CN106905995A

CN106905995A - A kind of hydro carbons continuous reforming process

Info

Publication number: CN106905995A
Application number: CN201510974463.2A
Authority: CN
Inventors: 袁忠勋
Original assignee: Sinopec Engineering Inc; Sinopec Engineering Group Co Ltd
Current assignee: Sinopec Engineering Inc; Sinopec Engineering Group Co Ltd
Priority date: 2015-12-22
Filing date: 2015-12-22
Publication date: 2017-06-30

Abstract

The invention discloses a kind of hydro carbons continuous reforming process, the technique includes：At least three reforming reactors and at least one catalyst regenerator are set, wherein, last reforming reactor is referred to as second group of reactor, reactor in addition to last reforming reactor is referred to as first group of reactor, reaction feed is carried out relative to the conveying series connection of each reforming reactor, and catalyst is that parallel connection is carried out with the circulation conveying between regenerator in first group of reactor and second group of reactor, and catalyst is carried out in first group of reactor with the conveying series connection following current between regenerator.In the present invention, every group of reactor can be carried out separately adjustable using fresh high activated catalyst and on demand 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

A kind of hydro carbons continuous reforming process

Technical field

The present invention relates to hydrocarbon reformation field, and in particular to a kind of hydro carbons continuous reforming process.

Background technology

CONTINUOUS REFORMER is a kind of oil secondary operation technology, and the raw material of processing is mainly the straight run of low octane rating Naphtha, hydrotreated naphtha etc., using platinum Pt- tin Sn bimetallic catalysts, at 500 DEG C or so Under high temperature, make molecule that rearrangement, isomery to occur, increase the yield of aromatic hydrocarbons, improve the technology of octane number.

Moving-burden bed reactor continuous regenerative reforming, abbreviation CONTINUOUS REFORMER.Industry should in the world at present Main three CONTINUOUS REFORMER patented technologies provider is respectively Uop Inc. of the U.S., France Axens With Chinese SEI.In continuous reformer, catalyst continuously flows successively through three (or four) of series connection Moving-burden bed reactor, is generally from the reclaimable catalyst carbon content of last reactor outflow 2%-8% (mass fraction), reclaimable catalyst is transported to regenerator and is regenerated by gravity or gas lift. Regenerated catalyst after activity recovery returns to first reactor and is reacted again, and catalyst is formed in system One closed cycle.

By catalyst transport model split, existing industrialized continuous reforming process can be divided into " suitable Stream " and " adverse current " two ways.

In the catalyst circulation conveying technique of " following current " CONTINUOUS REFORMER, reaction mass from first reactor according to It is secondary to flow to most end reactor, reacted on the catalyst in each reactor.Catalyst is in each reactor Between moving direction be consistent with reaction mass, that is, the high activated catalyst for regenerating is by reaction stream Order is introduced into first reactor, then passes sequentially through second reactor, the 3rd reactor until most end is anti- Device is answered, is gradually reduced to most end reactor pressure from first reactor, from the catalysis out of most end reactor Agent activity is relatively low, is sent in regenerator and is regenerated, and the catalyst after regeneration is lifted to the first reaction again Device completes the circulation of catalyst.In the technical process of this CONTINUOUS REFORMER, catalyst is in the reactor string What connection was used, the catalyst into the first reforming reactor is just to have regenerated urging for " fresh " high activity Agent, and reactor below is all the above reactor relatively low catalysis of used activity Agent.

In the catalyst circulation conveying technique of " adverse current " CONTINUOUS REFORMER, reaction mass from first reactor according to It is secondary to flow to most end reactor.And moving direction of the catalyst between each reactor is opposite with reaction mass , that is, the order of the high activated catalyst back reaction logistics for regenerating is introduced into rearmost reactor, so The direction of back reaction logistics is successively forward until first reactor afterwards, then is sent to regeneration from first reactor Regenerated in device, the catalyst after regeneration lifts last reactor and completes following for catalyst again Ring.The technical process of this adverse current CONTINUOUS REFORMER causes the difficult reaction for carrying out in high activated catalyst below Reactor in carry out, reaction easy to perform is carried out in the reactor of low activity catalyst above.

