CN105349180B - Hydro carbons continuous reforming process - Google Patents
Hydro carbons continuous reforming process Download PDFInfo
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- CN105349180B CN105349180B CN201410414891.5A CN201410414891A CN105349180B CN 105349180 B CN105349180 B CN 105349180B CN 201410414891 A CN201410414891 A CN 201410414891A CN 105349180 B CN105349180 B CN 105349180B
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Abstract
The invention discloses a kind of hydro carbons continuous reforming process, the technique includes：At least two reforming reactors and at least one catalyst regenerator are set, it is characterised in that：Conveying of the reaction feed relative to each reforming reactor is that series connection is carried out, and circulation conveying of the catalyst between reactor and regenerator is in parallel carry out.In the present invention, all reactors 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, make molecule occur reset, it is different
Structure, increases the yield of aromatic hydrocarbons, improves 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., France Axens and China SEI respectively.In continuous reformer
In, catalyst continuously flows successively through three (or four) moving-burden bed reactors of series connection, is flowed out from last reactor
Reclaimable catalyst carbon content is generally 2%-8% (mass fraction), and reclaimable catalyst is transported to regeneration by gravity or gas lift
Device is regenerated.Regenerated catalyst after activity recovery returns to first reactor and reacted again, and catalyst is formed in system
One 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 until most end reforming reactor from first reactor to most end reactor pressure, from most
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 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 that just regenerated " fresh " high activity, and reactor below
All it is the above reactor relatively low catalyst of used activity.This process is schematically as follows：
This catalyst circulation conveying mode makes it easy to the reaction carried out 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 is not matched 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 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 the difficult reaction carried out in the reaction of 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 is compared matching with the reaction complexity that it is carried out.
As shown in Figure 2.
But either " following current " still " adverse current " CONTINUOUS REFORMER, circulation conveying of the catalyst between reactor all adopt
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 is conveyed 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 be all catalyst in identical, each reactor must circular regeneration simultaneously, each
The catalyst flow of reactor can not on demand be carried out separately adjustable and changed, it is impossible to individually carry out circular regeneration.
CN 203513593U disclose a kind of regeneration CONTINUOUS REFORMER system side by side, and the system includes catalyst reformer
(relative to regenerator) and charging/effluent exchanger, heating furnace and the reactor being sequentially connected, catalyst reformer is provided with
Regulating valve for adjusting 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, all reactors are made to use fresh high activity
Regenerated catalyst, and can independently as required adjust and change the catalyst internal circulating load in each reactor, to fill
The activity of catalyst is waved in distribution, improves the utilization rate of catalyst, improves the operability of device, improves reforming conversion and product
Yield.
To achieve these goals, the present invention provides a kind of hydro carbons continuous reforming process, and the technique includes：Set at least two
Individual reforming reactor and at least one catalyst regenerator, it is characterised in that：Reaction feed is relative to each reforming reactor
Conveying is that series connection is carried out, i.e., reaction feed passes sequentially through each reforming reactor and reacted with catalyst therein；And
Circulation conveying of the catalyst between reactor and regenerator is that parallel connection is carried out, i.e., reacted in each reforming reactor
Reclaimable catalyst, which is all individually delivered in regenerator, carries out cyclic regeneration, and the regenerated catalyst after regenerating is transported to by parallel connection
Reaction is reused in each reforming reactor.
Preferably, the hydro carbons continuous reforming process, the technique also includes：Independently control from each reforming reactor
Conveying capacity and/or conveying opportunity to the reclaimable catalyst of regenerator, and independently control to reform from regenerator to each
The conveying capacity of the regenerated catalyst of reactor and/or conveying opportunity.
Preferably, the hydro carbons continuous reforming process, the technique also includes：Reclaimable catalyst is set to reprocess and distribution system
Unite WCTS, and the reclaimable catalyst in each reforming reactor is elevated in the way of parallel side-by-side to be delivered to the WCTS,
Mixed in WCTS, dust elutriation and locking transformation process, be then transferred to that regenerator is interior to be regenerated；And set again
Raw catalyst reprocessing and distribution system RCTS, regenerated catalyst are promoted to the elutriation of RCTS progress dust from regenerator, gone back
Former and redistribution process, then in the way of parallel side-by-side from RCTS be respectively delivered to each reforming reactor in be used for chemistry
Course of reaction.
