CN204111693U - Hydro carbons continuous reformer (five) - Google Patents
Hydro carbons continuous reformer (five) Download PDFInfo
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- CN204111693U CN204111693U CN201420475368.9U CN201420475368U CN204111693U CN 204111693 U CN204111693 U CN 204111693U CN 201420475368 U CN201420475368 U CN 201420475368U CN 204111693 U CN204111693 U CN 204111693U
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Abstract
The utility model discloses a kind of hydro carbons continuous reformer, this device comprises four reforming reactors and a catalyst regenerator, it is characterized in that: connected by reaction mass Tandem between each reforming reactor; Second and the 4th the catalyst outlet of reforming reactor (5,9) be connected in parallel respectively by the catalyst inlet of catalyst transport passage and revivifier (14); And first and the catalyst inlet of tri-reforming device (3,7) be connected in parallel respectively by the catalyst outlet of catalyst transport passage and revivifier (14).In the utility model, first and tri-reforming device can use fresh high activated catalyst and carry out on demand independence regulate and change catalyst flow, the activity of catalyzer can be given full play to, improve the utilization ratio of catalyzer, improve reforming conversion and product yield.
Description
Technical field
The utility model relates to a kind of hydro carbons continuous reformer.
Background technology
CONTINUOUS REFORMER is a kind of oil secondary processing technology, the raw material of processing is mainly low-octane virgin naphtha, hydrotreated naphtha etc., utilize platinum Pt-tin Sn bimetallic catalyst, under the high temperature of about 500 DEG C, molecule is reset, isomery, increases the output of aromatic hydrocarbons, improves the technology of gasoline octane rating.
Moving-burden bed reactor continuous regenerative reforming, is called for short CONTINUOUS REFORMER.Main three CONTINUOUS REFORMER patented technology providers of industrial application are American UOP company, French Axens and Chinese SEI respectively in the world at present.In continuous reformer, catalyzer flows through three (or four) moving-burden bed reactors of series connection continuously successively, the reclaimable catalyst carbon content flowed out from last reactor is generally 2%-8% (massfraction), and reclaimable catalyst is transported to revivifier by gravity or gas lift and regenerates.Regenerated catalyst after activity recovery returns the first reactor and reacts again, and catalyzer forms a closed cycle in system.
By reaction feed and catalyst transport model split, existing industrialized continuous reforming process can be divided into " following current " and " adverse current " two profiles formula.
The reaction mass of " following current " continuous reforming process flows to most end reactor successively from the first reactor, and the catalyzer in each reactor reacts.The travel direction of catalyzer between each reactor is consistent with reaction mass, namely regenerated high activated catalyst is introduced into the first reforming reactor by the order of reactant flow, then the second reforming reactor, tri-reforming device is passed through successively until most end reforming reactor, decline gradually from the first reactor to most end reactor pressure, lower from most end reactor catalyst activity out, be sent in revivifier and regenerate, the catalyzer after regeneration rises to the circulation that the first reactor completes catalyzer again.The technological process catalyzer of this CONTINUOUS REFORMER is that series connection uses in the reactor, the catalyzer entering the first reforming reactor is just regenerated " fresh " highly active catalyzer, and reactor below is all the catalyzer that the activity used of reactor is relatively low above.This process is schematically as follows:
This catalyst recirculation mode of movement makes reaction the having in the reactor of high activated catalyst above of easily carrying out carry out, and the reaction that difficulty is carried out having in the reactor of low activity catalyst is below carried out, the reaction complexity that the active condition of catalyst reactor is carried out with it does not match.The circulation arrangement of this catalyzer is irrational.As shown in Figure 1.
The reaction mass of " adverse current " continuous reforming process flows to most end reactor successively from the first reactor, and the travel direction of catalyzer between each reactor is contrary with reaction mass, the order of namely regenerated high activated catalyst reversed reaction logistics is introduced into rearmost reactor, then the direction of reversed reaction logistics is successively forward until first reactor, deliver to revivifier from the first reactor and regenerate, the catalyzer after regeneration rises to the circulation that last reactor completes catalyzer again.This process is schematically as follows:
Carry out in the reactor of the high activated catalyst of reaction below that the technological process of this adverse current CONTINUOUS REFORMER makes difficulty carry out, carry out in the reactor of the low activity catalyst of the reaction easily carried out above.It is comparatively reasonable that following current conveying is compared in the circulation arrangement of this catalyzer, and the reaction complexity that active condition and its of catalyst reactor carry out compares and matches.As shown in Figure 2.
