CN105441123B - Hydro carbons continuous reforming process - Google Patents
Hydro carbons continuous reforming process Download PDFInfo
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- CN105441123B CN105441123B CN201410414893.4A CN201410414893A CN105441123B CN 105441123 B CN105441123 B CN 105441123B CN 201410414893 A CN201410414893 A CN 201410414893A CN 105441123 B CN105441123 B CN 105441123B
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Abstract
The invention discloses a kind of hydro carbons continuous reforming process, it is characterised in that：The technique includes：Two reforming reactor groups and a regenerator are set, wherein, the first reforming reactor group includes three reforming reactors, and the second reforming reactor group only includes a reforming reactor；Wherein, reaction feed is that series connection is carried out relative to the conveying of each reactor in each reforming reactor group；And the circulation conveying between conveying and reactor group and regenerator of the catalyst between each reactor group is progress in parallel, but conveying of the catalyst in the first reforming reactor group is that series connection is carried out.In the present invention, all reactor groups can use fresh high activated catalyst and carry out on demand separately adjustable and change catalyst flow, can give full play to the activity of catalyst, improve the utilization rate of catalyst, improve reforming conversion and product yield.
Description
Technical field
The present invention relates to a kind of hydro carbons continuous reforming process.
Background technology
CONTINUOUS REFORMER is a kind of oil secondary operation technology, the raw material of processing be mainly the straight-run naphtha of low octane rating,
Hydrotreated naphtha etc., using platinum Pt- tin Sn bimetallic catalysts, at a high temperature of 500 DEG C or so, reset molecule, it is different
Structure, increase the yield of aromatic hydrocarbons, improve the technology of octane number.
Moving-burden bed reactor continuous regenerative reforming, abbreviation CONTINUOUS REFORMER.Commercial Application in the world is main at present
Three CONTINUOUS REFORMER patented technology providers are Uop Inc. of the U.S., French Axens and Chinese SEI respectively.Filled in CONTINUOUS REFORMER
Put, catalyst continuously flows successively through three (or four) moving-burden bed reactors of series connection, from the outflow of last reactor
Reclaimable catalyst carbon content is generally 2%-8% (mass fraction), and reclaimable catalyst is transported to regeneration by gravity or gas lift
Regenerated in device.Regenerated catalyst after activity recovery returns to first reactor and reacted again, catalyst shape in system
Into a closed cycle.
By reaction feed and catalyst transport model split, existing industrialized continuous reforming process can be divided into
" following current " and " adverse current " two kinds of patterns.
The reaction mass of " following current " continuous reforming process flows to most end reactor from first reactor successively, in each reactor
In catalyst on reacted.Moving direction of the catalyst between each reactor is consistent with reaction mass, that is, is regenerated
High activated catalyst be introduced into the first reforming reactor by the order of reaction stream, then pass sequentially through the second reforming reaction
Device, tri-reforming device are gradually reduced, from most until most end reforming reactor from first reactor to most end reactor pressure
The catalyst activity that last reactor comes out is relatively low, is sent in regenerator and is regenerated, and the catalyst after regeneration is lifted to the again
One reactor completes the circulation of catalyst.The technical process catalyst of this CONTINUOUS REFORMER is used in series in the reactor,
Catalyst into the first reforming reactor is the catalyst of " fresh " high activity just regenerated, and reactor below
All it is the above reactor relatively low catalyst of used activity.This process is schematically as follows：
The reaction that this catalyst circulation conveying mode makes it easy to carry out is in the reaction for having high activated catalyst above
Carried out in device, and the difficult reaction carried out having below is carried out in the reactor of low activity catalyst, catalyst reactor
The reaction complexity that activated state is carried out with it does not match that.The circulation arrangement of this catalyst is irrational.Such as accompanying drawing 1
It is shown.
The reaction mass of " adverse current " continuous reforming process flows to most end reactor from first reactor successively, and catalyst exists
Moving direction between each reactor is, that is, the order of the high activated catalyst back reaction logistics that regenerated opposite with reaction mass
Rearmost reactor is introduced into, then the direction of back reaction logistics is successively forward until first reactor, then anti-from first
Answer device to be sent in regenerator to be regenerated, the catalyst after regeneration lifts a last reactor and completes following for catalyst again
Ring.This process is schematically as follows：
The technical process of this adverse current CONTINUOUS REFORMER causes reaction of the difficult reaction carried out in high activated catalyst below
Carried out in device, reaction easy to perform is carried out in the reactor of low activity catalyst above.The circulation peace of this catalyst
It is more reasonable that row conveys compared to following current, and the activated state of catalyst reactor matches compared with its reaction carried out complexity.