But, either " following current " or " adverse current " continuous reforming process, catalyst reactor it Between circulation conveying all using series connection by the way of, this mode of movement is only transported to first from regenerator The catalyst of reactor is only " fresh " activity for just regenerating catalyst high, such as " following current " even Continuous the first reforming reactor reformed, last reforming reactor of " adverse current " CONTINUOUS REFORMER.And its Catalyst in his reforming reactor is all that above reactor is used to have dropped containing carbon distribution activity Low catalyst, catalyst is conveyed in the backward, and its activity is lower, the work in the reactor that catalyst leaves Property is minimum.The activity of catalyst can not give full play in all reactors as can be seen here.This catalyst The mode of series connection conveying, the catalyst internal circulating load by each reactor is all identical, in all reactors Catalyst must circular regeneration simultaneously, the catalyst flow of each reactor can not on demand carry out independence Regulation and change, it is impossible to be individually circulated regeneration.

The content of the invention

It is an object of the invention to provide a kind of hydro carbons continuous reforming process, prior art is overcome to realize instead Device is answered to be urged with can not on demand carry out separately adjustable and change using fresh high activated catalyst as needed The disadvantage of agent flow, to give full play to the activity of catalyst, improves the utilization rate of catalyst, improves weight Turn over rate and yield.

To achieve these goals, the present invention provides a kind of hydro carbons continuous reforming process, and the technique includes： At least three reforming reactors and at least one catalyst regenerator being parallel to each other are set；Wherein：Reaction Feed is carried out relative to the conveying series connection of each reforming reactor, i.e., reaction feed passes sequentially through each Reforming reactor is simultaneously reacted with catalyst therein；Wherein, flowed to according to reaction feed, will be described At least three reforming reactors are divided into first group of reactor and second group of reactor, and first group of reactor includes All reforming reactors in addition to last reforming reactor, second group of reactor for it is described last Individual reforming reactor；Catalyst is in first group of reactor and second group of reactor with the circulation between regenerator Conveying is that parallel connection is carried out, i.e., the reacted reclaimable catalyst in every group reactor is all individually delivered to Cyclic regeneration is carried out in regenerator, and the regenerated catalyst after regenerating is transported in every group of reactor by parallel connection It is reused for reaction；Catalyst is that series connection following current is carried out with the conveying between regenerator in first group of reactor , i.e., flowed to according to reaction feed, by the reclaimable catalyst in the end reactor in first group of reactor Being delivered in regenerator carries out cyclic regeneration, and the regenerated catalyst after regenerating is transported to first group of reaction Reacted in initial reactor in device, and catalyst is delivered to by the initial reactor successively following current Reacted in the end reactor and successively.

Preferably, the technique also includes：Independently control the catalysis to be generated from every group of reactor to regenerator The conveying capacity of agent and/or conveying opportunity, and independently control to be urged from regenerator to the regeneration of every group of reactor The conveying capacity of agent and/or conveying opportunity.

Preferably, the technique also includes：Reclaimable catalyst reprocessing and distribution system WCTS are set, often Group reactor in reclaimable catalyst it is elevated in the way of parallel side-by-side be delivered to the WCTS, Mixed in WCTS, dust elutriation and locking transformation process, be then transferred to be carried out in regenerator Regeneration；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, then with the side of parallel side-by-side Formula is respectively delivered to be used for chemical reaction process in each group reactor from RCTS.

Preferably, the technique includes setting four reforming reactors being parallel to each other and a regenerator, i.e., First reforming reactor, the second reforming reactor, tri-reforming device, fourth reforming reactor and again Raw device, and the technique also includes setting regenerated catalyst reprocessing and distribution system RCTS, to be generated urges Agent is reprocessed and distribution system WCTS, reclaimable catalyst lifting blower fan and regenerated catalyst lifting wind Machine；First, second, and third reforming reactor is first group of reactor, the fourth reforming reaction Device is second group of reactor；Reaction feed sequentially pass through the first reforming reactor, the second reforming reactor, Tri-reforming device and fourth reforming reactor；Regenerated catalyst regenerated catalyst lifts blower fan from again Raw device is promoted to RCTS；RCTS is connected with first and fourth reforming reactor respectively；Urged with to be generated Reclaimable catalyst in third and fourth reforming reactor is promoted to WCTS by agent lifting blower fan respectively； WCTS is connected by 1 tremie pipe with regenerator；Catalyst is in first group of reactor by One reforming reactor flows to the second reforming reactor and tri-reforming device successively.