But no matter be " following current " or " adverse current " CONTINUOUS REFORMER, the circulation conveying of catalyzer between reactor is all the mode adopting series connection, the catalyzer that this mode of movement is only transported to first reactor from revivifier is only just regenerated " fresh " active high catalyzer, such as first reforming reactor of " following current " CONTINUOUS REFORMER, last reforming reactor of " adverse current " CONTINUOUS REFORMER, and the catalyzer in other reforming reactor is all the used catalyzer reduced containing carbon deposition activity of reactor above, catalyzer is carried more backward, its activity is lower, activity in the reactor that catalyzer leaves is minimum.The activity of catalyzer can not give full play in all reactors as can be seen here.The mode of this catalyst cascade conveying, all identical by the catalyst recirculation amount of each reactor, the necessary cyclic regeneration simultaneously of all catalyzer in each reactor, the catalyst flow of each reactor can not carry out independence on demand and regulates and change, and cannot carry out cyclic regeneration separately.
CN 203513593 U discloses a kind of CONTINUOUS REFORMER of regeneration side by side system, this system comprises catalyzer reformer (relative to revivifier) and the charging/effluent exchanger, process furnace and the reactor that are connected successively, and catalyzer reformer is provided with the variable valve for regulating catalyst circulation rate.Although this system can regulate catalyst circulation rate according to response situation and catalyzer coking situation because being equipped with described variable valve, but the flow direction with regard to reaction feed and catalyzer is still the form of aforementioned " following current " continuous reforming process, does not overcome the foregoing problems of " following current " continuous reforming process.
Utility model content
The purpose of this utility model is to provide a kind of hydro carbons continuous reformer, make the multiple reactors in this device can use fresh high activity regenerated catalyzer, and can regulate independently as required and change the catalyst recirculation amount in these reactors, to give full play to the activity of catalyzer, improve the utilization ratio of catalyzer, improve the operability of device, improve reforming conversion and product yield.
To achieve these goals, the utility model provides a kind of continuous reformer of hydro carbons, this device comprises the first reforming reactor 3, second reforming reactor 5, tri-reforming device 7 and the 4th reforming reactor 9 successively, and a revivifier 14, it is characterized in that: connected by reaction mass Tandem between each reforming reactor, namely the outlet of the reaction mass of previous reforming reactor is communicated with the entrance of the reaction mass of a rear reforming reactor; The catalyst outlet of the first reforming reactor 3 is connected by catalyst channels with the catalyst inlet of the second reforming reactor 5, and the catalyst outlet of tri-reforming device 7 is also connected by catalyst channels with the catalyst inlet of the 4th reforming reactor 9; The catalyst outlet of the second reforming reactor 5 and the catalyst outlet of the 4th reforming reactor 9 are connected in parallel respectively by the catalyst inlet of catalyst transport passage and revivifier 14; And the catalyst inlet of the first reforming reactor 3 and the catalyst inlet of tri-reforming device 7 are connected in parallel respectively by the catalyst outlet of catalyst transport passage and revivifier 14.
Preferably, described hydro carbons continuous reformer, it is characterized in that: this device is set to: be opportunity independent controlled from the second reforming reactor 5 and the 4th reforming reactor 9 to the operational throughput of the reclaimable catalyst of described revivifier 14 and/or conveying, and from described revivifier to the operational throughput of the regenerated catalyst of the first reforming reactor 3 and tri-reforming device 7 and/or conveying opportunity be independent controlled.
Preferably, described hydro carbons continuous reformer, this device also comprises a regenerated catalyst reprocessing and a distribution system RCTS12 and reclaimable catalyst reprocessing and distribution system WCTS13; The catalyst inlet of RCTS12 and the catalyst outlet UNICOM of revivifier 14, the catalyst outlet of RCTS12 and the catalyst inlet UNICOM of the first reforming reactor 3 and tri-reforming device 7; The catalyst inlet of WCTS13 and the catalyst outlet UNICOM of the second reforming reactor 5 and the 4th reforming reactor 9, the catalyst outlet of WCTS13 and the catalyst inlet UNICOM of revivifier 14.
