also eliminating for recycle hydrogen and its recycle unit
Demand.Although this method technological process is simpler, still need newly-built a set of hydrogenation plant, operating cost with this method ratio
Also it is of a relatively high.
CN102911721A discloses a kind of method of reformed oil liquid phase circulation selective hydrogenation and olefin hydrocarbon removal.In pipeline
Middle progress hydrogen saturation, forms a kind of liquid phase mixture of raw material/hydrogenation products/hydrogen, under hydroconversion condition, liquid phase mixture point
Section enters multistage conventional hydro reactor；Segmentation enters beds area and reacted, the reaction come out from reactor bottom
Product section circulation afterwards is mixed with fresh feed, and follow-up separator is partly discharged from reaction system.This method technique stream
Journey is different with this method, is to be fed from reactor top, and is also a set of independent hydrogenation plant, investment and operating cost phase
To also higher.
In the technology of recapitalization generating oil hydrogenation processing, in the start-up process of hydrogenation plant, due to reaction condition and catalysis
The state that agent performance is not up to needed for reaction, therefore hydrogenation products are typically up to less than quality index, to follow-up Aromatics Extractive Project dress
Put influence larger.
The content of the invention
In view of the shortcomings of the prior art, the invention provides a kind of recapitalization generating oil hydrogenation processing method, by hydrotreating
Device is optimized with reformer and combined, and can not only be met olefin(e) centent after recapitalization generating oil hydrogenation and be met extracting requirement,
And investment, energy consumption, operating cost are greatly lowered compared with existing apparatus, are gone into operation while solving hydrogenation plant caused by initial stage
Product quality problem not up to standard.
The reformed oil liquid-phase hydrogenatin processing method of the present invention includes following content：Reformed oil is being entered de- penta
The hydrotreating systems that advance into of alkane tower carry out hydrotreating, and hydrotreating systems are included at mixed dissolution hydrogen device and hydrogenation
Reactor is managed, hydrotreating uses liquid-phase hydrogenatin treatment technology, including reformed oil to enter mixed dissolution hydrogen by temperature raising
Enter hydrotreating reactor after device, with hydrogen mixed dissolution, in hydrotreating reactor, reformed oil is at least partly
Remain and Hydrobon catalyst is used in liquid phase state, hydrotreating reactor, hydrotreating reaction effluent is directly entered
Depentanizer carries out fractionation processing；Main innovation technology is：Cross-line is set to be used for hydrotreating systems and reformer system
During isolation, reformed oil is introduced directly into depentanizer, cross-line is to be arranged on mixed dissolution hydrogen device suction line with taking off
Connecting pipeline between pentanizer suction line；Leakproof pipeline is set, and leakproof pipeline one end is connected with cross-line, the other end and de- penta
Alkane bottom of towe circulating-pump outlet pipeline is connected, and valve is set on leakproof pipeline；Cross-line and the cross-line both sides of leakproof pipeline communicating position
At least provided with one of valve；During normal operation, cross-line and every side of the cross-line both sides of leakproof pipeline communicating position are at least closed
The valve closed on one of valve, leakproof pipeline is in open mode, prevents reformed oil from leaking to depentanizer through cross-line.
In the present invention, it is preferably provided with connecting pipeline of the materials at bottom of tower with hydrogenation reactor entrance of depentanizer, in hydrogenation
When reactor goes into operation, hydrogenation reactor first introduces the materials at bottom of tower of depentanizer, after 5 minutes~24 hours, and preferably 1~10
Hour, stop introducing the materials at bottom of tower of depentanizer, reformed oil is introduced into hydrogenation reactor, carry out normal hydrotreating
Course of reaction.