Preferably, regenerated catalyst by from regenerator be promoted to RCTS carry out dust elutriation, reduction and again Assigning process, is then respectively delivered to each group and reacts from RCTS in the way of parallel side-by-side by tremie pipe It is used for chemical reaction process in device；From RCTS to every group of conveying capacity of the regenerated catalyst of reactor and/ Or conveying opportunity is individually controllable.

Preferably, the reclaimable catalyst in the third and fourth reforming reactor is carried in the way of parallel side-by-side Rise and be delivered to WCTS, mixed in WCTS, dust elutriation and locking transformation process, then Regenerator is delivered to by tremie pipe to be regenerated；From every group of reactor to the reclaimable catalyst of WCTS Lifting conveying capacity and/or conveying opportunity are individually controllable.

Preferably, the operating pressure of RCTS less than regenerator operating pressure, such that it is able to by catalyst From regenerator lifting to RCTS；The position of RCTS bottoms is higher than the position on each group reactor top simultaneously, The operating pressure of RCTS is higher than the first reforming reactor and the operating pressure of fourth reforming reactor so that Catalyst can be flowed into every group of reactor from RCTS.

Preferably, the position of WCTS bottoms is higher than the position on regenerator top, and it is two pressures that WCTS is divided to Power area, the upper zone before transformation is low-pressure area, and pressure is less than tri-reforming device and fourth reforming Reactor, can be low to this from tri-reforming device and the lifting of fourth reforming reactor by reclaimable catalyst Nip；Lower region after transformation is higher-pressure region, and pressure is higher than regenerator, and reclaimable catalyst can be from The higher-pressure region is flowed into regenerator.

The circulation conveying mode that continuous reforming process of the invention is combined using catalyst parallel connection and serial connection, So that being just to regenerate " newly into the catalyst being most difficult to wherein in the 4th reactor of reaction It is fresh " catalyst, and the reaction carried out in the first and second reforming reactors above is relatively easy, leaves The catalyzer coke content of the first reforming reactor seldom, can continue on for the second reforming reactor, anti-to its Shadow very little is answered, the catalyzer coke content for leaving the second reforming reactor is relatively low, can be continued on for triple Whole reactor, reacts it smaller, catalyst of such first, second, and third reforming reactor of influence Just conveying can be lifted from reactor to regenerator to reduce catalyst by the way of series connection following current conveying Number of times, simple flow.The circulation conveying being combined using this catalyst parallel connection and serial connection of the invention Mode, flow is relatively easy, and the average coke content of reactor is low, and the effect of catalyst more can fully be sent out Wave.

The present invention is overcome by changing circulation conveying mode of the catalyst between multiple reforming reactors The shortcoming that each catalyst reactor activity can not give full play in existing industrialized technology.Into Reactant in every group of reactor is all contacted with the active catalyst higher for just regenerating, and can reduce bed About 4~10 DEG C of mean temperature of layer, the side reaction such as is hydrocracked such that it is able to reduce, and has been industrialized with existing CONTINUOUS REFORMER technology compared to product yield about 1% can be increased, and the carbon deposit on catalyst can be reduced, prolong The life-span of catalyst long.

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 to constitute the part of specification, with Following specific embodiment is used to explain the present invention together, but is not construed as limiting the invention. In accompanying drawing：

Fig. 1 is a kind of schematic flow sheet of specific embodiment of hydro carbons continuous reforming process of the present invention.

Description of reference numerals

The reaction heating furnace of 1 reaction feed/product exchanger 2 first

The reaction heating furnace of 3 first reforming reactors (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 regenerated catalysts lifting blower fan 18 reclaimable catalyst lifting blower fan

Specific embodiment

Specific embodiment of the invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that Specific embodiment described herein is merely to illustrate and explain the present invention, and is not intended to limit the present invention.