Preferably, described hydro carbons continuous reformer, it is characterized in that: the catalyst outlet of the second reforming reactor 5 and the catalyst outlet of the 4th reforming reactor 9 promote blower fan 15 catalyst transport passage by being provided with reclaimable catalyst is communicated with distribution system WCTS13 with reclaimable catalyst reprocessing, reclaimable catalyst reprocessing is communicated with by the catalyst inlet of tremie pipe with revivifier 14 with distribution system WCTS13, and described WCTS13 is divided into low pressure area, top and high pressure area, bottom; The catalyst inlet of the first reforming reactor 3 is communicated with distribution system RCTS12 with regenerated catalyst reprocessing by catalyst transport passage with the catalyst inlet of tri-reforming device 7, and regenerated catalyst reprocessing and distribution system RCTS12 promote blower fan 16 catalyst transport passage by being provided with regenerated catalyst is communicated with the catalyst outlet of revivifier 14.
Preferably, described hydro carbons continuous reformer, is characterized in that: be provided with process furnace 2,4,6,8 in the described reaction mass passage of the material front end of each reforming reactor 3,5,7,9.
Preferably, described hydro carbons continuous reformer, is characterized in that: the position of reclaimable catalyst reprocessing and distribution system WCTS13 bottom is higher than the position of the catalyst inlet of revivifier 14; The position of regenerated catalyst reprocessing and distribution system RCTS12 bottom is higher than the position of the catalyst inlet of the first reforming reactor 3 and the catalyst inlet of tri-reforming device 7.
Preferably, described hydro carbons continuous reformer, is characterized in that: the first reforming reactor 3 and the second reforming reactor 5 are for setting up and down, and the first reforming reactor 3 is positioned at the top of the second reforming reactor 5; Tri-reforming device 7 and the 4th reforming reactor 9 are also setting up and down, and tri-reforming device 7 is also positioned at the top of the 4th reforming reactor 9.
The utility model overcomes by changing the circulation mode of movement of catalyzer between multiple moving-burden bed reactor the shortcoming that in existing industrialized technology, each catalyst reactor activity can not give full play to, and the catalyzer in multiple reforming reactor in parallel can carry out cyclic regeneration simultaneously.Between reaction and regeneration system rapidly, adopt the mode of conveying catalyzer in parallel, make the catalyzer entered in multiple reactor be all just regenerated high reactivity " fresh " catalyzer, reclaimable catalyst rises to regeneration system rapidly from the independent parallel connection of reactor, make the catalyzer from reactor to revivifier promote operational throughput can carry out as required regulating and changing, circulation conveying and the regeneration of catalyzer can be carried out neatly, thus optimize reaction and regeneration condition, make multiple reactor can use fresh high activated catalyst and carry out independence on demand regulate and change catalyst flow, reduce carbon deposit on catalyzer, to give full play to the activity of catalyzer, improve the utilization ratio of catalyzer, the life-span of extending catalyst, reduce the temperature in of each reactor, the side reaction reducing CONTINUOUS REFORMER occurs, improve reforming conversion and product yield, increasing gasoline yield and hydrogen, increase the benefit.In reforming reaction, what first reactor carried out is the reaction relatively easily carried out, on catalyzer, carbon deposit is few, activity decrease is less, directly can enter the second reactor and continue application, so the first reforming reactor and the second reforming reactor are connected in series by catalyst channels, thus decrease the number of times of catalyzer lifting.The reacting phase carried out in second reactor is more difficult for first reactor, and the catalyst carbon deposition leaving the second reactor is relatively many, and activity decrease is also more, so the catalyzer leaving the second reactor needs to regenerate.In the third and fourth reactor, reaction mass carries out the reactions such as cyclization of paraffins dehydrogenation, and it is more difficult to react, so need fresh catalyzer.The utility model overcomes by changing the circulation mode of movement of catalyzer between multiple reforming reactor the shortcoming that in existing industrialized technology, each catalyst reactor activity can not give full play to.