Preferably, the hydro carbons continuous reforming process, wherein, the technique includes, and sets four reforming reactors and one
Regenerator, i.e. the first reforming reactor 3, the second reforming reactor 5, tri-reforming device 7, fourth reforming reactor 9 and again
Raw device 14, and the technique also includes setting regenerated catalyst reprocessing and distribution system RCTS15, reclaimable catalyst are reprocessed
With distribution system WCTS16, reclaimable catalyst lifting blower fan 17 and regenerated catalyst lifting blower fan 18；Reaction feed is passed through successively
Cross the first reforming reactor 3, the second reforming reactor 5, tri-reforming device 7 and fourth reforming reactor 9；Regenerated catalyst
Blower fan 18, which is lifted, with regenerated catalyst is promoted to RCTS15 from regenerator 14；RCTS respectively with first, second, third and fourth weight
Whole reactor 3,5,7 is connected with 9；Blower fan 17 is lifted by first, second, third and fourth reforming reaction with reclaimable catalyst
Reclaimable catalyst in device 3,5,7 and 9 is promoted to WCTS16 respectively；WCTS16 is connected by 1 tremie pipe with regenerator 14.
Preferably, the hydro carbons continuous reforming process, wherein, regenerated catalyst is promoted to RCTS15 from regenerator 14 and entered
The elutriation of row dust, reduction and redistribution process, are then conveyed respectively in the way of parallel side-by-side from RCTS15 by tremie pipe
It is used for chemical reaction process into each reforming reactor；From RCTS15 to the conveying of the regenerated catalyst of each reforming reactor
Measure and/or conveying opportunity is individually controllable.
Preferably, the hydro carbons continuous reforming process, wherein, first, second, third and fourth reforming reactor 3,5,7,
Reclaimable catalyst in 9 is elevated in the way of parallel side-by-side to be delivered to WCTS16, is mixed in WCTS16, dust elutriation
With locking transformation process, regenerator 14 is then delivered to by tremie pipe and regenerated；From each reforming reactor to WCTS16
Reclaimable catalyst lifting conveying capacity and/or conveying opportunity be individually controllable.
Preferably, the hydro carbons continuous reforming process, wherein, RCTS15 operating pressure is less than the operation pressure of regenerator 14
Power, so as to which catalyst is lifted to RCTS15 from regenerator；The position of RCTS15 bottoms is higher than each reactor top simultaneously
Position, RCTS15 operating pressure is higher than the operating pressure of the first reforming reactor 3 so that catalyst can flow from RCTS15
Enter to all reforming reactors.
Preferably, the hydro carbons continuous reforming process, wherein, the position of WCTS16 bottoms is higher than the position on the top of regenerator 14
Put, WCTS16 is divided to for two pressure areas, 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 fourth reforming reactor 9；Lower region after transformation is higher-pressure region, pressure
Higher than regenerator 14, reclaimable catalyst can be flowed into regenerator 14 from the higher-pressure region.
The present invention overcome by changing circulation conveying mode of the catalyst between multiple moving-burden bed reactors it is existing
Through the shortcoming that each catalyst reactor activity can not give full play in industrialized technology, in multiple reforming reactors in parallel
Catalyst can carry out cyclic regeneration simultaneously.Between reaction and regenerative system, by the way of parallel connection conveying catalyst, make
The catalyst that each reactor must be entered is high activity " fresh " catalyst just regenerated；Reclaimable catalyst is from each anti-
Answering device, individually regenerative system is arrived in lifting in parallel so that can basis to the catalyst of regenerator lifting conveying capacity from each reactor
Need to be adjusted and change, can neatly carry out circulation conveying and the regeneration of catalyst, so as to optimize reaction and regenerate
Condition, makes all reactors to use fresh high activated catalyst and carry out on demand separately adjustable and change catalyst stream
Amount, reduces carbon deposit on catalyst, to give full play to the activity of catalyst, improves the utilization rate of catalyst, extends the longevity of catalyst
Life, reduces the inlet temperature of each reactor, and the side reaction for reducing CONTINUOUS REFORMER occurs, so as to improve reforming conversion and product
Yield, increasing gasoline yield and hydrogen, increase the benefit.
Other features and advantages of the present invention will be described in detail in subsequent embodiment part.
