CN108102699A - A kind of coal tar method of comprehensive utilization - Google Patents
A kind of coal tar method of comprehensive utilization Download PDFInfo
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- CN108102699A CN108102699A CN201611052155.5A CN201611052155A CN108102699A CN 108102699 A CN108102699 A CN 108102699A CN 201611052155 A CN201611052155 A CN 201611052155A CN 108102699 A CN108102699 A CN 108102699A
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- weighted bmo
- bmo spaces
- reactor
- bed hydrogenation
- fixed bed
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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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
Abstract
The invention discloses a kind of coal tar method of comprehensive utilization, and the described method includes herein below：Coal tar enters preatreating reactors with pretreating agent and mixes, and is uniformly mixed and isolates coal tar after insoluble matter is purified through precipitation filtration treatment；After coal tar is mixed with hydrogen after obtained purification hydrotreating is carried out into boiling bed hydrogenation processing reaction zone；Gas, naphtha, diesel oil, wax oil and tail oil are obtained after the reaction effluent separation that the reaction generation oil that boiling bed hydrogenation processing reaction zone obtains obtains successively by the fixed bed hydrogenation pretreatment reaction area being arranged in series and fixed bed hydrogenation processing reaction zone, fixed bed hydrogenation processing reaction zone.This method flow is simple, it is only necessary to carry out simple modifications to existing apparatus, it is possible to significantly extend the service cycle of device, and can realize the utilization ratio of catalyst and maximize.
Description
Technical field
The present invention relates to a kind of heavy oil lighting processing methods, and coal tar is handled using hydrogenation technique more particularly to a kind of
Process.
Background technology
High temperature coal-tar is one of major secondary chemical products of coke-oven gas recycling, rich in distinctive aromatic compound
Object is valuable chemical resource.During existing rectifying separation processing technique, the yield of coal tar pitch is up to more than 55%, and
The outlet of coal tar pitch is always to restrict the bottleneck problem of coal tar processing industry.Its is cheap, seriously affects tar production enterprise
The economic benefit of industry, it is difficult to which processing forces substantial amounts of high temperature coal-tar to yield processing and make fuel and directly burn up, serious wave
Valuable chemical products resource is taken.Solve the problems, such as that this fundamental solution is to excavate high temperature coal-tar property deeply
Analysis, distinctive processing route is tailored according to its property, final to realize " making the best use of everything ".In view of high temperature coal-tar boiling range across
Degree is big, and composition is complicated, the characteristics such as condensed-nuclei aromatics content height, from utilization of resources angle, compared to traditional pure chemical separating route or
The currently a popular pure hydrogenation production light-weight fuel oil route of person, for high temperature coal-tar " tailoring " " suitable hydrocarbon then hydrocarbon " " preferably oil
It is then oily " route economy higher, resource utilization also higher.Related high temperature coal-tar production industrial chemicals takes into account production at present
The report of light-weight fuel oil is relatively fewer.
Patent CN103254928A describes a kind of method for improving high temperature coal-tar added value and utilizing.This method is with high temperature
Coal tar or its with organic solvent than the high temperature coal-tar solution mixed be raw material by certain mass, by batch autoclave or
Continuous fixed-bed reactor under hydrogenation catalyst effect, carries out the selective catalytic hydrogenation conversion reaction of high temperature coal-tar,
Polycyclic aromatic hydrocarbon compound in high temperature coal-tar especially coal tar pitch directional catalyzing is converted into low aromatic compound.We
Method is using the full fraction of high temperature coal-tar as raw material, and existing structure is relatively easy in high temperature coal-tar, relatively high pair of reactivity
The aromatic hydrocarbons such as ring, tricyclic also have the heavy constituents such as coal tar pitch complicated, that reaction difficulty is larger, under the same conditions to different work
Property component be hydrogenated with, it is likely that original low cyclophane cycle compound such as naphthalenes is caused in system to be hydrogenated saturation generation saturation
Hydrocarbon ultimately causes low cyclophane cycle compound loss, also results in original phenolic compound in system and be removed.And high temperature coal-tar
In phenols and naphthalenes be the industrial chemicals being of great value, using the method for the full fraction direct hydrogenation of high temperature coal-tar can cause high price
It is worth the loss of industrial chemicals；In addition, high temperature coal-tar belongs to high carbon residue, the heavy charge of high asphalitine, using traditional continuous
Fixed-bed reactor is hydrogenated with, it is easy to bed is caused to block, causes shorten service cycle, and batch still high-pressure installation and
Device quantity-produced requirement can not be met.
The content of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of coal tar method of comprehensive utilization.This method flow is simple,
It only needs to carry out simple modifications to existing apparatus, it is possible to significantly extend the service cycle of device, and the profit of catalyst can be made
It is realized and maximized with efficiency.The method of the present invention organically combines fixed bed and boiling bed hydrogenation, and coal tar raw material adds by boiling
It can ensure utmostly to obtain light-end products using fixed bed hydrogenation after the processing of hydrogen bed.
The present invention provides a kind of coal tar method of comprehensive utilization, and the described method includes herein below：
（1）Coal tar enters preatreating reactors with pretreating agent and mixes, and is uniformly mixed and is isolated not through precipitating filtration treatment
Molten object is purified rear coal tar；
（2）Step（1）It is hydrogenated with after coal tar is mixed with hydrogen after obtained purification into boiling bed hydrogenation processing reaction zone
Processing；
（3）The reaction generation oil that boiling bed hydrogenation processing reaction zone the obtains fixed bed hydrogenation pretreatment by being arranged in series successively
Reaction zone and fixed bed hydrogenation processing reaction zone, obtain after the reaction effluent separation that fixed bed hydrogenation processing reaction zone obtains
Gas, naphtha, diesel oil, wax oil and tail oil；
Wherein, the fixed bed hydrogenation pretreatment reaction area includes at least two weighted BMO spaces reactors being arranged in parallel, when
When the pressure drop of any one weighted BMO spaces reactor reaches predetermined value in the fixed bed hydrogenation pretreatment reaction area, by pressure drop
The weighted BMO spaces reactor for reaching predetermined value is cut out from fixed bed hydrogenation pretreatment reaction area, and by the fixed bed hydrogenation
Pretreatment reaction area, the pressure drop reach predetermined value weighted BMO spaces reactor and the fixed bed hydrogenation processing reaction zone with
The mode of series connection is connected in turn, wherein, the predetermined value designs the 50%~80% of the upper limit for pressure drop, preferably 60%~
70%。
In the method for the present invention, step（1）Described in coal tar can be that the full fraction of middle coalite tar, high temperature coal-tar are complete
The fluid product and full fraction of coal tar that fraction, coal hydrogenation cracking obtain cut off the mixed of the one or several kinds in the fraction of tail oil
Close object.
In the method for the present invention, step（1）Described in pretreating agent for solvent naphtha, the boiling range of the solvent naphtha for 65~
450 DEG C, be preferably 120~400 DEG C, more preferably 150~320 DEG C, and in the composition of the solvent naphtha, alkane and cycloalkane contain
Measure as 70~90%, can be specifically hydrofining diesel oil, hydrofinishing naphtha, hydrofinishing washing oil, hydrofinishing light oil,
One or several kinds of mixtures in hydrofinishing carbolic oil.The mass ratio of the pretreating agent and coal tar is 1:20~1:3,
Preferably 1:10~1:5.