As shown in Figure 2.
But either " following current " still " adverse current " CONTINUOUS REFORMER, circulation conveying of the catalyst between reactor are all adopted
With the mode of series connection, the catalyst that this mode of movement is only transported to first reactor from regenerator is only what is just regenerated
The high catalyst of " fresh " activity, such as first reforming reactor of " following current " CONTINUOUS REFORMER, " adverse current " CONTINUOUS REFORMER it is last
One reforming reactor, and the catalyst in other reforming reactors is all that above reactor is used containing carbon deposition activity
Decreased catalyst, catalyst convey in the backward, and its activity is lower, active minimum in the reactor that catalyst leaves.
The activity of catalyst can not give full play in all reactors as can be seen here.The mode of this catalyst cascade conveying, passes through
The catalyst internal circulating load of each reactor is all identical, all catalyst in each reactor must circular regeneration simultaneously, each
The catalyst flow of reactor can not on demand be carried out separately adjustable and changed, and can not individually carry out circular regeneration.
CN203513593U, which discloses a kind of regeneration CONTINUOUS REFORMER system, the system side by side, includes catalyst reformer
(relative to regenerator) and charging/effluent exchanger, heating furnace and the reactor being sequentially connected, catalyst reformer are provided with
For adjusting the regulating valve of catalyst circulation rate.Although the system because equipped with the regulating valve can according to response situation and
Catalyst coking situation adjusts catalyst circulation rate, but with regard to being still foregoing " suitable from the point of view of reaction feed and the flow direction of catalyst
The form of stream " continuous reforming process, the foregoing problems of " following current " continuous reforming process are not overcome.
The content of the invention
It is an object of the invention to provide a kind of hydro carbons continuous reforming process, each reactor group group is used fresh height
Active regeneration catalyst, and can be as needed independently adjusted and change the catalyst circulation in each group of reactor
Flow, to give full play to the activity of catalyst, improve the utilization rate of catalyst, there is provided the operability of device, improve reformation and turn
Rate and product yield.
To achieve these goals, the present invention provides a kind of hydro carbons continuous reforming process, it is characterised in that：The technique bag
Include：Two reforming reactor groups and a regenerator 14 are set, wherein the first reforming reactor group include three reactors i.e. according to
Feedstock direction is sequentially connected in series the first reforming reactor 3, the second reforming reactor 5 and tri-reforming device 7 of setting, the second weight
Whole reactor group is fourth reforming reactor 9 including a reactor；Wherein, reaction feed is relative to each reforming reactor group
In the conveying of each reactor be that series connection is carried out, i.e., reaction feed pass sequentially through the first reforming reactor 3, second reform it is anti-
Answer device 5, tri-reforming device 7 and fourth reforming reactor 9 and reacted with catalyst therein；And catalyst is each
The circulation conveying between conveying and reactor group and regenerator between reactor group be it is in parallel carry out, but catalyst is the
The conveying between the first reforming reactor 3, the second reforming reactor 5 and tri-reforming device 7 in one reforming reactor group
It is sequentially connected in series progress.
Preferably, the hydro carbons continuous reforming process, wherein, the technique also includes setting being located at the first reforming reactor 3
The one anti-top hopper 10 on top, the four anti-top hoppers 11 positioned at the top of fourth reforming reactor 9, regenerated catalyst reprocessing
Blower fan 15 is lifted with distribution system RCTS12, reclaimable catalyst reprocessing and distribution system WCTS13, regenerated catalyst and is treated
Raw catalyst lifting blower fan 16；Reaction feed is anti-by the first reforming reactor 3, the second reforming reactor 5, tri-reforming successively
Device 7 and fourth reforming reactor 9 are answered, leaves the reaction product of fourth reforming reactor 9 with reaction feed in reaction feed/product
Exchanged heat in heat exchanger 1, then arrive follow-up separator again and separated；Regenerated catalyst lifts blower fan 15 with regenerated catalyst
RCTS12 is promoted to from regenerator 14；RCTS12 by 2 tremie pipes respectively with an anti-10 and four anti-top hopper of top hopper
11 are connected, and an anti-top hopper 10 is connected by tremie pipe and the first reforming reactor 3, and four anti-top hoppers 11 pass through tremie pipe
It is connected with fourth reforming reactor 9；It is respectively that tri-reforming device 7 and fourth reforming is anti-with reclaimable catalyst lifting blower fan 16
The reclaimable catalyst in device 9 is answered to be promoted to WCTS13；WCTS13 is connected by 1 tremie pipe with regenerator 14.