Brief description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute a part for specification, 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 reactors (one is anti-) 4 second
The reaction heating furnace of 5 second reforming reactors (two is anti-) 6 the 3rd
The reaction heating furnace of 7 tri-reforming devices (three is anti-) 8 the 4th
The anti-top hopper of 9 fourth reforming reactors (four is anti-) 10 1
The 11 2 anti-anti- top hoppers of top hopper 12 3
The 13 4 anti-regenerators of top hopper 14
15 regenerated catalysts are reprocessed and distribution system (RCTS)
16 reclaimable catalysts are reprocessed and distribution system (WCTS)
17 reclaimable catalysts lifting blower fan 18 regenerated 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, and the technique includes：At least two reforming reactors and extremely are set
A few catalyst regenerator, it is characterised in that：Conveying of the reaction feed relative to each reforming reactor is that series connection is carried out,
I.e. reaction feed passes sequentially through each reforming reactor and reacted with catalyst therein；And catalyst is in reactor and again
Circulation conveying between raw device is that the reacted reclaimable catalyst in progress in parallel, i.e., each reforming reactor is independent
It is delivered in regenerator and carries out cyclic regeneration, and the regenerated catalyst after regenerating is transported in each reforming reactor by parallel connection
It is reused for reaction.
According to the hydro carbons continuous reforming process of the present invention, the various process conditions employed in it, 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
(Sn) and rhenium (Re) etc. and acid carrier aluminum oxide etc. and other adjuvants, but not limited to this.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, described reforming reactor is that those skilled in the art institute is ripe
The moving-burden bed reactor known；Moving-burden bed reactor can be 2~6 series connection, preferably 3~4 series connection；Described regenerator
For making the reclaimable catalyst by reaction inactivation realize cyclic regeneration, including by burning, oxychlorination, drying (or roasting),
The techniques such as reduction make the high reclaimable catalyst activity recovery of carbon content, and the quantity of regenerator is preferably one, can also set again
One standby.
According to a kind of specific embodiment of the present invention, the hydro carbons continuous reforming process includes setting four to reform instead
Answer device and a regenerator, i.e. the first reforming reactor 3, the second reforming reactor 5, tri-reforming device 7, fourth reforming anti-
Device 9 and regenerator 14 are answered, and the technique also includes setting regenerated catalyst to reprocess and distribution system RCTS15, catalysis to be generated
Agent reprocessing and distribution system WCTS16, reclaimable catalyst lifting blower fan 17 and regenerated catalyst lifting blower fan 18；React into
Material sequentially passes through the first reforming reactor 3, the second reforming reactor 5, tri-reforming device 7 and fourth reforming reactor 9；Again
Raw catalyst regenerated catalyst lifting blower fan 18 is promoted to RCTS15 from regenerator 14；RCTS15 is respectively with first, second,
Three and fourth reforming reactor 3,5,7 be connected with 9；Blower fan 17 is lifted by first, second, third and fourth with reclaimable catalyst
Reclaimable catalyst in reforming reactor 3,5,7 and 9 is promoted to WCTS16 respectively；WCTS16 passes through 1 tremie pipe and regenerator
14 are connected.
According to the hydro carbons continuous reforming process of the present invention, regenerated catalyst reprocessing and distribution system RCTS15 can be with
Dust elutriation, reduction are carried out to regenerated catalyst and is reallocated, is then sent to respectively by tremie pipe in the way of parallel side-by-side
It is used for chemical reaction process in each reforming reactor.
According to the hydro carbons continuous reforming process of the present invention, reclaimable catalyst reprocessing and distribution system WCTS16 can be with
Reclaimable catalyst is mixed, dust elutriation and locking transformation, regenerator is then delivered to by tremie pipe and regenerated.
According to the hydro carbons continuous reforming process of the present invention, those skilled in the art 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 from regenerator lifting to RCTS15, then
Catalyst is respectively delivered to by tremie pipe to be chemically reacted in each reactor.Leave the reclaimable catalyst of each reactor
Lifting is delivered to WCTS16 respectively, and being then delivered to regenerator by tremie pipe is regenerated.