In the method for the present invention, step（1）Described in preprocessor reaction temperature be 150~250 DEG C.
In the method for the present invention, step（3）Described in tail oil can be recycled back to boiling bed hydrogenation processing and reaction zone or defocus
Change reaction or as fuel oil etc..
In the method for the present invention, in the reaction starting stage, step（3）Described in fixed bed hydrogenation pretreatment reaction area include 3
~6, preferably include 3~4 weighted BMO spaces reactors being arranged in parallel.
It is when the pressure drop of a weighted BMO spaces reactor reaches the predetermined value, the hydrogenation is pre- in the method for the present invention
Treatment reactor is cut out from fixed bed hydrogenation pretreatment reaction area, which is named as to the hydrogenation cut out
Preatreating reactors I, and by the fixed bed hydrogenation pretreatment reaction area, the weighted BMO spaces reactor I cut out and institute
It states fixed bed hydrogenation processing reaction zone to be connected in turn in series, at this time the weighted BMO spaces reactor I cut out
Charging be remaining all weighted BMO spaces reactors in parallel reaction effluent；When the pressure of next weighted BMO spaces reactor
Drop cuts out the weighted BMO spaces reactor when reaching the predetermined value from fixed bed hydrogenation pretreatment reaction area, by this plus
Hydrogen pretreatment reactor is named as the weighted BMO spaces reactor II cut out, and by the fixed bed hydrogenation pretreatment reaction area,
The weighted BMO spaces reactor II cut out, the weighted BMO spaces reactor I cut out and fixed bed hydrogenation processing
Reaction zone is connected in turn in series；In the manner described above, until all weighted BMO spaces reactor all
It is connected in series to.
In the method for the present invention, step（3）Described in weighted BMO spaces all in fixed bed hydrogenation pretreatment reaction area it is anti-
Reach predetermined value during the pressure drop difference for answering device, it is two neighboring to reach closest to the weighted BMO spaces reactor for reaching pressure drop predetermined value
The time difference of its pressure drop predetermined value is not less than the 20% of the whole device cycle of operation, is preferably 20%~60%.
In the method for the present invention, added by the setting of operating condition and/or the difference fixed bed of catalyst bed property
Reach pressure drop predetermined value in hydrogen pretreatment reaction zone during each weighted BMO spaces reactor difference, for example, can be each by controlling
Different catalyst packing heights, different inlet amounies, different feed properties, different behaviour in a weighted BMO spaces reactor
Make under the conditions of condition and identical filling height using one or more modes in different Catalyst packing density come real
Now make to reach pressure drop predetermined value during each weighted BMO spaces reactor difference in fixed bed hydrogenation pretreatment reaction area.
In the method for the present invention, when being used by controlling under the conditions of filling height identical in each weighted BMO spaces reactor
The mode of different Catalyst packing density is come when realizing, in each hydrogenation of fixed bed hydrogenation pretreatment reaction area parallel connection
In preatreating reactors, maximum loading density can be 400kg/m3~600kg/m3, it is preferably 450kg/m3~550kg/m3；
Minimum loading density can be 300kg/m3~550kg/m3, it is preferably 350kg/m3~450kg/m3.Preferably, loading density
The Catalyst packing density difference of immediate two weighted BMO spaces reactors is 50kg/m3~200kg/m3, it is preferably
80kg/m3~150kg/m3.The difference loading density can be equipped with by different types of catalyst grade tamps it is existing, such as can be with
Realize that the Catalyst packing density in each weighted BMO spaces reactor is different in different proportions by hydrotreating catalyst.
In the method for the present invention, when being realized by way of control inlet amount different in each weighted BMO spaces reactor
When, the ratio between feed volume air speed of the immediate two weighted BMO spaces reactors of inlet amount can be 1.1 ~ 3：1, be preferably
1.1~1.5：1.
In the method for the present invention, when by way of controlling feed properties different in each weighted BMO spaces reactor come real
Now, the tenor difference of the immediate two weighted BMO spaces reactors of feed properties can be the μ of 5 μ g/g ~ 50 g/g, excellent
Elect the μ g/g of 10 μ g/g ~ 30 as.
In the method for the present invention, when by way of controlling operating condition different in each weighted BMO spaces reactor come real
Now, in control operation pressure and the operating condition of the immediate two weighted BMO spaces reactors of volume space velocity, operation temperature
Difference can be 2 DEG C ~ 30 DEG C, be preferably 5 DEG C ~ 20 DEG C；Or control operation pressure and immediate two of operation temperature are hydrogenated with
In the operating condition of preatreating reactors, volume space velocity difference is 0.1 h-1~10 h-1, it is preferably 0.2 h-1~5 h -1。
In the method for the present invention, according to Flow of Goods and Materials direction, hydrogenation protecting is loaded successively in each weighted BMO spaces reactor
Agent, Hydrodemetalation catalyst；Each weighted BMO spaces reactor can set according to itself process conditions and not load hydrodesulfurization
Catalyst loads a certain proportion of hydrodesulfurization catalytic after Hydrodemetalation catalyst also can be set according to itself process conditions
Agent；The reactor in the hydrotreating reaction area loads Hydrobon catalyst and hydrodenitrogeneration carbon residue reforming catalyst successively.
In the method for the present invention, boiling bed hydrogenation processing reaction zone can set the boiling bed hydrogenation reactor of 1 or more, excellent
Choosing sets 1 or 2 boiling bed hydrogenation reactor being arranged in series.Boiling of the prior art may be employed in boiling bed hydrogenation reactor
Rise a reactor.The reaction condition of boiling bed hydrogenation processing reaction zone can be specific according to feed properties and reaction conversion ratio requirement
It determines, generally：Reaction temperature is 330~450 DEG C, is preferably 360~430 DEG C；Reaction pressure is 8~25MPa, is preferably 10
~16MPa；Hydrogen to oil volume ratio 300：1~1000：1, it is preferably 600：1~900：1；Liquid volume air speed（LHSV）For 0.3 h-1
~5.0h-1, it is preferably 0.3 h-1~2.0h-1。
In the method for the present invention, the operating condition in the fixed bed hydrogenation pretreatment reaction area is：Temperature is 370 DEG C~420
DEG C, it is preferably 380 DEG C~400 DEG C；Pressure is 10MPa~25MPa, is preferably 15MPa~20MPa；Hydrogen to oil volume ratio for 300~
1500, it is preferably 500~800；Volume space velocity is 0.15h during raw material fluid-1~2h-1, it is preferably 0.3h-1~1h-1。
In the method for the present invention, the fixed bed hydrogenation processing reaction zone can include 1~5 hydrotreating being arranged in series
Reactor preferably includes 1~2 hydrotreating reactor being arranged in series.