Other feature and advantage of the present utility model are described in detail in embodiment part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide further understanding of the present utility model, and forms a part for specification sheets, is used from explanation the utility model, but does not form restriction of the present utility model with embodiment one below.In the accompanying drawings:
Fig. 1 is the schematic diagram of existing downflow system hydro carbons continuous reformer
Fig. 2 is the schematic diagram of existing reverse-flow hydro carbons continuous reformer
Fig. 3 is the schematic diagram according to hydro carbons continuous reformer of the present utility model
Description of reference numerals
101 reaction feed/product exchanger 102 first reaction heating furnace
103 first reforming reactor (is anti-) 104 second reaction heating furnaces
105 second reforming reactor (two is anti-) 106 the 3rd reaction heating furnaces
107 tri-reforming device (three is anti-) 108 the 4th reaction heating furnaces
109 the 4th reforming reactor (four is anti-) 110 regenerated catalyst lifters
111 4 anti-top hopper 112 4 anticatalyzer lifters
113 3 anti-top hopper 114 3 anticatalyzer lifters
115 2 anti-top hopper 116 2 anticatalyzer lifters
117 1 anti-top hopper 118 reclaimable catalyst lifters
119 are separated hopper 120 revivifier
201 reaction feed/product exchanger 202 first reaction heating furnace
203 first reforming reactor (is anti-) 204 second reaction heating furnaces
205 second reforming reactor (two is anti-) 206 the 3rd reaction heating furnaces
207 tri-reforming device (three is anti-) 208 the 4th reaction heating furnaces
209 the 4th reforming reactor (four is anti-) 210 regenerated catalyst lifters
211 4 anti-top hopper 212 4 anticatalyzer lifters
213 3 anti-top hopper 214 3 anticatalyzer lifters
215 2 anti-top hopper 216 2 anticatalyzer lifters
217 1 anti-top hopper 218 reclaimable catalyst lifters
219 are separated hopper 220 revivifier
1 reaction feed/product exchanger 2 first reaction heating furnace
3 first reforming reactor 4 second reaction heating furnaces
5 second reforming reactor 6 the 3rd reaction heating furnaces
7 tri-reforming device 8 the 3rd reaction heating furnaces
9 the 4th reforming reactor 10 1 anti-top hoppers
11 3 anti-top hopper 12 regenerated catalyst reprocessing and distribution systems (RCTS)
13 reclaimable catalyst reprocessing and distribution system (WCTS) 14 revivifier
15 reclaimable catalysts promote blower fan 16 regenerated catalyst and promote blower fan
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the utility model, is not limited to the utility model.
The utility model provides a kind of continuous reformer of hydro carbons, this device comprises the first reforming reactor 3, second reforming reactor 5, tri-reforming device 7 and the 4th reforming reactor 9 successively, and a revivifier 14, it is characterized in that: connected by reaction mass Tandem between each reforming reactor, namely the outlet of the reaction mass of previous reforming reactor is communicated with the entrance of the reaction mass of a rear reforming reactor; The catalyst outlet of the first reforming reactor 3 is connected by catalyst channels with the catalyst inlet of the second reforming reactor 5, and the catalyst outlet of the second reforming reactor 5 is also connected by catalyst channels with the catalyst inlet of tri-reforming device 7; The catalyst outlet of tri-reforming device 7 and the catalyst outlet of the 4th reforming reactor 9 are connected in parallel respectively by the catalyst inlet of catalyst transport passage and revivifier 14; And the catalyst inlet of the catalyst inlet of the first reforming reactor 3 and the 4th reforming reactor 9 is connected in parallel respectively by the catalyst outlet of catalyst transport passage and revivifier 14.
According to hydro carbons continuous reformer of the present utility model, described reforming reactor is the moving-burden bed reactor known by those skilled in the art; Moving-burden bed reactor can be 2 ~ 6 series connection, is preferably 3 ~ 4 series connection; Described revivifier realizes cyclic regeneration for making the reclaimable catalyst through reacting inactivation, comprise burn, oxychlorination, drying (or roasting), the technique such as reduction device, the reclaimable catalyst activity recovery making carbon content high, the quantity of revivifier is preferably one, also can arrange again one for subsequent use.
According to a kind of embodiment of the present utility model, this hydro carbons continuous reformer can comprise four reforming reactors and a revivifier, i.e. the first reforming reactor 3, second reforming reactor 5, tri-reforming device 7, the 4th reforming reactor 9 and revivifier 14.More specifically, this device can also comprise reaction feed/product exchanger 1, first reaction heating furnace 2, second reaction heating furnace 4, the 3rd reaction heating furnace 6, the 4th process furnace 8, anti-top hopper 10, three anti-top hopper 11, regenerated catalyst reprocessing and distribution system RCTS12, reclaimable catalyst reprocessing and distribution system WCTS13, reclaimable catalyst lifting blower fan 15 and regenerated catalyst lifting blower fan 16.As shown in Figure 3.
According to a kind of embodiment of the present utility model, the first reforming reactor 3 and the second reforming reactor 5 can be setting up and down, and the first reforming reactor 3 can be positioned at the top of the second reforming reactor 5; Tri-reforming device 7 and the 4th reforming reactor 9 also can be setting up and down, and tri-reforming device 7 also can be positioned at the top of the 4th reforming reactor 9.