Embodiment
A kind of embodiment that 3 couples of present invention of the present embodiment combination accompanying drawing are provided is illustrated.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 in reaction feed/product exchanger 1 with sequentially passing through the after reaction product heat exchange
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 reactor 9 in reaction
Exchange heat with reaction feed in charging/product exchanger 1 and then arrive follow-up separator again and separated.Reaction mass is in flowing
During produce pressure drop, the order of reactor operating pressure from high to low is：First reforming reactor 3, the second reforming reaction
Device 5, tri-reforming device 7 and fourth reforming reactor 9.Catalyst after the regeneration of regenerator 14 is lifted by regenerated catalyst
Blower fan 18 is lifted to RCTS15 with nitrogen from regenerator 14.Carry out the dust elutriation of catalyst, Ran Houzai first in RCTS15
The catalyst after removing dust is reduced with hot hydrogen, the nitrogen after removing dust is sent to regenerated catalyst lifting blower fan
18 use as regenerated catalyst lifting nitrogen circulation.RCTS15 pressure is reformed anti-higher than an anti-top hopper 10 and first
Device 3 is answered, the catalyst after reduction respectively enters each reactor top hopper 10 by gravity by 4 tremie pipes, 11,12,13, most
Enter again by gravity afterwards and chemically reacted in corresponding reactor 3,5,7,9.Used in each reactor is all firm regeneration
The catalyst for the high activity crossed.Catalyst flow control device can be set on the tremie pipe or top hopper, to realize
The flow for entering the regenerated catalyst in each reactor is controlled or even dammed.Nitrogen is used with reclaimable catalyst lifting blower fan 17
Gas lifts reclaimable catalyst on the top low-pressure area for being delivered to WCTS16, WCTS16 from each reforming reactor 3,5,7,9 respectively
The operating pressure of portion's low-pressure area is less than fourth reforming reactor 9, is from each reactor to the lifting conveying of WCTS catalyst
Independent, and it is controllable to lift conveying capacity, can change the lifting conveying capacity of reclaimable catalyst as needed.
In WCTS16 top low-pressure area, catalyst is mixed first, the dust elutriation of catalyst is then carried out again, dust is removed
Nitrogen afterwards is sent to reclaimable catalyst lifting blower fan 17 and used as reclaimable catalyst lifting nitrogen circulation, after removing dust
Catalyst carry out locking transformation again, the catalyst after boosting enters back into WCTS16 bottom higher-pressure region, the operation pressure of higher-pressure region
Power is higher than regenerator 14, and the catalyst after boosting is delivered to regenerator 14 by tremie pipe and regenerated, the pressure of regenerator 14
Power is higher than RCTS15, and the catalyst for leaving regenerator is promoted to RCTS, so far completes the conveying circulation of catalyst.
The present embodiment carries out cycloalkanes dehydrogenation in the hydrogen gas atmosphere using C6~C12 naphthas hydro carbons, cyclization of paraffins dehydrogenation, different
Structure and the reaction such as it is hydrocracked.Reaction feed (naphtha and hydrogen mixture) reacted charging/product exchanger 1 exchanges heat
Afterwards, the first reaction heating furnace 2, the first reforming reactor 3, the second reaction heating furnace 4, the second reforming reactor 5, are sequentially passed through
Three reaction heating furnaces 6, tri-reforming device 7, the 4th reaction heating furnace 8 and fourth reforming reactor 9, reaction product leave
After four reforming reactors 9, exchanged heat in reaction feed/product exchanger 1 with reaction feed, follow-up separator is then arrived again
Separated.The inlet pressure of first reforming reactor 3 is about that 0.56MPa (g), the inlet pressure of the second reforming reactor 5 are about
0.49MPa (g), the inlet pressure of tri-reforming device 7 are about that 0.42MPa (g), the inlet pressure of fourth reforming reactor 9 are about
0.35MPa(g)。
Used catalyst contains noble metal platinum (Pt) and tin for what Research Institute of Petro-Chemical Engineering (RIPP) developed
(Sn) and other adjuvants PS-VI continuous reforming catalysts.Leave the catalyst carbon content after regenerator 14 regenerates substantially small
In 0.2% (wt), lifted by regenerated catalyst lifting blower fan 18 with nitrogen from regenerator 14 to RCTS15.In RCTS15 first
The dust elutriation of catalyst is carried out, then the catalyst after removing dust is reduced with hot hydrogen in RCTS15, is removed
Nitrogen after dust is sent to regenerated catalyst lifting blower fan 18 and used as regenerated catalyst lifting nitrogen circulation.RCTS behaviour
Make pressure ratio the first reforming reactor high 0.01~0.08MPa of operating pressure, than the low 0.01~0.08MPa of regenerator 14.Reduction
Catalyst afterwards respectively enters reactor top hopper 10,11,12,13, Ran Houzai after leaving RCTS through 4 tremie pipes by gravity
Enter by gravity from reactor top hopper and chemically reacted in corresponding reforming reactor 3,5,7,9.In each reactor
Used is all the catalyst of the high activity just regenerated.