In the method for the present invention, the operating condition of the fixed bed hydrogenation processing reaction zone is：Temperature is 370 DEG C~430 DEG C,
Preferably 380 DEG C~410 DEG C；Pressure is 10MPa~25MPa, is preferably 15MPa~20MPa；Hydrogen to oil volume ratio for 300~
1500, it is preferably 400~800；Volume space velocity is 0.15h during raw material fluid-1~0.8h-1, it is preferably 0.2h-1~0.6h-1。
Compared with prior art, provided by the invention described, coal tar method of comprehensive utilization has the following advantages that：
（1）The fixed bed hydrogenation pretreatment reaction area includes multiple weighted BMO spaces reactors in parallel so that entirely urges
Agent system takes off/holds metal ability and is increased dramatically.
（2）In coal tar method of comprehensive utilization method of the present invention, when the pressure drop of a weighted BMO spaces reactor increases
When length is to predetermined value, it from fixed bed hydrogenation pretreatment reaction area is cut out, and passes through the change of technological process, makes its pressure drop not
Rapid growth again, but can be slowly to increase in control range until device is stopped work, and then react some weighted BMO spaces
The pressure drop of device will not restrict the cycle of operation of whole device.
（3）In coal tar method of comprehensive utilization of the present invention, by will in fixed bed hydrogenation pretreatment reaction area it is each
To solve weighted BMO spaces reactor pressure decrease fast from the adjustment for being parallel to series connection handover operation mode for a weighted BMO spaces reactor
The problem that speed increases, while add the operating flexibility of device and raw material adaptability.
（4）In coal tar method of comprehensive utilization of the present invention, by setting weighted BMO spaces reactor parallel form
The appearance amount of metal of catalyst system is significantly increased so that the stability enhancing of system so that the growth of device pressure drop can obtain
Control extends the device cycle of operation.
（5）Coal tar method of comprehensive utilization of the present invention can utmostly realize that all kinds of catalyst synchronously inactivate,
So as to improve the operational efficiency of device, increase economic efficiency.
（6）In coal tar method of comprehensive utilization of the present invention, by weighted BMO spaces reaction zone catalyst performance
Energy is optimized and revised with technological parameter, the cooperation with subsequent high activity desulfurization carbon residue reforming catalyst so that whole improving
Desulfurization and carbon residue conversion performance are guaranteed while de-/appearance metal ability of catalyst.
（7）In coal tar method of comprehensive utilization of the present invention, pass through fixed bed and bubbling bed combined process, Ke Yishi
Now utmostly obtain light-end products.The method of the present invention combines fixed bed and the comprehensive advantage of ebullated bed improves dress on the whole
The operational efficiency put, increases economic efficiency.
Description of the drawings
Fig. 1 is a kind of schematic diagram of embodiment of coal tar method of comprehensive utilization of the present invention.
Fixed bed hydrogenation pretreatment reaction area and fixed bed hydrogenation in Fig. 2 coal tar method of comprehensive utilization of the present invention
Handle reaction zone schematic diagram.
Specific embodiment
The specific embodiment of the present invention is described in detail below.It is it should be appreciated that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The endpoint of disclosed scope and any value are not limited to the accurate scope or value herein, these scopes or
Value should be understood to comprising the value close to these scopes or value.For numberical range, between the endpoint value of each scope, respectively
It between the endpoint value of a scope and individual point value and can be individually combined with each other between point value and obtain one or more
New numberical range, these numberical ranges should be considered as specific open herein.
In coal tar method of comprehensive utilization of the present invention, the predetermined value for pressure drop design the upper limit 50%~
80%, for example, 50%, 51%, 53%, 54%, 55%, 56%, 57%, 58%, 60%, 61%, 62%, 63%, 64%, 65%, 66%, 67%, 68%,
69%th, 70%, 71%, 72%, 73%, 74%, 75%, 76%, 77%, 78%, 79%, 80% and any two value is formed in them model
Arbitrary value between enclosing.In the preferred case, the predetermined value designs the 60%~70% of the upper limit for pressure drop.In the present invention, institute
The maximum that the pressure drop design upper limit refers to reactor pressure decrease is stated, when reactor pressure decrease reaches the value, reaction system needs to stop work,
The pressure drop design upper limit is usually the MPa of 0.7 MPa ~ 1.0.
In coal tar method of comprehensive utilization of the present invention, during the pressure drop difference of all weighted BMO spaces reactors
Reach predetermined value.In the preferred case, it is two neighboring to reach it closest to the weighted BMO spaces reactor for reaching pressure drop predetermined value
The time difference of pressure drop predetermined value is not less than the 20% of whole service cycle, is preferably the 20-60% in whole service cycle, for example,
20%、25%、30%、35%、40%、45%、50%、55%、60%.In the present invention, the whole service cycle refers to that coal tar integrates
In Application way, bring into operation from device to the undergone time of stopping work.
In coal tar method of comprehensive utilization of the present invention, each of the fixed bed hydrogenation pretreatment reaction area adds
Hydrogenation protecting agent, Hydrodemetalation catalyst, Hydrobon catalyst and hydrodenitrogeneration can be loaded in hydrogen pretreatment reactor
One or more in carbon residue reforming catalyst, the fixed bed hydrogenation, which handles to load to be hydrogenated in the reactor of reaction zone, to be taken off
One or more in sulfur catalyst and hydrodenitrogeneration carbon residue reforming catalyst.
In a preferred embodiment, according to Flow of Goods and Materials direction, loaded successively in each weighted BMO spaces reactor
Hydrogenation protecting agent, Hydrodemetalation catalyst and optional Hydrobon catalyst；The reaction in the hydrotreating reaction area
Device loads Hydrobon catalyst and hydrodenitrogeneration carbon residue reforming catalyst successively.It is filled according to the catalyst of the preferred embodiment
Embankment formula so that de-/appearance metal ability of whole system is increased dramatically, while the adjustment matched somebody with somebody by catalyst grade is each
The pressure drop of a weighted BMO spaces reactor increases in control range.In fixed bed hydrogenation pretreatment reaction area it is in parallel each plus
The catalyst system of hydrogen pretreatment reactor filling is based on de-/appearance metal function so that while demetalization performance boost, by force
Change the ability to the hydro-conversion of such as gum asphalt of macromolecular in raw material, base is established for successive depths desulfurization and the conversion of carbon residue
Plinth so that hydrodesulfurizationreaction reaction zone is conducive to further deep reaction, therefore, and compared with routine techniques, side of the present invention
Although the ratio of Hydrodemetalation catalyst improves in method, the hydro-conversion of whole desulphurizing activated and carbon residue
Performance is not only improved instead without reducing.
In the present invention, the hydrogenation protecting agent, the Hydrodemetalation catalyst, the Hydrobon catalyst and institute
Stating hydrodenitrogeneration carbon residue reforming catalyst all can be the conventional use of catalyst of fixed bed heavy-oil hydrogenation processing procedure.These are urged
Agent is usually with porous refractory inorganic oxide（Such as aluminium oxide）For carrier, group VIB and/or group VIII metal（As W, Mo,
Co, Ni etc.）Oxide for active component, be selectively added the catalyst of the elements such as other various auxiliary agents such as P, Si, F, B.
For example, the FZC series heavy oil hydrogenating treatment catalysts produced by catalyst branch company of Sinopec Group.