Preferably, the hydro carbons continuous reforming process, wherein, the first reforming reactor 3, the second reforming reactor 5 and
Tri-reforming device 7 overlaps to be sequentially connected in series up and down, and the first reforming reactor 3 is in topmost, the second reforming reactor 5
In middle, tri-reforming device 7 in bottom；Between first reforming reactor 3 and the second reforming reactor 5 and second reforms
Beds between reactor 5 and tri-reforming device 7 have more diplegs to be connected, urging in the first reforming reactor
Agent can lean on gravity to enter the second reforming reactor through dipleg and then enter back into tri-reforming device.
Preferably, the hydro carbons continuous reforming process, wherein, regenerated catalyst is promoted to RCTS12 from regenerator 14 and entered
The elutriation of row dust, reduction and redistribution process, it is then defeated respectively by 2 tremie pipes from RCTS12 in a manner of parallel side-by-side
It is sent in the first reforming reactor 3 and fourth reforming reactor 9, the catalyst in the first reforming reactor 3 is again by gravity through material
Leg is sequentially entered in the second reforming reactor 5 and tri-reforming device 7；Regeneration from from RCTS12 to each reforming reactor group
The conveying capacity of catalyst and/or conveying opportunity are individually controllable.
Preferably, the hydro carbons continuous reforming process, wherein, in tri-reforming device 7 and fourth reforming reactor 9
Reclaimable catalyst in a manner of parallel side-by-side it is elevated be delivered in WCTS13 mixed, dust elutriation and locking become press through
Journey, regenerator 14 is then transported to by tremie pipe and regenerated；Urged from each reforming reactor group to the to be generated of WCTS13
The lifting conveying capacity of agent and/or conveying opportunity are all individually controllable.
Preferably, the hydro carbons continuous reforming process, wherein, RCTS12 operating pressure is less than the operation pressure of regenerator 14
Power, so as to which regenerated catalyst is lifted to RCTS12 from regenerator 14；The position of RCTS12 bottoms is higher than an anti-top material
The position on the top of 10 and four anti-top hopper 11 of bucket, and RCTS12 operating pressure is higher than the behaviour of the first reforming reactor 3
Make pressure, so that regenerated catalyst can be flowed into all reactors from RCTS12.
Preferably, the hydro carbons continuous reforming process, wherein, the position of WCTS13 bottoms is higher than the position on the top of regenerator 14
Put, it is two pressure areas that WCTS13, which is divided to, and the upper zone before transformation is low-pressure area, and pressure is less than fourth reforming reactor 9, can
So that reclaimable catalyst is lifted to the low-pressure area from tri-reforming device 7 and fourth reforming reactor 9；Under after the transformation
Area of portion is higher-pressure region, and pressure is higher than regenerator 14, and reclaimable catalyst can be flowed into regenerator 14 from the higher-pressure region.
The present invention is existing to overcome by changing circulation conveying mode of the catalyst between multiple moving-burden bed reactor groups
The shortcomings that each catalyst reactor activity can not give full play in industrialized technology, multiple reforming reactor groups in parallel
In catalyst can carry out cyclic regeneration simultaneously.Between reaction and regenerative system, by the way of parallel connection conveys catalyst,
So that the catalyst into each group of reactor is all high activity " fresh " catalyst for just having regenerated；Reclaimable catalyst is from each
Individually regenerative system is arrived in lifting in parallel to reactor group so that can to the catalyst of regenerator lifting conveying capacity from each reactor group
To be adjusted and change as needed, circulation conveying and the regeneration of catalyst can be neatly carried out, so as to optimize reaction
And regeneration condition, all reactors is used fresh high activated catalyst and is carried out on demand separately adjustable and change catalysis
Agent flux, carbon deposit on catalyst is reduced, to give full play to the activity of catalyst, improve the utilization rate of catalyst, extend catalyst
Life-span, reduce the inlet temperature of each reactor, the side reaction for reducing CONTINUOUS REFORMER occurs, and improves reforming conversion and product
Yield, increasing gasoline yield and hydrogen, increase the benefit.In CONTINUOUS REFORMER reaction, before all comparing of carrying out of two reactors
The reaction carried out is easier to, carbon deposit is few on catalyst, and activity decrease is less, can be directly entered the 3rd reactor and continue to answer
With so as to reduce the number of catalyst lifting.The reaction carried out in 3rd reactor is more difficult relative to the first two, leaves the 3rd
The catalyst carbon deposition of reactor is relatively more, and activity decrease is also more, and it is anti-that cyclization of paraffins dehydrogenation etc. is carried out in the 4th reactor