Reclaimable catalyst nitrogen is lifted from each reforming reactor 3,5,7,9 respectively with reclaimable catalyst lifting blower fan 17
WCTS16 tops low-pressure area is delivered to, the operating pressure of low-pressure area is less than than the low 0.01~0.08MPa of fourth reforming reactor 9
All reactors.It is independent progress from each reactor to the lifting conveying of WCTS catalyst, can changes as needed
Become the catalyst lifting conveying capacity of each reactor, the reclaimable catalyst in single or multiple reactors can also be carried out independent
Lifting conveying, can the flexible circulation conveying for carrying out catalyst in ground.Catalyst is carried out first in the low-pressure area of WCTS16 tops
Mixing, then carries out the dust elutriation of catalyst again, removes the nitrogen after dust and is sent to reclaimable catalyst lifting blower fan 18 and makees
Used for reclaimable catalyst lifting nitrogen circulation.Catalyst after removing dust carries out locking transformation again, the catalysis after boosting
Agent enters back into WCTS16 bottom higher-pressure region, the operating pressure about 0.01~0.08MPa higher than regenerator 14 of bottom higher-pressure region.It is high
The reclaimable catalyst of nip is delivered to regenerator 14 by tremie pipe and regenerated, and the operating pressure of regenerator is about 0.65MPa
(g), the catalyst after regeneration is lifted again is delivered to RCTS15, completes the circulation of catalyst.
Reaction mass is reacted in the reactor can all make carbon deposit on catalyst surface, leave on the catalyst of reactor
Coke content than entering the high of reactor, for the process of series connection conveying, carbon deposited catalyst will go successively to reactor below,
Therefore, its coke content can also be accumulated constantly, and the coke content of catalyst is higher in the backward, activity also constantly reduction, existing company
Continuous reform is exactly that its catalyst, which is circulated, causes the catalyst activity in downstream reactor less than upper using this series connection mode of movement
The reactor of trip, the activity of catalyst can not give full play to.The continuous reforming process of the present invention is defeated using catalyst parallel circulating
The mode sent so that the catalyst for entering each reactor is just to regenerate " fresh " catalyst, the average carbon deposit of reactor
Amount is low, and the effect of catalyst can more be not fully exerted.Into in each reactor reaction with just regenerated activity compared with
High catalyst contact, can reduce about 5~10 DEG C of bed mean temperature, the negative reaction such as be hydrocracked so as to reduce, with
Existing industrialized CONTINUOUS REFORMER technology, which is compared, can increase product yield about 1%, and can reduce the carbon deposit on catalyst, prolong
The life-span of long catalyst.
Table 1 is listed in the present embodiment respectively according to (conveying of catalyst parallel circulating) of the invention and according to prior art
(conveying of catalyst following current series circulation) carries out the result of the test of three groups of check experiments of hydro carbons CONTINUOUS REFORMER
Table 1
Continuous reforming process of the present invention and existing industrialized CONTINUOUS REFORMER work from the results shown in Table 1
Skill, which is compared, to be had the following advantages：
1st, the catalyst that continuous reforming process of the present invention enters each reactor was just regenerated without carbon deposit
Fresh catalyst, active highest, identical reaction severity conditions (reaction product reaches identical RON values), with it is existing
Compared through industrialized CONTINUOUS REFORMER, the inlet temperature of four reactors declines 5 DEG C.
2nd, under identical reaction severity conditions, continuous reforming process of the present invention is than existing industrialized company
Continuous reforming process average reaction temperature declines so that the average carbon deposit rate on catalyst reduces by 30~40%, C5 +Liquid yield increases
Plus 0.7~1.1%, hydrogen yield increase by 2.1~4.7%.
For a set for the treatment of capacity is 1,000,000 tons/year of catalytic reforming unit, using CONTINUOUS REFORMER work of the present invention
Skill is compared with using existing continuous reforming process, annual increasing gasoline yield 0.7~1.1 ten thousand ton, increase income about 2100~33,000,000
Member, increases production 720~1700 tons of hydrogen, about 720~17,000,000 yuan of increase income.