In the present invention, the boiling bed hydrogenation of the catalyst this field routine used in the boiling bed hydrogenation reactor is urged
For agent generally using aluminium oxide as carrier, particle is spherical shape, and a diameter of 0.1~0.8mm is preferably 0.1~0.6mm, wear≤
2.0wt%, catalyst specific surface are 100~300m2/ g, bore dia at least account for the 70% of total pore volume in the hole of 5~20nm；With weight
Meter, catalyst contain VI B family metal oxides（Such as MoO3）12.0%~30.0%, preferably 15.0%~25.0%, containing VIII race's metal
Oxide（Such as NiO or CoO）0.5%~10.0%, preferably 2.0%~8.0%.Containing at least one auxiliary agent, selected from following several
Element：B, Ca, F, Mg, P, Si, Ti etc., auxiliary agent content are 1.0%~8.0%.
Fig. 1 is a kind of schematic diagram of embodiment of coal tar method of comprehensive utilization of the present invention, and Fig. 2 is present invention side
Fixed bed hydrogenation pretreatment reaction area and fixed bed hydrogenation processing reaction zone schematic diagram in method.With reference to Fig. 1, Fig. 2 to this hair
The bright coal tar method of comprehensive utilization is further described, but not thereby limiting the invention.
As shown in Figure 1 and Figure 2, coal tar method of comprehensive utilization of the present invention includes following content：Coal tar raw material M1
Into preatreating reactors R5 after being mixed with pretreating agent M2, rear coal tar M3 and impurity M4 is purified after processing, is obtained
It is obtained after coal tar M3 is mixed with hydrogen M21 after purification into boiling bed hydrogenation reactor R1, boiling bed hydrogenation reactor R1
The material M5 of liquid phase pre-processes anti-through feeding line 1, feeding line 2 and feeding line 3 into the fixed bed hydrogenation being arranged in series
Area R2 and fixed bed hydrogenation is answered to handle reaction zone R3, after the reaction effluent separation that fixed bed hydrogenation processing reaction zone R3 is obtained
To gas M7, naphtha M8, diesel oil M9, wax oil M10 and tail oil M11.Wherein described fixed bed hydrogenation pretreatment reaction area R2 bags
Three weighted BMO spaces reactors being arranged in parallel are included, is respectively weighted BMO spaces reactor A, weighted BMO spaces reactor B, adds
Hydrogen pretreatment reactor C, the weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C into
Material mouth is connected respectively with feeding line 1, feeding line 2 and feeding line 3, the outlet point three of the weighted BMO spaces reactor A
Road, the first via are connected through pipeline 6 with the feed inlet of weighted BMO spaces reactor B, and the second tunnel is reacted through pipeline 7 and weighted BMO spaces
The feed inlet connection of device C, the 3rd tunnel is connected through pipeline 10 with the feed inlet of hydrodesulphurisatioreactors reactors D；The weighted BMO spaces are anti-
Three tunnels of outlet point of device B are answered, the first via is connected through pipeline 4 with the feed inlet of weighted BMO spaces reactor A, and the second tunnel is through pipeline 5
Feed inlet is obtained with weighted BMO spaces reactor C to be connected, the 3rd tunnel is connected through pipeline 11 with the feed inlet of hydrotreating reactor D；
Three tunnels of the outlet of the weighted BMO spaces reactor C point, feed inlet of the first via through pipeline 8 and weighted BMO spaces reactor A connect
It connects, the second tunnel is connected through pipeline 9 with the feed inlet of weighted BMO spaces reactor B, and the 3rd tunnel is through pipeline 12 and hydrotreating reaction
The feed inlet connection of device D；Valve 101 is provided on the pipeline 1, is provided with valve 102 on the pipeline 2, on the pipeline 3
Valve 103 is provided with, valve 104 is provided on the pipeline 4, valve 105 is provided on the pipeline 5, is set on the pipeline 6
Valve 106 is equipped with, valve 107 is provided on the pipeline 7, valve 108 is provided on the pipeline 8, is set on the pipeline 9
There is valve 109, valve 1010 is provided on the pipeline 10, be provided with valve 1011 on the pipeline 11, on the pipeline 12
Valve 1012 is provided with, the generation oil M6 that the hydrotreating reactor D is obtained obtains gas M7, naphtha after entering separation
M8, diesel oil M9, wax oil M10 and tail oil M11.The weighted BMO spaces reactor A, the weighted BMO spaces reactor B and described
It is each provided with monitoring the sensing unit of pressure drop in weighted BMO spaces reactor C（It is not shown in figure）, and further include control
Unit processed（It is not shown in figure）, for receive the pressure drop signal from the sensing unit, and according to the pressure drop signal control with
The corresponding valve of each weighted BMO spaces reactor.
In above-mentioned coal tar method of comprehensive utilization, weighted BMO spaces reactor A, weighted BMO spaces reactor B and hydrogenation
Preatreating reactors C can be inactivated in any order, it is preferred to use following six kinds of modes switch over operation：
Mode 1：It is sequentially reached according to weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C
Pressure drop predetermined value.
（1）When going into operation, pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, the valve 101 on pipeline 12, valve 102,
Valve 103, valve 1010, valve 1011, valve 1012 are opened, pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, on pipeline 9
Valve 104, valve 105, valve 106, valve 107, valve 108, valve 109 close；
（2）With sensing unit detection weighted BMO spaces reactor A, weighted BMO spaces reactor B and weighted BMO spaces reactor C
Pressure drop, when the pressure drop of weighted BMO spaces reactor A reaches predetermined value, from corresponding to the weighted BMO spaces reactor A
The pressure drop signal of sensing unit passes to control unit, and control unit performs to regulate and control valve after receiving the signal, tool
Body, valve 101, the valve 1011 of pipeline 11 and the valve 1012 of pipeline 12 of feeding line 1 are closed, is opened on pipeline 8
Valve 104 on valve 108 and pipeline 4 so that weighted BMO spaces reaction zone（It is pre- including weighted BMO spaces reactor B and hydrogenation
Treatment reactor C）, weighted BMO spaces reactor A and hydrodesulfurizationreaction reaction zone form series connection, complete at this time once by being parallel to string
The handover operation of connection；
（3）When the pressure drop of weighted BMO spaces reactor B reaches predetermined value, from corresponding to the weighted BMO spaces reactor B
The pressure drop signal of sensing unit pass to control unit, control unit performs to regulate and control valve after receiving the signal,
Specifically, valve 102, the valve 108 of pipeline 8 of feeding line 2 are closed, opens the valve 109 on pipeline 9 so that hydrogenation is pre-
Treatment reactor C, weighted BMO spaces reactor B, weighted BMO spaces reactor A and hydrodesulfurizationreaction reaction zone form series connection, at this time
Complete the 2nd handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor C reaches the design upper limit, entire reaction system needs shutdown process.
Mode 2：It is sequentially reached according to weighted BMO spaces reactor A, weighted BMO spaces reactor C, weighted BMO spaces reactor B
Pressure drop predetermined value.