In the inventive method, hydrogenation reactor is arranged on again between contact tower and depentanizer of reformer, if weight
Contain dechlorination tank in engagement positions, be then arranged between dechlorination tank and depentanizer.Contact tower again（Or dechlorination tank）The reformation of discharge
Generation oil carries out fully dissolving in air and liquid mixer after heat exchanger, with hydrogen and mixed, subsequently into hydrogenation reactor.Plus
Hydrogen reactor is entered in reactor using up flow type mode of operation, i.e. reaction mass from hydrogenation reactor bottom carries out the de- alkene of hydrogenation
Hydrocarbon reaction, after refined oil is by depentanizer, can be directly entered extraction unit.Hydrogenation reactor can also use downflow operation
Mode, i.e. reaction mass enter from the top of hydrogenation reactor carries out hydrogenation and olefin hydrocarbon removal reaction in reactor.Hydrogenation reactor is used
Liquid phase reactor state, i.e., at reaction conditions, at least part reformed oil are liquid phase state.The bottom of towe arranging thing of depentanizer
Material conveying device, hydrogenation reactor entrance is delivered to by device for transporting objects by the material that depentanizer bottom of towe is exported.De- penta
Alkane tower typically sets tower bottom reboiler to provide thermal source for depentanizer, and the depentanizer materials at bottom of tower for introducing hydrogenation plant can be
Draw, can also be drawn after tower bottom reboiler before tower bottom reboiler.Depentanizer bottoms is introduced in hydrogenation reactor
The volume space velocity of material is arbitrary, as long as fully wetting hydrogenation catalyst, generally 0.05 h-1~50.0h-1, according to just
The ability of normal device for transporting objects is preferably 0.5 h-1~10. 0h-1.Can be with dissolved hydrogen during introducing depentanizer materials at bottom of tower
Gas, can also not dissolve hydrogen, preferably by hydrogen to oil volume ratio 2：1~5：1 dissolving hydrogen.Introduced in the materials at bottom of tower of depentanizer
In the start-up process of hydrogenation reactor, reformed oil is introduced directly into depentanizer, or draws after Clay Refining Unit is refined
Enter depentanizer.When hydrogenation reactor goes into operation, the part or all of introducing hydrogenation reactor of the materials at bottom of tower of depentanizer.
In the inventive method, mixed dissolution hydrogen device is set before hydrogenation reactor is entered, for by hydrogen and reformation
Generation oil carries out being sufficiently mixed dissolving.Mixed dissolution hydrogen device can be static mixer or dynamic mixer.Static mixing
Device can be quiet selected from SV types static mixer, SK types static mixer, SX types static mixer, SH types static mixer, SL types
One or several kinds of combinations in state blender, dynamic mixer can be selected from mixing pump, overcritical blender, mixer
Middle one or several kinds of combinations.
Reformed oil in the inventive method can be the full cut of reformed oil, can also pass through reformed oil
Benzene fraction or BTX cuts.
In the inventive method, hydroprocessing operations condition and catalyst are also close with prior art.As reaction pressure
For the MPa of 0.5 MPa ~ 6.0, the MPa of preferably 1.2 MPa ~ 3.0, reaction pressure is according to contact tower again（Or dechlorination tank）Pressure
It is determined that, regulation is typically not required to, can also suitably be adjusted as needed；Reaction temperature be 100 DEG C ~ 200 DEG C, preferably 120
℃~170℃；Volume space velocity is 1.0 h-1~10. 0h-1, preferably 2.0 h-1~6.0 h-1；Hydrogen oil body before into air and liquid mixer
Product is than being 0 ~ 20：1（Due to the hydrogen containing dissolving in reformed oil, therefore it can be 0 to introduce the hydrogen of air and liquid mixer）,
Preferably 2：1~5：1.In the inventive method, hydrogen to oil volume ratio can be reduced substantially compared with existing conventional method.Above-mentioned anti-
Under the conditions of answering, by calculating, reformed oil at least 80%（Quality）Liquid phase state is kept, under preferred reaction conditions, life is reformed
Into oil at least 90%（Quality）Keep liquid phase state.