Should, reaction is most difficult to, and the present invention is existing to overcome by changing circulation conveying mode of the catalyst between multiple reforming reactors
The shortcomings that the 3rd, fourth reforming catalyst reactor activity can not give full play in industrialized technology.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Accompanying drawing is for providing a further understanding of the present invention, and a part for constitution instruction, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is existing downflow type hydro carbons continuous reforming process schematic flow sheet
Fig. 2 is existing reverse-flow hydro carbons continuous reforming process schematic flow sheet
Fig. 3 is the hydro carbons continuous reforming process schematic flow sheet according to the present invention
Description of reference numerals
The reaction heating furnace of 101 reaction feeds/product exchanger 102 first
The reaction heating furnace of 103 first reforming reactors (one is anti-) 104 second
The reaction heating furnace of 105 second reforming reactors (two is anti-) 106 the 3rd
The reaction heating furnace of 107 tri-reforming devices (three is anti-) 108 the 4th
The regenerated catalyst lifter of 109 fourth reforming reactors (four is anti-) 110
The 111 4 anti-anticatalyst lifters of top hopper 112 4
The 113 3 anti-anticatalyst lifters of top hopper 114 3
The 115 2 anti-anticatalyst lifters of top hopper 116 2
The 117 1 anti-reclaimable catalyst lifters of top hopper 118
The 119 separation regenerators of hopper 120
The reaction heating furnace of 201 reaction feeds/product exchanger 202 first
The reaction heating furnace of 203 first reforming reactors (one is anti-) 204 second
The reaction heating furnace of 205 second reforming reactors (two is anti-) 206 the 3rd
The reaction heating furnace of 207 tri-reforming devices (three is anti-) 208 the 4th
The regenerated catalyst lifter of 209 fourth reforming reactors (four is anti-) 210
The 211 4 anti-anticatalyst lifters of top hopper 212 4
The 213 3 anti-anticatalyst lifters of top hopper 214 3
The 215 2 anti-anticatalyst lifters of top hopper 216 2
The 217 1 anti-reclaimable catalyst lifters of top hopper 218
The 219 separation regenerators of hopper 220
The reaction heating furnace of 1 reaction feed/product exchanger 2 first
The reaction heating furnace of 3 first reforming reactor 4 second
The reaction heating furnace of 5 second reforming reactor 6 the 3rd
The reaction heating furnace of 7 tri-reforming device 8 the 4th
9 fourth reforming reactor, 10 1 anti-top hopper
The 11 4 anti-regenerated catalyst of top hopper 12 reprocessing and distribution system
(RCTS)
13 reclaimable catalysts are reprocessed and the regenerator of distribution system (WCTS) 14
15 regenerated catalysts lifting blower fan 16 reclaimable catalyst lifting blower fan
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The present invention provides a kind of hydro carbons continuous reforming process, it is characterised in that：The technique includes：Two reforming reactions are set
Device group and a regenerator 14, wherein the first reforming reactor group includes three reactors is sequentially connected in series setting according to feedstock direction
The first reforming reactor 3, the second reforming reactor 5 and tri-reforming device 7, the second reforming reactor group include one it is anti-
Answer device i.e. fourth reforming reactor 9；Wherein, reaction feed relative to each reactor in each reforming reactor group conveying
It is that series connection is carried out, i.e., reaction feed passes sequentially through the first reforming reactor 3, the second reforming reactor 5, tri-reforming device
7 and fourth reforming reactor 9 and reacted with catalyst therein；And conveying of the catalyst between each reactor group with
And the circulation conveying between reactor group and regenerator be it is in parallel carry out, but catalyst in the first reforming reactor group the
Conveying between one reforming reactor 3, the second reforming reactor 5 and tri-reforming device 7 is sequentially connected in series progress.
According to the hydro carbons continuous reforming process of the present invention, wherein used various process conditions, including feedstock oil, made
Catalyst, the operating condition of reactor, operating condition of regenerator etc. be all it is well known to those of ordinary skill in the art,
There is no particular limitation to it by the present invention.
For example, described catalyst can contain primary activity component noble metal platinum (Pt) etc., cocatalyst component tin
And the aluminum oxide of rhenium (Re) etc. and acid carrier etc. and other adjuvants, but not limited to this (Sn).The operation of each reactor
Condition can be independently, but be not limited to：0.1~1.5MPa of reaction pressure, preferably 0.2~1.0MPa；(raw material enters reaction temperature
Mouthful temperature) 400~550 DEG C, preferably 480-520 DEG C；Hydrogen-oil ratio (mol ratio) 0.1~10.0, preferably 1.0~5.0；Weight space velocity
For 0.5~5, preferably 1.5~3.Described feedstock oil may be, but not limited to,：Straight-run naphtha, the hydrogenation stone of low octane rating
Cerebrol etc..