The present invention provides a kind of hydro carbons continuous reforming process, and the technique includes：Set at least three mutually flat Capable reforming reactor and at least one catalyst regenerator；Wherein：Reaction feed is reformed relative to each Reactor conveying series connection carry out, i.e., reaction feed pass sequentially through each reforming reactor and with wherein Catalyst reacted；Wherein, flowed to according to reaction feed, by least three reforming reactor It is divided into first group of reactor and second group of reactor, first group of reactor includes removing last reforming reaction All reforming reactors beyond device, second group of reactor is described last reforming reactor；Catalysis Agent is that parallel connection is carried out with the circulation conveying between regenerator in first group of reactor and second group of reactor, Reacted reclaimable catalyst in i.e. every group reactor is carried out continuously in being all individually delivered to regenerator Regeneration, and the regenerated catalyst after regenerating is transported in every group of reactor by parallel connection and is reused for reaction；Urge Agent first group of reactor between regenerator conveying series connection following current carry out, i.e., according to react into Stream is to the reclaimable catalyst in the end reactor in first group of reactor to be delivered in regenerator Row cyclic regeneration, and the regenerated catalyst after regenerating is transported to the initial reactor in first group of reactor In reacted, and catalyst is delivered in the end reactor by the initial reactor successively following current And reacted successively.

Hydro carbons continuous reforming process of the invention, the various process conditions employed in it, including original Material oil, catalyst, the operating condition of reactor, the operating condition of regenerator for being used etc. are all abilities Known to the those of ordinary skill of domain, there is no particular limitation to it for the present invention.

For example, described catalyst can contain primary activity component noble metal platinum (Pt) etc., co-catalysis Aluminum oxide of agent component tin (Sn) and rhenium (Re) etc. and acid carrier etc. and other adjuvants, but not It is limited to this.The operating condition of each reactor can be independently, but be not limited to：Reaction pressure 0.1~1.5MPa, preferably 0.2~1.0MPa；400~550 DEG C of reaction temperature (feedstock inlet temperature), it is excellent Select 480-520 DEG C；Hydrogen-oil ratio (mol ratio) 0.1~10.0, preferably 1.0~5.0；Weight space velocity is 0.5~5, Preferably 1.5~3.Described feedstock oil may be, but not limited to,：The straight-run naphtha of low octane rating, Hydrotreated naphtha etc..

Hydro carbons continuous reforming process of the invention, described reforming reactor is the affiliated technology in this area Moving-burden bed reactor known to personnel；Moving-burden bed reactor can be 3~6 series connection, preferably 3~4 Platform is connected；Described regenerator is used to make to realize cyclic regeneration by the reclaimable catalyst of reaction inactivation, wraps Include by burning, oxychlorination, drying (or roasting) technique make carbon content reclaimable catalyst high recover to live Property, the quantity of regenerator is preferably one, it is also possible to set again one it is standby.

A kind of specific embodiment of the invention, the hydro carbons continuous reforming process includes setting four The individual reforming reactor being parallel to each other and a regenerator, i.e. the first reforming reactor 3, second are reformed anti- Device 5, tri-reforming device 7, fourth reforming reactor 9 and regenerator 14 are answered, and the technique is also Including setting regenerated catalyst reprocessing and distribution system RCTS15, reclaimable catalyst reprocessing and distributing System WCTS16, reclaimable catalyst lifting blower fan 18 and regenerated catalyst lifting blower fan 17；It is described First, second, and third reforming reactor is first group of reactor, and the fourth reforming reactor is second Group reactor；Reaction feed sequentially passes through the first reforming reactor 3, the second reforming reactor the 5, the 3rd Reforming reactor 7 and fourth reforming reactor 9；Regenerated catalyst lifts blower fan 17 with regenerated catalyst RCTS15 is promoted to from regenerator 14；RCTS15 respectively with first and fourth reforming reactor 3 and 9 It is connected；Blower fan 18 is lifted by treating in the third and fourth reforming reactor 7 and 9 with reclaimable catalyst Raw catalyst is promoted to WCTS16 respectively；WCTS16 is connected by 1 tremie pipe with regenerator 14 Connect；It is anti-that catalyst flows to the second reformation successively in first group of reactor by the first reforming reactor 3 Answer device 5 and tri-reforming device 7.

Hydro carbons continuous reforming process of the invention, the regenerated catalyst reprocessing and distribution system RCTS 15 can carry out dust elutriation, reduction and reallocate to regenerated catalyst, then with parallel side-by-side Mode be sent to respectively in each group reactor for chemical reaction process by tremie pipe.

Hydro carbons continuous reforming process of the invention, the reclaimable catalyst reprocessing and distribution system WCTS 16 can be mixed to reclaimable catalyst, dust elutriation and locking transformation, then by blanking Pipe is delivered to regenerator and is regenerated.