In the inventive method, the Hydrobon catalyst used can be commodity Hydrobon catalyst, such as with noble metal
Or the Hydrobon catalyst that reduced state nickel is active component, such catalyst, can be mutually with higher hydrogenation activity
Hydrogenation reaction is carried out at relatively low temperature.It is preferred to use the Hydrobon catalyst using middle noble metal as active component, such as Fushun
The HDO-18 catalyst of Petroleum Chemical Engineering Institute's development and production.Noble metal hydrogenation catalyst for refining is general using aluminum oxide as carrier,
Using Pt and/or Pd as active component, the content of active component by weight in the catalyst be not less than 0.1%, generally 0.1%~
1.5%.For the Hydrobon catalyst using reduced state nickel as active component, typically using aluminum oxide or modified aluminas as carrier,
Using nickel oxide as active component（The 15%~70% of catalyst weight, preferably 25%~45% are accounted in terms of nickel oxide weight）,
Reduction activation is being carried out to catalyst using preceding, nickel oxide reduction-state is being converted into, to improve catalyst hydrogenation activity.Counterweight
For whole generation oil distillate raw material, using the Hydrobon catalyst reformed oil bromine index can be made to be less than 100mgBr/
100g, and aromatic hydrocarbons loss is less than 0.5%, meets the charging index request of follow-up aromatic extraction unit.
In recapitalization generating oil hydrogenation processing procedure, the bromine index of reformed oil is higher, can typically reach it is thousands of even
Up to ten thousand, for the reformer that severity is larger, the bromine index of reformed oil is higher.Therefore, if cross-line valve is slightly interior
Leakage, will result in that product bromine index is unqualified, and valves leakage be it is relatively universal, more difficult find, be difficult to the problem effected a radical cure completely, such as
Fruit is intended to thoroughly solve valves leakage, need to pay higher cost.In the present invention, ingenious use leakproof pipeline designs, with reference to the device
Actual features, i.e. depentanizer bottoming cycle pump discharge pressure is more slightly higher than cross-line pressure, introduces after leakproof pipeline, in leakproof pipeline
Pressure in a little higher than cross-line of liquid phase pressure, in this state, even if the slightly interior leakage of valve on cross-line, is also thing in leakproof pipeline
Material leaks into hydrogenation reactor or leaks into depentanizer because in leakproof pipeline material be by hydrotreating, its
Bromine index is qualified, therefore leakage does not influence final products property in which kind of, ingenious to solve product caused by valves leakage and do not conform to
Lattice problem.The inventive method is skillfully constructed, it is easy to accomplish, maintenance cost is low, is conducive to device long period steady running.
The inventive method takes full advantage of and connect again on the premise of pressure needed for meeting system pressure balance and hydrogenation reaction
Tower top hydrogen is touched as raw hydrogen, is sufficiently mixed with bottom of towe feedstock oil in air and liquid mixer from reactor lower part and enters liquid phase
Hydrogenation and olefin hydrocarbon removal reactor, simplifies technological process, reduces cost of investment.Simultaneously when hydrogenation plant goes into operation, one is first introduced
The depentanizer bottom of towe oil of section time, the optimum state for making hydrogenation reactor and hydrogenation catalyst be rapidly achieved needed for reaction, no
Not the problem of hydrogenation reaction product does not reach index when can cause the device to go into operation.This method makes this process have preferably flexibly
Property, the normal operation of subsequent extraction device will not be influenceed because of this process.
Brief description of the drawings
Fig. 1 is a kind of idiographic flow schematic diagram of the inventive method.Wherein：1- reformation stabilizer base oils, 2- heat exchangers, 3- is again
Contact tower, 4- valves, 5- contacts tower top hydrogen-rich gas, 6- air and liquid mixers, 7- heat exchangers, 8- hydrogenation reactors, 9- hydrogenation again
Reactor outlet pipeline, 10- depentanizers, 11- depentanizers bottom pump, 12- depentanizers bottom reboiler, 13- valves, 14- valves
Door, 15- cross-line valve A, 16- depentanizer base oils, 17- pentane admixtures, 18- cross-line valve B, 19- leakproof pipelines, 20- across
Line.