According to a kind of concrete embodiment of the present utility model, described reaction feed/product exchanger 1, first reaction heating furnace 2, first reforming reactor 3, second reaction heating furnace 4, second reforming reactor 5, the 3rd reaction heating furnace 6, tri-reforming device 7, the 4th reaction heating furnace 8 are connected by reaction mass Tandem successively with the 4th reforming reactor 9, and the 4th reforming reactor 9 is connected with reaction feed/product exchanger 1 again by reaction mass passage.Reactor operating pressure order is from high to low: the first reforming reactor 3, second reforming reactor 5, tri-reforming device 7 and the 4th reforming reactor 9.Second and the 4th reforming reactor 5, the lower end of 9 is connected with WCTS13 by the catalyst transport pipeline being provided with reclaimable catalyst lifting blower fan 15, WCTS13 is connected with revivifier 14 by 1 tremie pipe, revivifier 14 is connected with RCTS12 with the catalyst transport pipeline being provided with regenerated catalyst lifting blower fan 16 by 1 tremie pipe successively, RCTS12 by 2 tremie pipes respectively and be positioned at first and tri-reforming device 3, one of 7 upper ends are instead connected with three anti-top hoppers 10,11.
According to hydro carbons continuous reformer of the present utility model, described regenerated catalyst reprocessing and distribution system RCTS12 may be used for carrying out dust elutriation, reduction and reallocation to regenerated catalyst, are then delivered to respectively in each reforming reactor for chemical reaction process by tremie pipe in the mode of parallel side-by-side.By arranging RCTS12, pipage control and further process can be carried out to regenerated catalyst better.
According to hydro carbons continuous reformer of the present utility model, described reclaimable catalyst reprocessing and distribution system WCTS13 may be used for mixing reclaimable catalyst, dust elutriation and locking transformation, are then delivered to revivifier by tremie pipe and regenerate.By arranging WCTS13, pipage control and further process can be carried out to reclaimable catalyst better.
According to hydro carbons continuous reformer of the present utility model, described reaction mass passage and catalyst transport passage are well-known to those skilled in the art, and there is no particular limitation to it for the utility model.Such as, reaction mass passage can comprise line of pipes and necessary pumping equipment or analogue; Temperature required in order to make reaction mass reach reaction, in the material channel of each reforming reactor front end, can process furnace be set.Equally, such as, catalyst transport passage can comprise catalyst transport pipeline, reclaimable catalyst for reclaimable catalyst is risen to WCTS or revivifier from reforming reactor promotes blower fan, and promotes blower fan etc. for the regenerated catalyst that the catalyzer after regeneration is risen to RCTS or each reforming reactor from revivifier.
According to another kind of embodiment of the present utility model, described WCTS13 is divided into low pressure area, top and high pressure area, bottom; The object arranging high pressure area is when reclaimable catalyst is after low pressure area processes and enters high pressure area, and because the pressure ratio revivifier internal pressure of high pressure area is large, catalyzer can flow in revivifier automatically.
Be described below in conjunction with the working process of accompanying drawing 3 to a kind of embodiment of the present utility model.Due to carried out be long commerical test, wherein said various process conditionss allow the fluctuation of approximately ± 10%.
As shown in Figure 3, reaction feed in reaction feed/product exchanger 1 with reaction product heat exchange after successively through the first reaction heating furnace 2, first reforming reactor 3, second reaction heating furnace 4, second reforming reactor 5, the 3rd reaction heating furnace 6, tri-reforming device 7, the 4th reaction heating furnace 8 and the 4th reforming reactor 9, after reaction product leaves reactor 9, with reaction feed heat exchange in reaction feed/product exchanger 1, and then be separated to follow-up tripping device.Reactant produces Pressure Drop in flow process, and reactor operating pressure order is from high to low: the first reforming reactor 3, second reforming reactor 5, tri-reforming device 7 and the 4th reforming reactor 9.