Hydro carbons continuous reforming process of the invention, those skilled in the art are it is appreciated that reaction Charging can first be exchanged heat with product, then successively and alternately enter heating furnace and reaction below Device, product to be left and arrive follow-up separator again after heat exchanger and separated.

Hydro carbons continuous reforming process of the invention, catalyst after regeneration from regenerator lifted to , be respectively delivered to for catalyst by tremie pipe then to be chemically reacted in each group reactor by RCTS15. The reclaimable catalyst for leaving each group reactor is lifted be delivered to WCTS16 respectively, then defeated by tremie pipe Regenerator is delivered to be regenerated.

The present invention will be further illustrated by embodiment below, but therefore the present invention is not taken office What is limited.

Embodiment

A kind of specific embodiment that 1 couple of present invention of the present embodiment combination accompanying drawing is provided is illustrated.Due to What is carried out is prolonged commerical test, wherein described various process conditions allowed about ± 10% fluctuation.

As shown in figure 1, after reaction feed exchanges heat in reaction feed/product exchanger 1 with product Sequentially pass through the first reaction heating furnace 2, the first reforming reactor 3, the second reaction heating furnace 4, the second weight Whole reactor 5, the 3rd reaction heating furnace 6, tri-reforming device 7, the 4th reaction heating furnace 8 and Four reforming reactors 9, product leave reactor 9 in reaction feed/product exchanger 1 with reaction Then charging heat exchange is arrived follow-up separator and is separated again, wherein, first, second, and third reforms Reactor is referred to as first group of reactor, and fourth reforming reactor is referred to as second group of reactor.Reaction mass exists Pressure drop is produced in flow process, reactor operating pressure order from high to low is：First reforming reaction Device 3, the second reforming reactor 5, tri-reforming device 7 and fourth reforming reactor 9.In regenerator 14 regeneration after catalyst by regenerated catalyst lifting blower fan 17 with nitrogen from regenerator 14 lifted to RCTS15.Carry out the dust elutriation of catalyst first in RCTS15, then reusable heat hydrogen is to removing Catalyst after dust is reduced, and is removed the nitrogen after dust and is sent to regenerated catalyst lifting blower fan 17 use as regenerated catalyst lifting nitrogen circulation.The pressure of RCTS15 is higher than first group and second group The anti-top hopper 10 of reactor, i.e., one, the first reforming reactor 3, four anti-top hoppers 13 and the 4th Reforming reactor 9, the catalyst after reduction respectively enters each group reactor by gravity by 2 tremie pipes Top hopper 10,13, then by gravity enter corresponding reactor 3, chemically reacted in 9.From React that the catalyst for finishing sequentially enters reactor 5 and reactor 7 is reacted in reactor 3.

In each group reactor it is used be all the high activity for just regenerating catalyst.Can be in the blanking Catalyst flow control device is set on pipe or top hopper, to realize to entering in each group reactor again The flow of raw catalyst is controlled or even dams.Lifting the nitrogen of blower fan 18 with reclaimable catalyst will treat Raw catalyst is tri-reforming device 7 from each group reactor respectively and fourth reforming reactor 9 lifted it is defeated Deliver to the top low-pressure area of WCTS16, the operating pressure of WCTS16 tops low-pressure area is triple less than the Whole reactor 7 and fourth reforming reactor 9, are lifted to the catalyst of WCTS from every group of reactor and conveyed All it is independent, and it is controllable to lift conveying capacity, can as needed change carrying for reclaimable catalyst Rise conveying capacity.In the top low-pressure area of WCTS16, catalyst is mixed first, then entered again The dust elutriation of row catalyst, the nitrogen after removing dust is sent to reclaimable catalyst lifting blower fan 18 and makees For reclaimable catalyst lifting nitrogen circulation is used, remove the catalyst after dust carries out locking transformation again, Catalyst after boosting enters back into the bottom higher-pressure region of WCTS16, and the operating pressure of higher-pressure region is higher than regeneration Device 14, the catalyst after boosting is delivered to regenerator 14 and is regenerated by tremie pipe, regenerator 14 Pressure be higher than RCTS15, the catalyst for leaving regenerator is promoted to RCTS, so far completes catalyst Conveying circulation.