Embodiment
The inventive method is described in detail with specific embodiment below in conjunction with the accompanying drawings.
New device for using the inventive method, as shown in Figure 1：Hydrogenation plant goes into operation, and reforms stabilizer base oil 1 and passes through
Cross heat exchanger 2 and enter contact tower 3 again, close valve 4, open valve 15, then the bottom of towe oil of contact tower 3 is directly entered depentanizer
10, it is heated to reacting required temperature into reboiler 12 by depentanizer bottom pump 11, opens valve 14, control valve 13, warp
The material return air and liquid mixer 6 for crossing heating is sufficiently mixed with hydrogen-rich gas 5, is then entered from the bottom of hydrogenation reactor 8,
Contacted with noble metal hydrogenation olefinic hydrocarbon expelling catalyzer, the deep hydrogenation saturated reaction of trace amounts of olefin is carried out under liquid phase atmosphere, refined
The lighter hydrocarbons that oil enters below the removing light dydrocarbon of depentanizer 10 by hydrogenation and olefin hydrocarbon removal reactor outlet pipeline 9, the tower of depentanizer 16
Base oil goes extraction unit to be used to produce all kinds of aromatic compounds.When hydrogenation and olefin hydrocarbon removal reactor 8 enter nominal situation after, close across
Line valve A15, cross-line valve B18 and valve 14, open valve 4 and valve 13, and hydrogenation and olefin hydrocarbon removal part enters normal production work
Skill flow, this flexible technological process avoids the initial production that goes into operation unqualified stationary phase.
When running well, pressure and depentanizer bottom pump 11 in the valve on leakproof pipeline 19, leakproof pipeline 19 are opened
Outlet pressure is identical, and the pressure is higher than the pressure of hydrotreating systems, if cross-line valve A15 has in interior leakage, leakproof pipeline 19
Material enter hydrotreating reactor 8；If cross-line valve B18 has the material in interior leakage, leakproof pipeline 19 to enter de- pentane
The underproof problem of depentanizer base oil 16 will not occur for tower 10, two kinds of situations.
During for the use of clay-filtered technological transformation being the inventive method, operating method is essentially identical.Hydrogenation plant goes into operation
When, depentanizer can be introduced first by reformed oil after Clay Refining Unit is handled, the materials at bottom of tower of depentanizer draws
Enter hydrogenation reactor, after hydrogenation catalyst and hydrogenation reactor are in stable state, by reformed oil without carclazyte essence
Device processed, is introduced directly into hydrogenation plant.Can also be directly foregoing newly-built（Without clay-filtered technique）The start-up method behaviour of device
Make.
The reformed oil handled by the inventive method, product can reach following property：Refined oil bromine index is less than
100mgBr/100g, aromatic hydrocarbons loss 0.5%.Other properties meet requirement of the extraction device to feedstock oil.
The advantage of the invention is that：Technological process is simple, easy to operate, invests less.For having weighed for oil refining enterprise
Engagement positions, only need to increase a hydrogenation and olefin hydrocarbon removal reactor and a gas again in reformer between contact tower and depentanizer
Liquid mixer both may be used, it is not necessary to independent newly-built a set of hydrogenation and olefin hydrocarbon removal device, and investment and operating cost can be greatly lowered.This hair
Bright method technological process is simple, and operating condition more relaxes, and exploitativeness is strong, and clay-filtered unit or hydrogenation can be substituted completely
Refined unit；And without the dynamic equipment such as make-up hydrogen compressor, circulating hydrogen compressor.If using existing process method, needed newly-built
Hydrogenation plant and corollary equipment, and investment and operating cost are higher.Contact tower bottom to depentanizer returns to gas again for increase simultaneously
Liquid mixer circular route, goes into operation initial stage, and depentanizer substrate material introduces hydrogenation plant, it is ensured that product quality directly meets and taken out
Make demands, it is to avoid initial production unqualified stationary phase.