According to the hydro carbons continuous reforming process of the present invention, the continuous reforming reactor is those skilled in the art institute
Well known moving-burden bed reactor；Described regenerator is used to make the reclaimable catalyst by reaction inactivation realize cyclic regeneration, wraps
Include by burning, oxychlorination, drying (or roasting), the technique such as reduction make the high reclaimable catalyst activity recovery of carbon content, regenerate
The quantity of device is preferably one, can also set again one it is standby.
According to the hydro carbons continuous reforming process of the present invention, wherein, the technique also includes setting being located at the first reforming reactor 3
The one anti-top hopper 10 on top, the four anti-top hoppers 11 positioned at the top of fourth reforming reactor 9, regenerated catalyst reprocessing
Blower fan 15 is lifted with distribution system RCTS12, reclaimable catalyst reprocessing and distribution system WCTS13, regenerated catalyst and is treated
Raw catalyst lifting blower fan 16；Reaction feed is anti-by the first reforming reactor 3, the second reforming reactor 5, tri-reforming successively
Device 7 and fourth reforming reactor 9 are answered, leaves the reaction product of fourth reforming reactor 9 with reaction feed in reaction feed/product
Exchanged heat in heat exchanger 1, then arrive follow-up separator again and separated；Regenerated catalyst lifts blower fan 15 with regenerated catalyst
RCTS12 is promoted to from regenerator 14；RCTS12 by 2 tremie pipes respectively with an anti-10 and four anti-top hopper of top hopper
11 are connected, and an anti-top hopper 10 is connected by tremie pipe and the first reforming reactor 3, and four anti-top hoppers 11 pass through tremie pipe
It is connected with fourth reforming reactor 9；It is respectively that tri-reforming device 7 and fourth reforming is anti-with reclaimable catalyst lifting blower fan 16
The reclaimable catalyst in device 9 is answered to be promoted to WCTS13；WCTS13 is connected by 1 tremie pipe with regenerator 14.
According to the hydro carbons continuous reforming process of the present invention, the regenerated catalyst reprocessing and distribution system RCTS can be right
Regenerated catalyst carries out dust elutriation, reduction and reallocation, is then sent to respectively by tremie pipe in a manner of parallel side-by-side each
It is used for chemical reaction process in individual reforming reactor.
According to the hydro carbons continuous reforming process of the present invention, the reclaimable catalyst reprocessing and distribution system WCTS can be right
Reclaimable catalyst is mixed, dust elutriation and locking transformation, is then delivered to regenerator by tremie pipe and is regenerated.
According to the hydro carbons continuous reforming process of the present invention, those skilled in the art are it is appreciated that reaction feed can be with
First exchanged heat with reaction product, then successively and alternately enter heating furnace and reactor below, reaction product leaves heat exchange
Follow-up separator is arrived after device again to be separated.
According to the hydro carbons continuous reforming process of the present invention, the catalyst after regeneration is lifted to RCTS, Ran Houtong from regenerator
Tremie pipe is crossed to be respectively delivered to be chemically reacted in each reactor by catalyst.Leave the reclaimable catalyst difference of each reactor
Lifting is delivered to WCTS, and being then delivered to regenerator by tremie pipe is regenerated.
Embodiment
The present embodiment combination accompanying drawing 3 illustrates to a kind of embodiment provided by the invention.By carried out
It is prolonged commerical test, wherein described various process conditions allow to have about ± 10% fluctuation.
As shown in figure 3, reaction feed exchanged heat in reaction feed/product exchanger 1 with reaction product after successively by the
One reaction heating furnace 2, the first reforming reactor 3, the second reaction heating furnace 4, the second reforming reactor 5, the 3rd reaction heating furnace
6th, tri-reforming device 7, the 4th reaction heating furnace 8 and fourth reforming reactor 9, reaction product leave fourth reforming reactor
After 9, exchanged heat in reaction feed/product exchanger 1 with reaction feed, then arrive follow-up separator again and separated.Instead
Thing is answered to produce pressure drop in flow process, the order of reactor operating pressure from high to low is：First reforming reactor 3,
Two reforming reactors 5, tri-reforming device 7 and fourth reforming reactor 9.