Catalyzer after revivifier 14 regenerates promotes blower fan 16 nitrogen by regenerated catalyst and rises to RCTS12 from revivifier 14.In RCTS12, first carry out the dust elutriation of catalyzer, then reusable heat hydrogen reduces to the catalyzer after removing dust, and the nitrogen after removing dust is delivered to regenerated catalyst and promoted blower fan 16 as the use of regenerated catalyst lifting nitrogen circulation.Catalyzer after reduction enters into anti-top hopper 10 and three anti-top hoppers 11 by gravity respectively by 2 tremie pipes, and then enter corresponding first reforming reactor 3 and tri-reforming device 7 respectively by gravity, the catalyst stream entering the first reforming reactor 3 participates in after reformate chemical reaction through beds, the second reforming reactor 5 is entered by the dipleg between two reactors again by gravity, the catalyst stream entering tri-reforming device 7 participates in after reformate chemical reaction through beds, the 4th reforming reactor 9 is entered by the dipleg between two reactors again by gravity, catalyzer participates in chemical reaction process in each reactor.First reforming reactor 3 and tri-reforming device 7 used be all just regenerated highly active catalyzer.Catalyst stream amount control device can be set on described tremie pipe or top hopper, to realize controlling even to dam to the flow of the regenerated catalyst entered in each reactor.In two group reaction devices, the working pressure of the first reforming reactor 3 is the highest, and in order to make the catalyzer of RCTS12 can enter each group reaction device, the pressure of RCTS is higher than anti-top hopper 10 and first reforming reactor 3.
Reclaimable catalyst promotes blower fan 15 nitrogen by reclaimable catalyst and promotes from the second reforming reactor 5 and the 4th reforming reactor 9 low pressure area, top being delivered to WCTS13 respectively, and the working pressure of WCTS low pressure area is lower than the 4th reforming reactor 9.Promoting conveying from the second reforming reactor 5 and the 4th reforming reactor 9 to the catalyzer of revivifier 14 is all independently, can carry out change as required and promote operational throughput.First catalyzer is mixed in WCTS13 low pressure area, and then carry out the dust elutriation of catalyzer, nitrogen after removing dust is delivered to reclaimable catalyst and is promoted blower fan 15 as the use of reclaimable catalyst lifting nitrogen circulation, catalyzer after removing dust boosts through locking again, the high pressure area of WCTS13 bottom delivered to by catalyzer after boosting, the working pressure of high pressure area is higher than revivifier 14, reclaimable catalyst is delivered to revivifier 14 by tremie pipe from the high pressure area of WCTS13 again and regenerates, the pressure of revivifier 14 is higher than RCTS12, the catalyzer leaving revivifier is promoted to RCTS12, so far the delivery cycle of catalyzer is completed.
The working process of this embodiment adopts C6 ~ C12 petroleum naphtha hydro carbons to carry out the reactions such as cycloalkanes dehydrogenation, cyclization of paraffins dehydrogenation, isomerization and hydrocracking in the hydrogen gas atmosphere, hydrogen/the oil ratio 2.1 of reaction raw materials, P/N/A consists of 58/30/12 (wt%), inlet amount is 600,000 tons/year, and the time of CONTINUOUS REFORMER is 1 year.Reaction feed petroleum naphtha and hydrogen mixture are after reaction feed/product exchanger 1 heat exchange, successively through the first reaction heating furnace 2, first reforming reactor 3, second reaction heating furnace 4, second reforming reactor 5, the 3rd reaction heating furnace 6, tri-reforming device 7, the 4th reaction heating furnace 8 and the 4th reforming reactor 9, after reaction product leaves reactor 9, with reaction feed heat exchange in reaction feed/product exchanger 1, and then be separated to follow-up tripping device.First reforming reactor 3 inlet pressure 0.56MPa (g), the second reforming reactor 5 inlet pressure 0.49MPa (g), tri-reforming device 7 inlet pressure 0.43MPa (g), the 4th reforming reactor 9 inlet pressure 0.35MPa (g), reaction weight space velocity is 2.1, and the temperature in of each reactor is 519 DEG C.
The PS-VI continuous reforming catalyst containing noble metal platinum (Pt) and tin (Sn) and other auxiliarys that the catalyzer used is developed for Research Institute of Petro-Chemical Engineering (RIPP).The catalyzer carbon content left after revivifier 14 regeneration is less than 0.2% (wt), promotes blower fan 16 nitrogen rise to RCTS12 from revivifier 14 by regenerated catalyst.In RCTS, first carry out the dust elutriation of catalyzer, reusable heat hydrogen reduces to the catalyzer after removing dust, and the nitrogen after removing dust is delivered to regenerated catalyst and promoted blower fan 16 as the use of regenerated catalyst lifting nitrogen circulation.The working pressure of RCTS12 reduction zone is 0.58MPa (g), than the first reforming reactor height 0.02MPa (g).Catalyzer after reduction enters into anti-top hopper 10 and three anti-top hoppers 11 respectively by gravity after 2 tremie pipes leave RCTS, and then enter corresponding first reforming reactor 3 and tri-reforming device 7 respectively by gravity, the catalyst stream entering the first reforming reactor 3 participates in entering the second reforming reactor 5 by gravity by the dipleg between two reactors again after reformate chemical reaction through beds, the catalyst stream entering tri-reforming device 7 participates in entering the 4th reforming reactor 9 by gravity by the dipleg between two reactors again after reformate chemical reaction through beds, catalyzer participates in chemical reaction process in each reactor, first reforming reactor 3 and tri-reforming device 7 used be all just regenerated highly active catalyzer.