The following examples illustrate the present invention further.
Experiment, using the hydrotreating catalyst that catalyst is commercial Application, is Fushun Petrochemical Research Institute's development and production
HDO-18 hydrogenation catalysts, its physicochemical property index is shown in Table 1.
Embodiment 1
By the newly-built reformer of application scheme.Reformed oil raw material 1 passes through stabilizer, again contact tower and tower top hydrogen partial
After being sufficiently mixed dissolving in SX type static mixers, into hydrogenation and olefin hydrocarbon removal reactor, reaction condition is：Reaction pressure
1.5MPa ﹑ volume space velocities 3.8h-1, 143 DEG C of reaction temperature.Hydrogenation plant is carried out using method of the present invention and carries out the place that goes into operation
Reason, reformed oil first introduces depentanizer when going into operation, and whole materials at bottom of tower of depentanizer introduce hydrogenation reactor, by 5
After hour, normal operating process is switched to（Reformed oil enters hydrogenation reactor, and depentanizer bottom of towe oil, which is not re-introduced into, to be added
Hydrogen reactor）.Raw material oil nature and product property are listed in table 2.
From table 2, use the technology can make the bromine index of reformed oil be reduced to 100mgBr/100g with
Under, and aromatic hydrocarbons loss 0.5%, and whole start-up process product quality also keeps stable.
Comparative example 1
According to the scheme of embodiment 1, simply when going into operation, reformed oil is directly entered hydrogenation reactor.In start-up process,
Reaction product has the requirement that can not touch the mark in about 30 hours.
Embodiment 2
The use of the clay-filtered technological transformation of reformed oil is herein described method.Reformed oil raw material 2 is by stable
After tower, again contact tower and tower top hydrogen partial are sufficiently mixed dissolving in SK type static mixers, into hydrogenation and olefin hydrocarbon removal reaction
Device, reaction condition is：Reaction pressure 1.6MPa ﹑ volume space velocities 4.2h-1, 157 DEG C of reaction temperature.Using method of the present invention
Carry out hydrogenation plant and carry out the processing that goes into operation, reformed oil first introduces Clay Refining Unit and introduced after clay-filtered when going into operation
Depentanizer, the 50% of the materials at bottom of tower of depentanizer（Quality）Hydrogenation reactor is introduced, after 30 minutes, is switched to normal
Operating process（Reformed oil enters hydrogenation reactor, and depentanizer bottom of towe oil is not re-introduced into hydrogenation reactor）.Feedstock oil
Property and product property are listed in table 2.
From table 3, use the technology can make the bromine index of reformed oil be reduced to 100mgBr/100g with
Under, and aromatic hydrocarbons loss 0.5%, and also quality keeps stable to whole start-up process product quality.
Comparative example 2
According to the scheme of embodiment 2, simply when going into operation, reformed oil is directly entered hydrogenation reactor.In start-up process,
Reaction product has the requirement that can not touch the mark in about 30 hours.
The physicochemical property index of the catalyst of table 1
The raw material oil nature of 2 embodiment of table 1 and result of the test
The raw material oil nature of 3 embodiment of table 2 and result of the test
Embodiment 3
During trial run, cross-line valve A15 and cross-line valve B18 very little apertures are opened, valves leakage operating mode is simulated, not
When enabling leakproof pipeline, product bromine index exceeds well over Con trolling index, and enables after leakproof pipeline, and product bromine index, which can be stablized, to be closed
Lattice.
By calculating, under some operating modes, when catalyst performance is good（Product index is far below Con trolling index）If,
There is 0.5% interior leakage, product index will not be up to standard；The later stage is used in catalyst（Product index is approached with Con trolling index）, it is slightly interior
Leakage, product index just will be unable to up to standard.