The present embodiment uses C₆~C₁₂Naphtha hydro carbons carries out cycloalkanes dehydrogenation, alkane ring in the hydrogen gas atmosphere Fluidized dehydrogenation, isomerization and the reaction such as it is hydrocracked.Reaction feed (naphtha and hydrogen mixture) is through anti- Should feed/product exchanger 1 exchange heat after, sequentially pass through the first reaction heating furnace 2, the first reforming reactor 3rd, the second reaction heating furnace 4, the second reforming reactor 5, the 3rd reaction heating furnace 6, tri-reforming are anti- Device 7, the 4th reaction heating furnace 8 and fourth reforming reactor 9 are answered, it is anti-that product leaves fourth reforming After answering device 9, exchanged heat with reaction feed in reaction feed/product exchanger 1, follow-up dividing then is arrived again Separated from device.The inlet pressure of first reforming reactor 3 is about 0.56MPa (g), the second reformation instead The inlet pressure of device 5 about 0.49MPa (g), the inlet pressure of tri-reforming device 7 is answered to be about 0.42MPa (g), the inlet pressure of fourth reforming reactor 9 are about 0.35MPa (g).

The catalyst for being used contains noble metal platinum for Research Institute of Petro-Chemical Engineering (RIPP) exploitation (Pt) and tin (Sn) and other adjuvants PS-VI continuous reforming catalysts.Leave regenerator 14 Catalyst carbon content after regeneration is approximately less than 0.2% (wt), and nitrogen is used by regenerated catalyst lifting blower fan 17 Gas is lifted to RCTS15 from regenerator 14.Carry out the dust elutriation of catalyst first in RCTS15, Then the catalyst after removing dust is reduced with hot hydrogen in RCTS15, after removing dust Nitrogen be sent to regenerated catalyst lifting blower fan 17 as regenerated catalyst lifting nitrogen circulation use. The operating pressure of RCTS compares regenerator than first reforming reactor operating pressure 0.01~0.08MPa high 14 low 0.01~0.08MPa.Catalyst after reduction divides after leaving RCTS through 2 tremie pipes by gravity Not Jin Ru reactor top hopper 10,13, then enter corresponding from reactor top hopper by gravity again Reforming reactor 3, is chemically reacted in 9, reacted in reforming reactor 3 catalyst for finishing again according to It is secondary to be delivered to reforming reactor 5,7.Used in each group reactor is all urging for the high activity that just regenerated Agent.

Blower fan 18 is lifted with reclaimable catalyst by reclaimable catalyst nitrogen respectively from each group reactor The lifting of reforming reactor 7,9 is delivered to WCTS16 tops low-pressure area, and the operating pressure of low-pressure area compares the Low 0.01~the 0.08MPa of four reforming reactor 9, less than all of reactor.From every group of reactor to The catalyst lifting conveying of WCTS is all independently carried out, and can as needed change each group reactor Catalyst lifts conveying capacity, it is also possible to which the reclaimable catalyst in single group or multigroup reactor is individually carried Conveying is risen, the circulation conveying of catalyst can be neatly carried out.In the low-pressure area of WCTS16 tops first The mixing of catalyst is carried out, the dust elutriation of catalyst is then carried out again, removed the nitrogen after dust and send Used as reclaimable catalyst lifting nitrogen circulation to reclaimable catalyst lifting blower fan 18.Remove dust it Catalyst afterwards carries out locking transformation again, and the catalyst after boosting enters back into the bottom high pressure of WCTS16 Area, the operating pressure about 0.01~0.08MPa higher than regenerator 14 of bottom higher-pressure region.Higher-pressure region is treated Raw catalyst is delivered to regenerator 14 and is regenerated by tremie pipe, and the operating pressure of regenerator is about 0.65 MPa (g), the catalyst after regeneration is lifted be delivered to RCTS15 again, completes the circulation of catalyst.