（1）When going into operation, pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, the valve 101 on pipeline 12, valve 102,
Valve 103, valve 1010, valve 1011, valve 1012 are opened, pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, on pipeline 9
Valve 104, valve 105, valve 106, valve 107, valve 108, valve 109 close；
（2）With sensing unit detection weighted BMO spaces reactor A, weighted BMO spaces reactor B and weighted BMO spaces reactor C
Pressure drop, when the pressure drop of weighted BMO spaces reactor A reaches predetermined value, from corresponding to the weighted BMO spaces reactor A
The pressure drop signal of sensing unit passes to control unit, and control unit performs to regulate and control valve after receiving the signal, tool
Body, valve 101, the valve 1011 of pipeline 11 and the valve 1012 of pipeline 12 of feeding line 1 are closed, is opened on pipeline 8
Valve 104 on valve 108 and pipeline 4 so that weighted BMO spaces reaction zone（It is pre- including weighted BMO spaces reactor B and hydrogenation
Treatment reactor C）, weighted BMO spaces reactor A and hydrodesulfurizationreaction reaction zone form series connection, complete at this time once by being parallel to string
The handover operation of connection；
（3）When the pressure drop of weighted BMO spaces reactor C reaches predetermined value, from corresponding to the weighted BMO spaces reactor C
The pressure drop signal of sensing unit pass to control unit, control unit performs to regulate and control valve after receiving the signal,
Specifically, valve 103, the valve 104 of pipeline 4 of feeding line 3 are closed, opens the valve 105 on pipeline 5 so that hydrogenation is pre-
Treatment reactor B, weighted BMO spaces reactor C, weighted BMO spaces reactor A and hydrodesulfurizationreaction reaction zone form series connection, at this time
Complete the 2nd handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor C reaches predetermined value, entire reaction system needs shutdown process.
Mode 3：It is sequentially reached according to weighted BMO spaces reactor B, weighted BMO spaces reactor C, weighted BMO spaces reactor A
Pressure drop predetermined value.
（1）When going into operation, pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, the valve 101 on pipeline 12, valve 102,
Valve 103, valve 1010, valve 1011, valve 1012 are opened, pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, on pipeline 9
Valve 104, valve 105, valve 106, valve 107, valve 108, valve 109 close；
（2）With sensing unit detection weighted BMO spaces reactor A, weighted BMO spaces reactor B and weighted BMO spaces reactor C
Pressure drop, when the pressure drop of weighted BMO spaces reactor B reaches predetermined value, from corresponding to the weighted BMO spaces reactor B
The pressure drop signal of sensing unit passes to control unit, and control unit performs to regulate and control valve after receiving the signal, tool
Body, valve 102, the valve 1010 of pipeline 10 and the valve 1012 of pipeline 12 of feeding line 2 are closed, is opened on pipeline 9
Valve 106 on valve 109 and pipeline 6 so that weighted BMO spaces reaction zone（It is pre- including weighted BMO spaces reactor A and hydrogenation
Treatment reactor C）, weighted BMO spaces reactor B and hydrodesulfurizationreaction reaction zone form series connection, complete at this time once by being parallel to string
The handover operation of connection；
（3）When the pressure drop of weighted BMO spaces reactor C reaches predetermined value, from corresponding to the weighted BMO spaces reactor C
The pressure drop signal of sensing unit pass to control unit, control unit performs to regulate and control valve after receiving the signal,
Specifically, valve 103, the valve 106 of pipeline 6 of feeding line 3 are closed, opens the valve 107 on pipeline 7 so that hydrogenation is pre-
Treatment reactor A, weighted BMO spaces reactor C, weighted BMO spaces reactor B and hydrodesulfurizationreaction reaction zone form series connection, at this time
Complete the 2nd handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor A reaches predetermined value, entire reaction system needs shutdown process.
Mode 4：It is sequentially reached according to weighted BMO spaces reactor B, weighted BMO spaces reactor A, weighted BMO spaces reactor C
Pressure drop predetermined value.
（1）When going into operation, pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, the valve 101 on pipeline 12, valve 102,
Valve 103, valve 1010, valve 1011, valve 1012 are opened, pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, on pipeline 9
Valve 104, valve 105, valve 106, valve 107, valve 108, valve 109 close；
（2）With sensing unit detection weighted BMO spaces reactor A, weighted BMO spaces reactor B and weighted BMO spaces reactor C
Pressure drop, when the pressure drop of weighted BMO spaces reactor B reaches predetermined value, from corresponding to the weighted BMO spaces reactor B
The pressure drop signal of sensing unit passes to control unit, and control unit performs to regulate and control valve after receiving the signal, tool
Body, valve 102, the valve 1010 of pipeline 10 and the valve 1012 of pipeline 12 of feeding line 2 are closed, is opened on pipeline 9
Valve 106 on valve 109 and pipeline 6 so that weighted BMO spaces reaction zone（It is pre- including weighted BMO spaces reactor A and hydrogenation
Treatment reactor C）, weighted BMO spaces reactor B and hydrodesulfurizationreaction reaction zone form series connection, complete at this time once by being parallel to string
The handover operation of connection；
（3）When the pressure drop of weighted BMO spaces reactor A reaches predetermined value, from corresponding to the weighted BMO spaces reactor A
The pressure drop signal of sensing unit pass to control unit, control unit performs to regulate and control valve after receiving the signal,
Specifically, valve 101, the valve 109 of pipeline 9 of feeding line 1 are closed, opens the valve 108 on pipeline 8 so that hydrogenation is pre-
Treatment reactor C, weighted BMO spaces reactor A, weighted BMO spaces reactor B and hydrodesulfurizationreaction reaction zone form series connection, at this time
Complete the 2nd handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor C reaches predetermined value, entire reaction system needs shutdown process.
Mode 5：It is sequentially reached according to weighted BMO spaces reactor C, weighted BMO spaces reactor B, weighted BMO spaces reactor A
Pressure drop predetermined value.
（1）When going into operation, pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, the valve 101 on pipeline 12, valve 102,
Valve 103, valve 1010, valve 1011, valve 1012 are opened, pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, on pipeline 9
Valve 104, valve 105, valve 106, valve 107, valve 108, valve 109 close；
（2）With sensing unit detection weighted BMO spaces reactor A, weighted BMO spaces reactor B and weighted BMO spaces reactor C
Pressure drop, when the pressure drop of weighted BMO spaces reactor C reaches predetermined value, from corresponding to the weighted BMO spaces reactor C's
The pressure drop signal of sensing unit passes to control unit, and control unit performs to regulate and control valve after receiving the signal, tool
Body, valve 103, the valve 1010 of pipeline 10 and the valve 1011 of pipeline 11 of feeding line 3 are closed, is opened on pipeline 7
Valve 105 on valve 107 and pipeline 5 so that weighted BMO spaces reaction zone（It is pre- including weighted BMO spaces reactor A and hydrogenation
Treatment reactor B）, weighted BMO spaces reactor C and hydrodesulfurizationreaction reaction zone form series connection, complete at this time once by being parallel to string
The handover operation of connection；
（3）When the pressure drop of weighted BMO spaces reactor B reaches predetermined value, from corresponding to the weighted BMO spaces reactor B
The pressure drop signal of sensing unit pass to control unit, control unit performs to regulate and control valve after receiving the signal,
Specifically, valve 102, the valve 107 of pipeline 7 of feeding line 2 are closed, opens the valve 106 on pipeline 6 so that hydrogenation is pre-
Treatment reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C and hydrodesulfurizationreaction reaction zone form series connection, at this time
Complete the 2nd handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor A reaches predetermined value, entire reaction system needs shutdown process.