Claims (10)
1. a kind of reformed oil liquid-phase hydrogenatin processing method, including following content：Reformed oil is being entered into de- advance
Enter hydrotreating systems and carry out hydrotreating, hydrotreating systems include mixed dissolution hydrogen device and hydrotreating reactor,
Hydrotreating uses liquid-phase hydrogenatin treatment technology, including reformed oil to enter mixed dissolution hydrogen device by temperature raising, with hydrogen
Enter hydrotreating reactor after gas mixed dissolution, in hydrotreating reactor, reformed oil remains at least partly in liquid
Hydrobon catalyst is used in phase state, hydrotreating reactor, hydrotreating reaction effluent is directly entered depentanizer
Carry out fractionation processing；It is characterized in that：When setting cross-line is isolated for hydrotreating systems with reformer system, given birth to reforming
Be introduced directly into depentanizer into oil, cross-line be arranged on mixed dissolution hydrogen device suction line and depentanizer suction line it
Between connecting pipeline；Leakproof pipeline is set, and leakproof pipeline one end is connected with cross-line, the other end and depentanizer bottoming cycle pump discharge
Pipeline is connected, and valve is set on leakproof pipeline；The cross-line both sides of cross-line and leakproof pipeline communicating position are at least provided with first valve
Door；During normal operation, cross-line at least closed with every side of the cross-line both sides of leakproof pipeline communicating position together with valve, anti-fistulae
Valve on line is in open mode, prevents reformed oil from leaking to depentanizer through cross-line.
2. in accordance with the method for claim 1, it is characterised in that：The materials at bottom of tower and hydrogenation reaction of connection depentanizer are set
The pipeline of device entrance, when hydrogenation reactor goes into operation, hydrogenation reactor first introduced the materials at bottom of tower of depentanizer, by 5 minutes
After~24 hours, after preferably 1~10 hour, stop introducing the materials at bottom of tower of depentanizer, it is anti-that reformed oil is introduced into hydrogenation
Device is answered, normal hydrotreating reaction process is carried out.
3. in accordance with the method for claim 1, it is characterised in that：Hydrogenation reactor be arranged on reformer contact tower again and
Between depentanizer.
4. in accordance with the method for claim 1, it is characterised in that：Contain dechlorination tank in reformer, hydrogenation reactor is set
Between dechlorination tank and depentanizer.
5. in accordance with the method for claim 1, it is characterised in that：Hydrogenation reactor uses liquid phase reactor state, i.e., in reaction
Under the conditions of, at least part reformed oil is liquid phase state.
6. in accordance with the method for claim 1, it is characterised in that：The bottom of towe of depentanizer sets device for transporting objects, passes through
The material that depentanizer bottom of towe is exported is delivered to hydrogenation reactor entrance by device for transporting objects.
7. in accordance with the method for claim 1, it is characterised in that：Depentanizer sets tower bottom reboiler to be provided for depentanizer
Thermal source, the depentanizer materials at bottom of tower for introducing hydrogenation plant is drawn before tower bottom reboiler, or after tower bottom reboiler
Draw.
8. in accordance with the method for claim 1, it is characterised in that：Mixed dissolution hydrogen device is that static mixer or dynamic are mixed
Clutch.
9. in accordance with the method for claim 1, it is characterised in that：Hydrofining reaction pressure is the MPa of 0.5 MPa ~ 6.0, most
It is well the MPa of 1.2 MPa ~ 3.0；Reaction temperature is 100 DEG C ~ 200 DEG C, preferably 120 DEG C ~ 170 DEG C；Volume space velocity is 1.0 h-1
~10. 0h-1, preferably 2.0 h-1~6.0 h-1；The hydrogen to oil volume ratio for introducing hydrogen is 0 ~ 20：1, preferably 2：1~5：1.
10. in accordance with the method for claim 1, it is characterised in that：Hydrobon catalyst is with noble metal or reduced state nickel
For the Hydrobon catalyst of active component；Wherein using middle noble metal as the Hydrobon catalyst of active component, with aluminum oxide
For carrier, using Pt and/or Pd as active component, the content of active component by weight in the catalyst is not less than 0.1%, typically
For 0.1%~1.5%.
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