Reaction mass is reacted in the reactor can all make carbon deposit on catalyst surface, leave reactor , than entering the high of reactor, for the process of series connection conveying, carbon deposited catalyst will for coke content on catalyst Go successively to reactor below, therefore, its coke content can also be accumulated constantly, in the backward catalyst Coke content is higher, and activity is also constantly reduced, and existing CONTINUOUS REFORMER is exactly to use this series connection mode of movement, Its catalyst is circulated and causes the catalyst activity in downstream reactor less than the reactor of upstream, at last What is carried out in individual reactor is the chemical reaction being most difficult to, and uses above reactor used The minimum catalyst of activity so that the activity of catalyst can not give full play to.CONTINUOUS REFORMER work of the invention Skill is by the way of the circulation conveying that catalyst connection in series-parallel is combined so that enter every group of catalysis of reactor Agent is all " fresh " catalyst for just regenerating, and the average coke content of reactor is low, and the effect of catalyst is more Can be not fully exerted.It is all higher with the activity for just regenerating into the reactant in most latter two reactor Catalyst contact, about 4~10 DEG C of bed mean temperature can be reduced, be hydrocracked such that it is able to reduce Side reaction, product yield about 1% can be increased compared with existing industrialized CONTINUOUS REFORMER technology, and The carbon deposit on catalyst can be reduced, extends the life-span of catalyst.Into every group of catalyst circulation of reactor Amount can be adjusted as needed, so as to optimize reaction and regeneration condition, improve catalyst and use effect Rate.

Table 1 listed in the present embodiment and according to (catalyst connection in series-parallel circulation conveying) of the invention and press respectively Three groups of check experiments of hydro carbons CONTINUOUS REFORMER are carried out according to prior art (conveying of catalyst following current series circulation) Result of the test.

Continuous reforming process of the present invention and existing industrialized company from the results shown in Table 1 Continuous reforming process is compared and had the following advantages：

1st, continuous reforming process of the present invention is all into the catalyst of first, fourth reforming reactor The fresh catalyst without carbon deposit for just regenerating, active highest reacts severity conditions (anti-in identical Product is answered to reach identical RON values), compared with existing industrialized CONTINUOUS REFORMER, each reaction The inlet temperature of device declines 3~5 DEG C.

2nd, identical reaction severity conditions under, continuous reforming process of the present invention than it is existing Industrialized continuous reforming process average reaction temperature declines so that the average carbon deposit rate reduction on catalyst 30~40%, C₅ ⁺Liquid yield increases by 0.7~1.1%, and hydrogen yield increases by 2.1~4.7%.

For the catalytic reforming unit that a set for the treatment of capacity is 1,000,000 tons/year, using of the present invention Continuous reforming process with using compared with existing continuous reforming process, annual increasing gasoline yield 0.7~1.1 ten thousand ton, Increase about 2100~33,000,000 yuan of income, increase production 720~1700 tons of hydrogen, increase income about 720~1700 Wan Yuan.

In above-mentioned comparative example, continuous reforming process of the present invention and existing industrial continuous reforming process Operating mode uses identical air speed and identical catalyst filling ratio, i.e., continuous reforming process of the present invention Operating mode does not optimize.If optimizing reaction condition (such as catalyst of continuous reforming process of the present invention Filling ratio etc.), then can reduce catalyst filling amount or further improve liquid yield, increase the benefit.

Table 1

Claims

1. a kind of hydro carbons continuous reforming process, the technique includes：At least three weights being parallel to each other are set Whole reactor and at least one catalyst regenerator；It is characterized in that：

Reaction feed is carried out relative to the conveying series connection of each reforming reactor, i.e., reaction feed is successively Reacted by each reforming reactor and with catalyst therein；Wherein, flowed to according to reaction feed, At least three reforming reactor is divided into first group of reactor and second group of reactor, first group of reaction Device includes all reforming reactors in addition to last reforming reactor, and second group of reactor is described Last reforming reactor；

Catalyst is simultaneously with the circulation conveying between regenerator in first group of reactor and second group of reactor What connection was carried out, i.e., the reacted reclaimable catalyst in every group reactor is all individually delivered in regenerator Cyclic regeneration is carried out, and the regenerated catalyst after regenerating is transported in every group of reactor by parallel connection and is reused for Reaction；

Catalyst first group of reactor between regenerator conveying series connection following current carry out, i.e., according to Reaction feed is flowed to, and the reclaimable catalyst in the end reactor in first group of reactor is delivered into regeneration Cyclic regeneration is carried out in device, and the regenerated catalyst after regenerating is transported to the starting in first group of reactor Reacted in reactor, and catalyst to be delivered to the end by the initial reactor successively following current anti- Answer in device and reacted successively.