Mode 6：It is sequentially reached according to weighted BMO spaces reactor C, weighted BMO spaces reactor A, weighted BMO spaces reactor B
Pressure drop predetermined value.
（1）When going into operation, pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, the valve 101 on pipeline 12, valve 102,
Valve 103, valve 1010, valve 1011, valve 1012 are opened, pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, on pipeline 9
Valve 104, valve 105, valve 106, valve 107, valve 108, valve 109 close；
（2）With sensing unit detection weighted BMO spaces reactor A, weighted BMO spaces reactor B and weighted BMO spaces reactor C
Pressure drop, when the pressure drop of weighted BMO spaces reactor C reaches predetermined value, from corresponding to the weighted BMO spaces reactor C's
The pressure drop signal of sensing unit passes to control unit, and control unit performs to regulate and control valve after receiving the signal, tool
Body, valve 103, the valve 1010 of pipeline 10 and the valve 1011 of pipeline 11 of feeding line 3 are closed, is opened on pipeline 7
Valve 105 on valve 107 and pipeline 5 so that weighted BMO spaces reaction zone（It is pre- including weighted BMO spaces reactor A and hydrogenation
Treatment reactor B）, weighted BMO spaces reactor C and hydrodesulfurizationreaction reaction zone form series connection, complete at this time once by being parallel to string
The handover operation of connection；
（3）When the pressure drop of weighted BMO spaces reactor A reaches predetermined value, from corresponding to the weighted BMO spaces reactor A
The pressure drop signal of sensing unit pass to control unit, control unit performs to regulate and control valve after receiving the signal,
Specifically, valve 101, the valve 105 of pipeline 5 of feeding line 1 are closed, opens the valve 104 on pipeline 4 so that hydrogenation is pre-
Treatment reactor B, weighted BMO spaces reactor A, weighted BMO spaces reactor C and hydrodesulfurizationreaction reaction zone form series connection, at this time
Complete the 2nd handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor B reaches predetermined value, entire reaction system needs shutdown process.
Illustrate the effect of the present invention with reference to specific embodiment, it is used in embodiment of the present invention and comparative example
Raw material includes three kinds, respectively raw material A, raw material B, raw material C, and specific nature is shown in Table 1, and the boiling bed hydrogenation reaction zone sets 1
A boiling bed hydrogenation reactor, the catalyst of the interior filling of the boiling bed hydrogenation reactor is boiling bed hydrogenation catalyst.Boiling
Bed hydrogenation catalyst prepares the spherical carrier of catalyst that average pore size is 13nm, and spherical catalyst particles 0.1-0.3mm is other
Catalyst preparation process is carried out with reference to US7074740 and CN200710010377.5 methods.It is molten that Mo-Co-P is prepared according to a conventional method
Liquid, MoO3 mass meters content is 18.00% in solution, and it is 3.50%, P mass contents for 1.05% to count content using CoO mass.With this
Solution impregnates above-mentioned carrier by incipient impregnation method and obtains final catalyst.
Boiling bed hydrogenation reactor of the present invention is a kind of three-phase fluidized bed reactor, be may be employed
The fluidized bed reactor that CN02109404.7, CN200610134154.5 and CN200710012680.9 etc. are announced, Neng Gouman
Sufficient gas, liquid, solid three-phase separates in fluidized bed reactor.
The type of feed of catalyst is shown in Table 2 in the Examples 1 to 3, the filling side of catalyst in the comparative example 1~3
Formula is shown in Table 3, and the reaction condition of the Examples 1 to 3 is shown in Table 4, and the reaction condition of the comparative example 1~3 is shown in Table 5, the implementation
The reaction result of example 1~3 and comparative example 1~3 is shown in Table 6.Using conventional tandem process, other difference in the comparative example 1-3
It is corresponding identical with Examples 1 to 3.Weighted BMO spaces reactor A, weighted BMO spaces reactor B described in the embodiment of the present invention,
Weighted BMO spaces reactor C is pattern, the identical reactor of size, reactor A, reactor B in the comparative example, reactor
C is pattern, the identical reactor of size.
Pretreating agent solvent oil nature is as follows used in the embodiment of the present invention and comparative example：Density is 0.86kg/m3（20℃）,
Viscosity is 5.31mm2/s（40℃）, sulfur content is 55 μ g/g, and nitrogen content is 15 μ g/g, and saturation is divided into 75.70%, and aromatic hydrocarbons is
24.3%。
Embodiment 1
It is all used in weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C described in embodiment 1
Raw material A, the catalyst general assembly of the weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C
Amount, feed properties are identical with inlet amount, the pre- place of the weighted BMO spaces reactor A, weighted BMO spaces reactor B, hydrogenation
Reason reactor C, the catalyst of hydrodesulphurisatioreactors reactors D load in the way of in table 2, and the operating condition is shown in Table 4, specific anti-
6 should be the results are shown in Table, the product property obtained after boiling bed hydrogenation cracking is shown in Table 7.Preprocessor used in the embodiment 1
Reaction temperature is 200 DEG C.
Embodiment 2
In embodiment 2, all adopted in the weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C
With raw material B, specific nature is shown in Table 1, and each anti-Feed space velocities are different, and volume space velocity is during the weighted BMO spaces reactor A liquid
0.20h-1, volume space velocity is 0.32h during weighted BMO spaces reactor B liquid-1, volume space velocity is during weighted BMO spaces reactor C liquid
0.44h-1.Identical catalysis is used in weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C
Agent type of feed, catalyst loading pattern are shown in Table 2, and the operating condition of each reactor is shown in Table 4, and specific reaction result is shown in Table
6.Preprocessor reaction temperature used is 220 DEG C.
Embodiment 3
In embodiment 3, in the weighted BMO spaces reactor A using raw material A, in weighted BMO spaces reactor B using raw material B,
In weighted BMO spaces reactor C 1 is shown in Table using raw material C, raw materials used property.The pre- place of the weighted BMO spaces reactor A, hydrogenation
It is identical to manage reactor B, the inlet amount of weighted BMO spaces reactor C, the weighted BMO spaces reactor A, weighted BMO spaces reaction
Using identical catalyst loading pattern in device B, weighted BMO spaces reactor C, catalyst loading pattern is shown in Table 2, described each
The operating condition of reactor is shown in Table 4, and specific reaction result is shown in Table 6.Preprocessor reaction temperature used is 180 DEG C.
Comparative example 1
It is respectively reactor A, reactor B, reactor C, reactor D also using 4 reactors in comparative example 1, it is reactor A, anti-
Device B, reactor C is answered to be connected with reactor D in the form of being sequentially connected in series.Raw materials used A properties are shown in Table 1 in comparative example 1, reaction
The inlet amount and feed properties of device A are identical with the total feed and feed properties of embodiment 1.Preprocessor reaction temperature used
It spends for 200 DEG C.The reactor A, reactor B, the catalyst inventory of reactor C and reactor D hydrogenation corresponding with embodiment
Preatreating reactors A, weighted BMO spaces reactor B, weighted BMO spaces reactor C, hydrodesulphurisatioreactors reactors D are identical, but each
The loadings of a species catalyst are different, loaded in the way of in table 3, and the operating condition is shown in Table 5, specific reaction knot
Fruit is shown in Table 6.