The carbon deposition quantity leaving the reclaimable catalyst of each reactor is 2.8% ~ 3.3% (wt).Reclaimable catalyst promotes blower fan 15 nitrogen by reclaimable catalyst and promotes from the second reforming reactor 5 and the 4th reforming reactor 9 low pressure area, top being delivered to WCTS13 respectively, the working pressure of low pressure area, WCTS13 top is 0.30MPa, than the low 0.05MPa of the 4th reforming reactor 9.Promote conveying all independently to carry out from the second reforming reactor 5 and the 4th reforming reactor 9 to the catalyzer of WCTS13, the catalyzer that can change each group reaction device as required promotes operational throughput, also can promote conveying separately to the reclaimable catalyst in single group reaction device, the circulation conveying of catalyzer can be carried out neatly.In WCTS13 low pressure area, first catalyzer is mixed, and then carry out the dust elutriation of catalyzer, nitrogen after removing dust is delivered to reclaimable catalyst and is promoted blower fan 15 as the use of reclaimable catalyst lifting nitrogen circulation, catalyzer after removing dust boosts through locking again, the high pressure area of WCTS13 bottom delivered to by catalyzer after boosting, the working pressure of high pressure area is 0.68MPa, reclaimable catalyst is delivered to revivifier 14 by tremie pipe from the high pressure area of WCTS13 again and regenerates, the working pressure of revivifier is 0.65 MPa (g), catalyzer after regeneration promotes and is delivered to RCTS12, complete the circulation of catalyzer.
The utility model hydro carbons continuous reformer adopts the mode of catalyzer parallel circulating conveying, the catalyzer making to enter in wherein multiple reactor is all just regenerated " fresh " catalyzer, reactor average product carbon amounts is low, and the effect of catalyzer more can be not fully exerted.Enter the catalyst exposure that reaction mass in these reactors is all higher with just regenerated activity, reduce bed medial temperature about 4 ~ 5 DEG C, thus reduce the side reactions such as hydrocracking, and reduce the carbon distribution on catalyzer, the life-span of extending catalyst.
Under identical operating mode, operation and reaction conditions, hydro carbons continuous reformer described in the utility model adds gasoline products yield 1.0% compared with existing industrialized continuous reformer, C5+ liquid yield increases by 0.9%, and hydrogen yield adds 2.0%.For the catalytic reforming unit that a set for the treatment of capacity is 1,000,000 tons/year, annual increasing gasoline yield 1.0 ten thousand tons, increases income 3,000 ten thousand yuan.Annual volume increase hydrogen 700 tons, increases income 7,000,000 yuan.
Due in the working process of this embodiment, the utility model continuous reformer and the operating mode of existing industrial continuous reformer adopt identical air speed and identical catalyst filling ratio, and namely the operating mode of continuous reformer described in the utility model is not optimized.If optimize the reaction conditions (as catalyst filling ratio etc.) of continuous reformer described in the utility model, then can reduce catalyst filling amount or improve liquid yield further, increasing the benefit.
Claims (7)
1. the continuous reformer of a hydro carbons, this device comprises the first reforming reactor (3), the second reforming reactor (5), tri-reforming device (7) and the 4th reforming reactor (9) successively, and a revivifier (14), it is characterized in that: connected by reaction mass Tandem between each reforming reactor, namely the outlet of the reaction mass of previous reforming reactor is communicated with the entrance of the reaction mass of a rear reforming reactor; The catalyst outlet of the first reforming reactor (3) is connected by catalyst channels with the catalyst inlet of the second reforming reactor (5), and the catalyst outlet of tri-reforming device (7) is also connected by catalyst channels with the catalyst inlet of the 4th reforming reactor (9); The catalyst outlet of the second reforming reactor (5) and the catalyst outlet of the 4th reforming reactor (9) are connected in parallel respectively by the catalyst inlet of catalyst transport passage and revivifier (14); And the catalyst inlet of the first reforming reactor (3) and the catalyst inlet of tri-reforming device (7) are connected in parallel respectively by the catalyst outlet of catalyst transport passage and revivifier (14).