Regenerator 14 regeneration after catalyst by regenerated catalyst lifted blower fan 15 with nitrogen from regenerator 14 lifted to
RCTS12.Carry out the dust elutriation of catalyst first in RCTS12, then reusable heat hydrogen is to the catalyst after removing dust
Reduced, the nitrogen after removing dust is sent to regenerated catalyst lifting blower fan 15 as regenerated catalyst lifting nitrogen circulation
Use.Catalyst after reduction has respectively entered an anti-10 and four anti-top hopper of top hopper by gravity by 2 tremie pipes
11, corresponding first reforming reactor 3 and fourth reforming reactor 9 then are respectively enterd by gravity again, is reformed into first anti-
Answer the catalyst of device 3 to flow through after beds participate in reformate chemical reaction and pass sequentially through the second reforming reactor 5 by gravity again
With tri-reforming device 7, catalyst participates in chemical reaction process in each reactor.It is used in reactor group each
The catalyst of the high activity just regenerated.Catalyst flow control device can be set on the tremie pipe or top hopper,
The flow for entering the regenerated catalyst in each reactor is controlled or even dammed to realize.In two groups of reactors, first
The operating pressure highest of reforming reactor, in order that RCTS12 catalyst can enter each group reactor, RCTS12 pressure is high
In an anti-reforming reactor 3 of top hopper 10 and first.
Reclaimable catalyst lifts blower fan 16 with nitrogen respectively from tri-reforming device 7 and fourth reforming by reclaimable catalyst
Reactor 9 lifts the top low-pressure area for being delivered to WCTS13, and the operating pressure of WCTS low-pressure areas is less than fourth reforming reactor 9,
It is independent from each reactor group to the lifting conveying of the catalyst of regenerator, lifting conveying can be changed as needed
Amount.Catalyst is mixed first in WCTS13, then carries out the dust elutriation of catalyst again, removes the nitrogen after dust
Pneumatic transmission is used to reclaimable catalyst lifting blower fan 16 as reclaimable catalyst lifting nitrogen circulation, and powder is removed in WCTS13 low-pressure areas
Catalyst after dirt carries out locking boosting again, and subsequently into the higher-pressure region of WCTS13 bottom, the operating pressure of higher-pressure region is high
Catalyst in regenerator 14, higher-pressure region is delivered to regenerator 14 by tremie pipe and regenerated, and the pressure of regenerator 14 is high
In RCTS12, the catalyst for leaving regenerator is promoted to RCTS12, so far completes the conveying circulation of catalyst.
The present embodiment carries out cycloalkanes dehydrogenation, cyclization of paraffins dehydrogenation, different in the hydrogen gas atmosphere using C6~C12 naphthas hydro carbons
Structure and the reaction such as it is hydrocracked, hydrogen/oil ratio 2.1 of reaction raw materials, it is 58/30/12 (wt%) that P/N/A, which is formed, and inlet amount is
600000 tons/year, the time of CONTINUOUS REFORMER is 1 year.Reaction feed naphtha and the reacted charging of hydrogen mixture/product heat exchange
After device 1 exchanges heat, reformed successively by the first reaction heating furnace 2, the first reforming reactor 3, the second reaction heating furnace 4, second anti-
Answer device 5, the 3rd reaction heating furnace 6, tri-reforming device 7, the 4th reaction heating furnace 8, fourth reforming reactor 9, reaction production
Thing exchanges heat after leaving fourth reforming reactor 9 in reaction feed/product exchanger 1 with reaction feed, then arrives follow-up again
Separator is separated.The inlet pressure 0.56MPa (g) of first reforming reactor 3, the inlet pressure of the second reforming reactor 5
0.51MPa (g), the inlet pressure 0.42MPa (g) of tri-reforming device 7, the inlet pressure 0.35MPa of fourth reforming reactor 9
(g) it is 2.1, to react weight space velocity, and the inlet temperature of each reactor is 513 DEG C.
Used catalyst contains noble metal platinum (Pt) and tin for Research Institute of Petro-Chemical Engineering (RIPP) exploitation
(Sn) and other adjuvants PS-VI continuous reforming catalysts.The catalyst phosphorus content after regenerator 14 regenerates is left to be less than
0.2% (wt), lifted by regenerated catalyst lifting blower fan 15 with nitrogen from regenerator 14 to RCTS12.Enter first in RCTS12
The dust elutriation of row catalyst, reusable heat hydrogen reduce to the catalyst after removing dust, remove the nitrogen after dust
It is sent to regenerated catalyst lifting blower fan 15 to use as regenerated catalyst lifting nitrogen circulation, the operating pressure of RCTS12 reducing zones
For 0.58MPa (g), 0.02MPa (g) higher than the first reforming reactor.Catalyst after reduction leaves by gravity through 2 tremie pipes
An anti-10 and four anti-top hopper 11 of top hopper is had respectively entered after RCTS12, then respectively enters corresponding by gravity again
One reforming reactor 3 and fourth reforming reactor 9, the catalyst into the first reforming reactor 3 flow through beds participation
The second reforming reactor 5 and tri-reforming device 7 are passed sequentially through by gravity again after reformate chemical reaction, catalyst is each anti-
Answer and chemical reaction process is participated in device, used in each reactor group is the catalyst of the high activity just regenerated.