Comparative example 2
It is respectively reactor A, reactor B, reactor C, reactor D also using 4 reactors in comparative example 2, it is reactor A, anti-
Device B, reactor C is answered to be connected with reactor D in the form of being sequentially connected in series.1 is shown in Table using raw material B, property in comparative example 2, instead
Answer device A entrances identical with the inlet amount and feed properties that embodiment 2 is total.Preprocessor reaction temperature used is 220 DEG C.Institute
The catalyst inventory for stating reactor A, reactor B, reactor C and reactor D is reacted with 2 corresponding weighted BMO spaces of embodiment
Device A, weighted BMO spaces reactor B, weighted BMO spaces reactor C, hydrodesulphurisatioreactors reactors D are identical, but various species are catalyzed
The loadings of agent are different, loaded in the way of in table 3, and the operating condition is shown in Table 5.
Comparative example 3
It is respectively reactor A, reactor B, reactor C, reactor D also using 4 reactors in comparative example 3, it is reactor A, anti-
Device B, reactor C is answered to be connected with reactor D in the form of being sequentially connected in series.Comparative example 3 uses raw material A, the ratios such as raw material B, raw material C
Example mixed raw material, reactor A, reactor B, reactor C and reactor D are using the form of series connection, reactor A entrance in comparative example
It is identical with the inlet amount and mixed feeding property that embodiment 3 is total.Preprocessor reaction temperature used is 180 DEG C.The reactor
A, the catalyst inventory of reactor B, reactor C and reactor D weighted BMO spaces reactor A corresponding with embodiment, hydrogenation are pre-
Treatment reactor B, weighted BMO spaces reactor C, hydrodesulphurisatioreactors reactors D are identical, but the loadings of various species catalyst
It is different, it is loaded in the way of in table 3, the operating condition is shown in Table 5.
1 feedstock property of table
Catalyst loading pattern in 2 Examples 1 to 3 of table
Catalyst loading pattern in 3 comparative example 1~3 of table
The reaction condition of 4 Examples 1 to 3 of table
The reaction condition of 5 comparative example 1~3 of table
6 steady running cycle of table and residual hydrogenation generation oil nature
Claims (20)
1. a kind of coal tar method of comprehensive utilization, the described method includes herein below：
（1）Coal tar enters preatreating reactors with pretreating agent and mixes, and is uniformly mixed and is isolated not through precipitating filtration treatment
Molten object is purified rear coal tar；
（2）Step（1）It is hydrogenated with after coal tar is mixed with hydrogen after obtained purification into boiling bed hydrogenation processing reaction zone
Processing；
（3）The reaction generation oil that boiling bed hydrogenation processing reaction zone the obtains fixed bed hydrogenation pretreatment by being arranged in series successively
Reaction zone and fixed bed hydrogenation processing reaction zone, obtain after the reaction effluent separation that fixed bed hydrogenation processing reaction zone obtains
Gas, naphtha, diesel oil, wax oil and tail oil；
Wherein, the fixed bed hydrogenation pretreatment reaction area includes at least two weighted BMO spaces reactors being arranged in parallel, when
When the pressure drop of any one weighted BMO spaces reactor reaches predetermined value in the fixed bed hydrogenation pretreatment reaction area, by pressure drop
The weighted BMO spaces reactor for reaching predetermined value is cut out from fixed bed hydrogenation pretreatment reaction area, and by the fixed bed hydrogenation
Pretreatment reaction area, the pressure drop reach predetermined value weighted BMO spaces reactor and the fixed bed hydrogenation processing reaction zone with
The mode of series connection is connected in turn, wherein, the predetermined value designs the 50%~80% of the upper limit for pressure drop, preferably 60%~
70%。
2. according in claim 1 method, wherein, step（1）Described in coal tar for the full fraction of middle coalite tar, high-temperature coal
It is a kind of or several in the fraction for fluid product and full fraction of coal tar the excision tail oil that the full fraction of tar, coal hydrogenation cracking obtain
The mixture of kind.
3. according to claim 1 method, it is characterised in that：Step（1）Described in preprocessor reaction temperature for 150~
250℃。
4. according to claim 1 method, wherein, step（1）Described in pretreating agent for solvent naphtha, the boiling range of the solvent naphtha
It is preferably 120~400 DEG C for 65~450 DEG C, more preferably 150~320 DEG C, in the composition of the solvent naphtha, alkane and ring
Determination of Alkane Content is 70~90%.
5. according to claim 4 method, wherein, step（1）Described in solvent naphtha be hydrofining diesel oil, hydrofinishing stone brain
One or several kinds of mixtures in oil, hydrofinishing washing oil, hydrofinishing light oil, hydrofinishing carbolic oil.
6. according to claim 4 method, wherein, step（1）Described in the mass ratio of pretreating agent and coal tar be 1:20~1:
3, it is preferably 1:10~1:5.
7. according to claim 1 method, wherein, it, will when the pressure drop of a weighted BMO spaces reactor reaches the predetermined value
The weighted BMO spaces reactor is cut out from fixed bed hydrogenation pretreatment reaction area, which is named as and is cut
The weighted BMO spaces reactor I gone out, and the fixed bed hydrogenation pretreatment reaction area, the weighted BMO spaces cut out are reacted
Device I and fixed bed hydrogenation processing reaction zone are connected in turn in series, at this time the weighted BMO spaces cut out
The charging of reactor I is the reaction effluent of remaining all weighted BMO spaces reactors in parallel；When next weighted BMO spaces are anti-
When the pressure drop of device being answered to reach the predetermined value, which is cut from fixed bed hydrogenation pretreatment reaction area
Go out, which is named as to the weighted BMO spaces reactor II cut out, and the fixed bed hydrogenation is located in advance
Manage reaction zone, the weighted BMO spaces reactor II cut out, the weighted BMO spaces reactor I cut out and the fixed bed
Hydrotreating reaction area is connected in turn in series；In the manner described above, until all weighted BMO spaces react
Device is all connected in series to.
8. according to claim 1 method, wherein, step（3）Described in hydrogenation all in fixed bed hydrogenation pretreatment reaction area
Reach predetermined value during the pressure drop difference of preatreating reactors, it is two neighboring anti-closest to the weighted BMO spaces for reaching pressure drop predetermined value
The time difference that device reaches its pressure drop predetermined value is answered to be not less than the 20% of the whole device cycle of operation, is preferably 20%~60%.
9. according to claim 1 method, wherein, pass through the setting of operating condition and/or the difference of catalyst bed property
Reach pressure drop predetermined value during each weighted BMO spaces reactor difference in fixed bed hydrogenation pretreatment reaction area, it is each by controlling
Different catalyst packing heights, different inlet amounies, different feed properties, different operations in weighted BMO spaces reactor
It is realized under the conditions of condition and identical filling height using one or more modes in different Catalyst packing density
Make to reach pressure drop predetermined value during each weighted BMO spaces reactor difference in fixed bed hydrogenation pretreatment reaction area.