In above-mentioned comparative example, the operating mode of continuous reforming process of the present invention and existing industrial continuous reforming process is used
Identical air speed and identical catalyst filling ratio, i.e., the operating mode of continuous reforming process of the present invention do not optimize.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 (6)
1. a kind of hydro carbons continuous reforming process, the technique includes：At least two reforming reactors and at least one catalyst are set
Regenerator, it is characterised in that：Conveying of the reaction feed relative to each reforming reactor be series connection carry out, i.e., reaction feed according to
It is secondary to be reacted by each reforming reactor and with catalyst therein；And catalyst following between reactor and regenerator
Ring conveying is that the reacted reclaimable catalyst in progress in parallel, i.e., each reforming reactor is individually delivered to regenerator
Middle carry out cyclic regeneration, and the regenerated catalyst after regenerating is transported in each reforming reactor by parallel connection and is reused for instead
Should；
Set reclaimable catalyst to reprocess and distribution system WCTS, the reclaimable catalyst in each reforming reactor with it is parallel simultaneously
The mode of row is elevated to be delivered to the WCTS, is mixed in WCTS, dust elutriation and locking transformation process, is then conveyed
Regenerated in regenerator；And regenerated catalyst reprocessing and distribution system RCTS are set, and regenerated catalyst is by from regeneration
Device is promoted to the RCTS and carries out dust elutriation, reduction and redistribution process, is then distinguished in the way of parallel side-by-side from RCTS
Being transported in each reforming reactor is used for chemical reaction process；
Conveying capacity and/or the conveying opportunity of reclaimable catalyst from from each reforming reactor to regenerator are independently controlled, and
And independently control conveying capacity and/or the conveying opportunity of regenerated catalyst from from regenerator to each reforming reactor.
2. hydro carbons continuous reforming process according to claim 1, wherein, the technique includes, and sets four reforming reactors and one
Individual regenerator, i.e. the first reforming reactor (3), the second reforming reactor (5), tri-reforming device (7), fourth reforming reaction
Device (9) and regenerator (14), and the technique also includes setting regenerated catalyst to reprocess and distribution system RCTS (15), to be generated
Catalyst is reprocessed and distribution system WCTS (16), reclaimable catalyst lifting blower fan (17) and regenerated catalyst lifting blower fan
(18)；Reaction feed sequentially pass through the first reforming reactor (3), the second reforming reactor (5), tri-reforming device (7) and
Fourth reforming reactor (9)；Regenerated catalyst lifts blower fan (18) with regenerated catalyst and is promoted to RCTS from regenerator (14)
(15)；RCTS (15) respectively with first, second, third and fourth reforming reactor (3,5,7 with 9) be connected；With catalysis to be generated
Agent lifting blower fan (17) by first, second, third and fourth reforming reactor (3,5,7 and 9) in reclaimable catalyst carry respectively
Rise to WCTS (16)；WCTS (16) is connected by 1 tremie pipe with regenerator (14).
3. hydro carbons continuous reforming process according to claim 2, wherein, regenerated catalyst is promoted to RCTS from regenerator (14)
(15) dust elutriation, reduction and redistribution process are carried out, then passes through tremie pipe point from RCTS (15) in the way of parallel side-by-side
Not being transported in each reforming reactor is used for chemical reaction process；From RCTS (15) to the regeneration catalyzing of each reforming reactor
The conveying capacity of agent and/or conveying opportunity are individually controllable.
4. hydro carbons continuous reforming process according to claim 2, wherein, first, second, third and fourth reforming reactor (3,
5,7,9) reclaimable catalyst in is elevated in the way of parallel side-by-side to be delivered to WCTS (16), is mixed in WCTS (16)
Conjunction, dust elutriation and locking transformation process, are then delivered to regenerator (14) by tremie pipe and are regenerated；Reformed instead from each
Answer lifting conveying capacity from device to WCTS (16) reclaimable catalyst and/or conveying opportunity be individually controllable.
5. hydro carbons continuous reforming process according to claim 2, wherein, RCTS (15) operating pressure is less than regenerator (14)
Operating pressure, so as to which catalyst is lifted to RCTS (15) from regenerator；The position of RCTS (15) bottom is higher than each simultaneously
The position on reactor top, RCTS (15) operating pressure is higher than the operating pressure of the first reforming reactor (3) so that catalyst
All reforming reactors can be flowed into from RCTS (15).
6. hydro carbons continuous reforming process according to claim 2, wherein, the position of WCTS (16) bottom is higher than on regenerator (14)
The position in portion, WCTS (16) is divided into two pressure areas, and the upper zone before transformation is low-pressure area, and pressure is anti-less than fourth reforming
Device (9) is answered, reclaimable catalyst can be lifted to the low-pressure area from fourth reforming reactor (9)；Lower region after transformation
For higher-pressure region, pressure is higher than regenerator (14), and reclaimable catalyst can be flowed into regenerator (14) from the higher-pressure region.
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| CN107267192A (en) * | 2017-08-17 | 2017-10-20 | 山东京博石油化工有限公司 | A kind of method for reducing the loss of catalyst lifting process |
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| 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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| 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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