The carbon deposition quantity for leaving the reclaimable catalyst of each group reactor is 2.8%~3.3% (wt).Reclaimable catalyst is by be generated
Catalyst lifts blower fan 16 and is delivered to WCTS13 from tri-reforming device 7 and the lifting of fourth reforming reactor 9 respectively with nitrogen
Top low-pressure area, the operating pressure of WCTS13 tops low-pressure area is 0.30MPa, than 9 low 0.05MPa of fourth reforming reactor.
Independently carried out from each reactor group to the lifting conveying of WCTS13 catalyst, each group reaction can be changed as needed
The catalyst lifting conveying capacity of device, can also carry out individually lifting conveying to the reclaimable catalyst in single group reactor, can ground
Flexibly carry out the circulation conveying of catalyst.Catalyst is mixed first in WCTS13 low-pressure areas, is then catalyzed again
The dust elutriation of agent, remove dust after nitrogen be sent to reclaimable catalyst lifting blower fan 16 as reclaimable catalyst lifting nitrogen
Recycle, the catalyst after removing dust carries out locking boosting again, and the catalyst after locking is boosted enters under WCTS13
The higher-pressure region in portion, the operating pressure of higher-pressure region is 0.68MPa, and the reclaimable catalyst of higher-pressure region is delivered to regenerator by tremie pipe
14 are regenerated, and the operating pressure of regenerator is 0.65MPa (g), and the catalyst after regeneration is lifted again is delivered to RCTS12, are completed
The circulation of catalyst.
Hydro carbons continuous reforming process of the present invention is by the way of the conveying of catalyst parallel circulating so that enters each reactor
The catalyst of group is all " fresh " catalyst just regenerated, and the average carbon deposition quantity of reactor is low, and the effect of catalyst can more obtain
Give full play to.The catalyst higher with the activity just regenerated into the reaction in each reactor group contacts, and reduces bed
About 4~5 DEG C of mean temperature, the side reaction such as it is hydrocracked so as to reduce, and reduces the carbon distribution on catalyst, extends the longevity of catalyst
Life.
Under identical operating mode, operation and reaction condition, hydro carbons continuous reforming process of the present invention and existing work
The CONTINUOUS REFORMER technology of industry is compared and adds gasoline products yield 0.8%, C5 +Liquid yield increase by 0.9%, hydrogen yield increases
Add 2.0%.For the catalytic reforming unit that a set for the treatment of capacity is 1,000,000 tons/year, annual 0.8 ten thousand tons of increasing gasoline yield, increase
Add into 24,000,000 yuan.Annual 700 tons of hydrogen of volume increase, 7,000,000 yuan of increase income.
Because in the present embodiment, the operating mode of continuous reforming process of the present invention and existing industrial continuous reforming process uses
Identical air speed and identical catalyst filling ratio, i.e., the operating mode of continuous reforming process of the present invention do not optimize.It is if excellent
Changed the reaction condition (such as catalyst filling ratio) of continuous reforming process of the present invention, then can reduce catalyst filling amount or
Liquid yield is further improved, is increased the benefit.