2. hydro carbons continuous reforming process according to claim 1, the technique also includes：Independently control From every group of reactor to the conveying capacity of the reclaimable catalyst of regenerator and/or conveying opportunity, and independently control Make the conveying capacity from regenerator to every group of regenerated catalyst of reactor and/or conveying opportunity.

3., according to the hydro carbons continuous reforming process of claim 1 or 2, the technique also includes：Setting is treated Raw catalyst reprocessing and distribution system WCTS, the reclaimable catalyst in every group of reactor is with parallel side-by-side Mode it is elevated be delivered to the WCTS, mixed in WCTS, dust elutriation and locking become Journey is pressed through, is then transferred to be regenerated in regenerator；And regenerated catalyst reprocessing is set and is divided Match system RCTS, regenerated catalyst is promoted to the RCTS from regenerator carries out dust elutriation, reduction And redistribution process, then it is respectively delivered in each group reactor from RCTS in the way of parallel side-by-side For chemical reaction process.

4. hydro carbons continuous reforming process according to claim 1, the technique includes setting four mutually flat Capable reforming reactor and a regenerator, i.e. the first reforming reactor (3), the second reforming reactor (5), Tri-reforming device (7), fourth reforming reactor (9) and regenerator (14), and the technique is also Including setting regenerated catalyst reprocessing and distribution system RCTS (15), reclaimable catalyst reprocessing and dividing Match system WCTS (16), reclaimable catalyst lift blower fan (18) and regenerated catalyst lifting blower fan (17)；First, second, and third reforming reactor is first group of reactor, the fourth reforming Reactor is second group of reactor；Reaction feed sequentially passes through the first reforming reactor (3), the second reformation Reactor (5), tri-reforming device (7) and fourth reforming reactor (9)；Regenerated catalyst is used Regenerated catalyst lifts blower fan (17) and is promoted to RCTS (15) from regenerator (14)；RCTS(15) It is connected with first and fourth reforming reactor (3 and 9) respectively；Blower fan (18) is lifted with reclaimable catalyst Reclaimable catalyst in third and fourth reforming reactor (7 and 9) is promoted to WCTS (16) respectively； WCTS (16) is connected by 1 tremie pipe with regenerator (14)；Catalyst is at described first group The second reforming reactor (5) and tri-reforming are flowed to by the first reforming reactor (3) successively in reactor Reactor (7).

5. hydro carbons continuous reforming process according to claim 4, wherein, regenerated catalyst is by from regeneration Device (14) is promoted to RCTS (15) and carries out dust elutriation, reduction and redistribution process, then with flat Row mode arranged side by side from RCTS (15) each group reactor is respectively delivered to by tremie pipe in for chemistry Course of reaction；During from RCTS (15) to the conveying capacity of every group of regenerated catalyst of reactor and/or conveying Machine is individually controllable.

6. hydro carbons continuous reforming process according to claim 4, wherein, the third and fourth reforming reaction Reclaimable catalyst in device (7 and 9) is elevated in the way of parallel side-by-side to be delivered to WCTS (16), Mixed in the WCTS (16), dust elutriation and locking transformation process, it is then defeated by tremie pipe Regenerator (14) is delivered to be regenerated；From every group of reactor to the reclaimable catalyst of WCTS (16) Lifting conveying capacity and/or conveying opportunity are individually controllable.

7. hydro carbons continuous reforming process according to claim 4, wherein, the operation pressure of RCTS (15) Power is less than the operating pressure of regenerator (14), such that it is able to catalyst is lifted to RCTS from regenerator (15)；The position of RCTS (15) bottom is higher than the position on each group reactor top, RCTS (15) simultaneously Operating pressure of the operating pressure higher than the first reforming reactor (3) and fourth reforming reactor (9), Allow that catalyst is flowed into every group of reactor from RCTS (15).

8. hydro carbons continuous reforming process according to claim 4, wherein, WCTS (16) bottom Higher than the position on regenerator (14) top, WCTS (16) is divided into two pressure areas, in transformation for position Upper zone before is low-pressure area, and pressure is less than tri-reforming device (7) and fourth reforming reactor (9), reclaimable catalyst can be carried from tri-reforming device (7) and fourth reforming reactor (9) It is raised to the low-pressure area；Lower region after transformation is higher-pressure region, and pressure is higher than regenerator (14), is treated Raw catalyst can be flowed into regenerator (14) from the higher-pressure region.