10. according to claim 9 method, wherein, when by controlling filling height identical in each weighted BMO spaces reactor
Under the conditions of by the way of different Catalyst packing density come when realizing, it is in parallel in the fixed bed hydrogenation pretreatment reaction area
Each weighted BMO spaces reactor in, maximum loading density be 400kg/m3~600kg/m3, it is preferably 450kg/m3~
550kg/m3；Minimum loading density is 300kg/m3~550kg/m3, it is preferably 350kg/m3~450kg/m3。
11. according to claim 10 method, wherein, the catalyst dress of the immediate two weighted BMO spaces reactors of loading density
Filling density difference is 50kg/m3~200kg/m3, it is preferably 80kg/m3~150kg/m3。
12. according to claim 9 method, wherein, when by controlling inlet amount different in each weighted BMO spaces reactor
Mode is come when realizing, the ratio between feed volume air speed of the immediate two weighted BMO spaces reactors of inlet amount is 1.1 ~ 3：1, it is excellent
Elect 1.1 ~ 1.5 as：1.
13. according to claim 9 method, wherein, when by controlling feed properties different in each weighted BMO spaces reactor
Mode come when realizing, the tenor differences of the immediate two weighted BMO spaces reactors of feed properties is the μ of 5 μ g/g ~ 50
G/g is preferably the μ g/g of 10 μ g/g ~ 30.
14. according to claim 9 method, wherein, when by controlling operating condition different in each weighted BMO spaces reactor
Mode come when realizing, the operating condition of control operation pressure and the immediate two weighted BMO spaces reactors of volume space velocity
In, operation temperature difference is 2 DEG C ~ 30 DEG C, is preferably 5 DEG C ~ 20 DEG C；Or control operation pressure and operation temperature immediate two
In the operating condition of platform weighted BMO spaces reactor, volume space velocity difference is 0.1 h-1~10 h-1, it is preferably 0.2 h-1~5 h-1。
15. according to claim 1 method, wherein, according to Flow of Goods and Materials direction, loaded successively in each weighted BMO spaces reactor
Hydrogenation protecting agent, Hydrodemetalation catalyst and optional Hydrobon catalyst；The reaction in the hydrotreating reaction area
Device loads Hydrobon catalyst and hydrodenitrogeneration carbon residue reforming catalyst successively.
16. according to claim 1 method, wherein, boiling bed hydrogenation processing reaction zone sets the boiling bed hydrogenation reaction of 1 or more
Device is preferably provided with 1 or 2 boiling bed hydrogenation reactor being arranged in series.
17. according to claim 1 method, wherein, the reaction condition of boiling bed hydrogenation processing reaction zone is：Reaction temperature is 330
~450 DEG C, be preferably 360~430 DEG C；Reaction pressure is 8~25MPa, is preferably 10~16MPa；Hydrogen to oil volume ratio 300：1~
1000：1, it is preferably 600：1~900：1；Liquid volume air speed（LHSV）For 0.3 h-1~5.0h-1, it is preferably 0.3 h-1~
2.0h-1。
18. according to claim 1 method, wherein, the operating condition in the fixed bed hydrogenation pretreatment reaction area is：Temperature is
370 DEG C~420 DEG C, be preferably 380 DEG C~400 DEG C；Pressure is 10MPa~25MPa, is preferably 15MPa~20MPa；Hydrogen oil body
Product is preferably 500~800 than being 300~1500；Volume space velocity is 0.15h during raw material fluid-1~2h-1, it is preferably 0.3h-1~
1h-1。
19. according to claim 1 method, wherein, the fixed bed hydrogenation processing reaction zone include 1~5 it is being arranged in series plus
Hydrogen treatment reactor preferably includes 1~2 hydrotreating reactor being arranged in series.
20. according to claim 1 method, wherein, the operating condition of the fixed bed hydrogenation processing reaction zone is：Temperature is 370
DEG C~430 DEG C, it is preferably 380 DEG C~410 DEG C；Pressure is 10MPa~25MPa, is preferably 15MPa~20MPa；Hydrogen to oil volume ratio
For 300~1500, preferably 400~800；Volume space velocity is 0.15h during raw material fluid-1~0.8h-1, it is preferably 0.2h-1~
0.6h-1。
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109536205A (en) * | 2019-01-23 | 2019-03-29 | 陕西东鑫垣化工有限责任公司 | A kind of light tar mixes refining wax oil processing unit (plant) and method |
| CN109666510A (en) * | 2019-01-25 | 2019-04-23 | 内蒙古晟道催化技术有限公司 | The production method of big density boat coal, ultralow coagulation diesel oil and low solidifying special lubricating oil base oil |
| CN113149665A (en) * | 2021-04-08 | 2021-07-23 | 北京联合荣大工程材料股份有限公司 | Environment-friendly bonding agent and stemming for blast furnace |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20110210045A1 (en) * | 2005-12-16 | 2011-09-01 | c/o Chevron Corporation | Systems and Methods for Producing a Crude Product |
| CN102311786A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Residual oil hydrotreatment method for prolonging device operating cycle |
| CN102676218A (en) * | 2011-03-16 | 2012-09-19 | 中国石油化工股份有限公司 | Fixed bed residue oil hydrogenating process |
| CN103102940A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Combined process for hydrotreatment of heavy oil |
-
2016
- 2016-11-25 CN CN201611052155.5A patent/CN108102699B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20110210045A1 (en) * | 2005-12-16 | 2011-09-01 | c/o Chevron Corporation | Systems and Methods for Producing a Crude Product |
| CN102311786A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Residual oil hydrotreatment method for prolonging device operating cycle |
| CN102676218A (en) * | 2011-03-16 | 2012-09-19 | 中国石油化工股份有限公司 | Fixed bed residue oil hydrogenating process |
| CN103102940A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Combined process for hydrotreatment of heavy oil |
Non-Patent Citations (1)
| Title |
|---|
| 杨涛等: "沸腾床-固定床组合渣油加氢处理技术研究", 《炼油技术与工程》 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109536205A (en) * | 2019-01-23 | 2019-03-29 | 陕西东鑫垣化工有限责任公司 | A kind of light tar mixes refining wax oil processing unit (plant) and method |
| CN109666510A (en) * | 2019-01-25 | 2019-04-23 | 内蒙古晟道催化技术有限公司 | The production method of big density boat coal, ultralow coagulation diesel oil and low solidifying special lubricating oil base oil |
| WO2020151371A1 (en) * | 2019-01-25 | 2020-07-30 | 内蒙古晟道催化技术有限公司 | Method for producing high density aviation fuel, ultra-low freezing point diesel and low freezing point special lubricating oil base oil |
| CN113149665A (en) * | 2021-04-08 | 2021-07-23 | 北京联合荣大工程材料股份有限公司 | Environment-friendly bonding agent and stemming for blast furnace |
| CN113149665B (en) * | 2021-04-08 | 2022-06-14 | 北京联合荣大工程材料股份有限公司 | Environment-friendly bonding agent and stemming for blast furnace |
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