Claims (4)
- A kind of 1. hydro carbons continuous reforming process, it is characterised in that：The technique includes：Two reforming reactor groups and one are set again Raw device (14), wherein it is to be sequentially connected in series the first of setting according to feedstock direction to reform that the first reforming reactor group, which includes three reactors, Reactor (3), the second reforming reactor (5) and tri-reforming device (7), the second reforming reactor group include a reactor That is fourth reforming reactor (9)；Wherein, reaction feed is relative to the conveying of each reactor in each reforming reactor group What series connection was carried out, i.e., reaction feed passes sequentially through the first reforming reactor (3), the second reforming reactor (5), tri-reforming Device (7) and fourth reforming reactor (9) are simultaneously reacted with catalyst therein；And catalyst is between each reactor group Conveying and the circulation conveying between reactor group and regenerator are progress in parallel, but catalyst is in the first reforming reactor group In the first reforming reactor (3), the conveying between the second reforming reactor (5) and tri-reforming device (7) be to go here and there successively What connection was carried out；The technique, which also includes setting, is located at an anti-top hopper (10) on the first reforming reactor (3) top, positioned at fourth reforming The four anti-top hoppers (11) on reactor (9) top, regenerated catalyst is reprocessed and distribution system RCTS (12), reclaimable catalyst Reprocessing and distribution system WCTS (13), regenerated catalyst lifting blower fan (15) and reclaimable catalyst lifting blower fan (16)；Instead It should feed and pass through the first reforming reactor (3), the second reforming reactor (5), tri-reforming device (7) and fourth reforming successively Reactor (9), the reaction product of fourth reforming reactor (9) is left with reaction feed in reaction feed/product exchanger (1) Heat exchange, then arrives follow-up separator and is separated again；Regenerated catalyst lifts blower fan (15) from regeneration with regenerated catalyst Device (14) is promoted to RCTS (12)；RCTS (12) is expected with an anti-top hopper (10) and four anti-tops respectively by 2 tremie pipes Bucket (11) is connected, and an anti-top hopper (10) is connected by tremie pipe and the first reforming reactor (3), four anti-top hoppers (11) It is connected by tremie pipe and fourth reforming reactor (9)；With reclaimable catalyst lifting blower fan (16) respectively by tri-reforming Reclaimable catalyst in device (7) and fourth reforming reactor (9) is promoted to WCTS (13)；WCTS (13) by 1 tremie pipe with Regenerator (14) is connected；Regenerated catalyst is promoted to the elutriation of RCTS (12) progress dust, reduction from regenerator (14) and divided again With process, the first reforming reactor is then transported to respectively from RCTS (12) by 2 tremie pipes in a manner of parallel side-by-side (3) and in fourth reforming reactor (9), catalyst in the first reforming reactor (3) sequentially enters the by gravity through dipleg again In two reforming reactors (5) and tri-reforming device (7)；From RCTS (12) to the regenerated catalyst of each reforming reactor group Conveying capacity and/or conveying opportunity be individually controllable；Treated in tri-reforming device (7) and fourth reforming reactor (9) Raw catalyst in a manner of parallel side-by-side it is elevated be delivered in WCTS (13) mixed, dust elutriation and locking become and pressed through Journey, regenerator (14) is then transported to by tremie pipe and regenerated；Treated from each reforming reactor group to WCTS (13) The lifting conveying capacity of raw catalyst and/or conveying opportunity are all individually controllable.
- 2. hydro carbons continuous reforming process according to claim 1, wherein, the first reforming reactor (3), the second reforming reactor (5) overlapped with tri-reforming device (7) to be sequentially connected in series up and down, the first reforming reactor (3) is in topmost, the second weight Whole reactor (5) is in middle, tri-reforming device (7) in bottom；First reforming reactor (3) and the second reforming reactor (5) beds between and between the second reforming reactor (5) and tri-reforming device (7) have more diplegs to be connected Connect, gravity can be leaned on through dipleg to enter the second reforming reactor for the catalyst in the first reforming reactor and then to enter back into the triple Whole reactor.
- 3. according to the hydro carbons continuous reforming process of claim 1 or 2, wherein, RCTS (12) operating pressure is less than regenerator (14) operating pressure, so as to which regenerated catalyst is lifted to RCTS (12) from regenerator (14)；RCTS (12) bottom Position is higher than the position on the top of an anti-top hopper (10) and four anti-top hoppers (11), and RCTS (12) operating pressure Higher than the operating pressure of the first reforming reactor (3) so that regenerated catalyst can be flowed into from RCTS (12) it is all Reactor.
- 4. according to the hydro carbons continuous reforming process of claim 1 or 2, wherein, the position of WCTS (13) bottom is higher than regenerator (14) position on top, WCTS (13) are divided into two pressure areas, and the upper zone before transformation is low-pressure area, and pressure is less than the 4th Reforming reactor (9), reclaimable catalyst can be lifted to this from tri-reforming device (7) and fourth reforming reactor (9) Low-pressure area；Lower region after transformation is higher-pressure region, and pressure is higher than regenerator (14), and reclaimable catalyst can be from the higher-pressure region It is flowed into regenerator (14).
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1530427A (en) * | 2003-03-11 | 2004-09-22 | A New Approach to Regeneration | |
| CN1715371A (en) * | 2004-06-29 | 2006-01-04 | 中国石油化工股份有限公司 | Parallel-flow catalytic reforming processing method for multiple movable bed reactors |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1530427A (en) * | 2003-03-11 | 2004-09-22 | A New Approach to Regeneration | |
| CN1715371A (en) * | 2004-06-29 | 2006-01-04 | 中国石油化工股份有限公司 | Parallel-flow catalytic reforming processing method for multiple movable bed reactors |
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