2. hydro carbons continuous reformer according to claim 1, it is characterized in that: this device is set to: be opportunity independent controlled from the second reforming reactor (5) and the 4th reforming reactor (9) to the operational throughput of the reclaimable catalyst of described revivifier (14) and/or conveying, and from described revivifier to the operational throughput of the regenerated catalyst of the first reforming reactor (3) and tri-reforming device (7) and/or conveying opportunity be that independence is controlled.
3. hydro carbons continuous reformer according to claim 1, this device also comprises a regenerated catalyst reprocessing and distribution system RCTS (12) and a reclaimable catalyst reprocessing and distribution system WCTS (13); The catalyst inlet of RCTS (12) and the catalyst outlet UNICOM of revivifier (14), the catalyst outlet of RCTS (12) and the catalyst inlet UNICOM of the first reforming reactor (3) and tri-reforming device (7); The catalyst outlet UNICOM of the catalyst inlet of WCTS (13) and the second reforming reactor (5) and the 4th reforming reactor (9), the catalyst outlet of WCTS (13) and the catalyst inlet UNICOM of revivifier (14).
4. according to the hydro carbons continuous reformer of claim 1 or 2, it is characterized in that: the catalyst outlet of the second reforming reactor (5) and the catalyst outlet of the 4th reforming reactor (9) promote blower fan (15) catalyst transport passage by being provided with reclaimable catalyst is communicated with distribution system WCTS (13) with reclaimable catalyst reprocessing, reclaimable catalyst reprocessing is communicated with by the catalyst inlet of tremie pipe with revivifier (14) with distribution system WCTS (13), and described WCTS (13) is divided into low pressure area, top and high pressure area, bottom; The catalyst inlet of the first reforming reactor (3) is communicated with distribution system RCTS (12) with regenerated catalyst reprocessing by catalyst transport passage with the catalyst inlet of tri-reforming device (7), and regenerated catalyst reprocessing and distribution system RCTS (12) promote blower fan (16) catalyst transport passage by being provided with regenerated catalyst is communicated with the catalyst outlet of revivifier (14).
5. according to the hydro carbons continuous reformer of claim 1 or 2, it is characterized in that: in the described reaction mass passage of the material front end of each reforming reactor (3,5,7,9), be provided with process furnace (2,4,6,8).
6. according to the hydro carbons continuous reformer of claim 1 or 2, it is characterized in that: the position of reclaimable catalyst reprocessing and distribution system WCTS (13) bottom is higher than the position of the catalyst inlet of revivifier (14); The position of regenerated catalyst reprocessing and distribution system RCTS (12) bottom is higher than the position of the catalyst inlet of the first reforming reactor (3) and the catalyst inlet of tri-reforming device (7).
7. according to the hydro carbons continuous reformer of claim 1 or 2, it is characterized in that: the first reforming reactor (3) and the second reforming reactor (5) are for setting up and down, and the first reforming reactor (3) is positioned at the top of the second reforming reactor (5); Tri-reforming device (7) and the 4th reforming reactor (9) are also setting up and down, and tri-reforming device (7) is also positioned at the top of the 4th reforming reactor (9).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420475368.9U CN204111693U (en) | 2014-08-21 | 2014-08-21 | Hydro carbons continuous reformer (five) |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420475368.9U CN204111693U (en) | 2014-08-21 | 2014-08-21 | Hydro carbons continuous reformer (five) |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106905996A (en) * | 2015-12-22 | 2017-06-30 | 中国石化工程建设有限公司 | A kind of hydro carbons continuous reforming process |
| CN117101552A (en) * | 2023-10-25 | 2023-11-24 | 万华化学集团股份有限公司 | Regeneration process of propane dehydrogenation catalyst |
-
2014
- 2014-08-21 CN CN201420475368.9U patent/CN204111693U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106905996A (en) * | 2015-12-22 | 2017-06-30 | 中国石化工程建设有限公司 | A kind of hydro carbons continuous reforming process |
| CN117101552A (en) * | 2023-10-25 | 2023-11-24 | 万华化学集团股份有限公司 | Regeneration process of propane dehydrogenation catalyst |
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