CN204111687U - Hydro carbons continuous reformer (one) - Google Patents
Hydro carbons continuous reformer (one) Download PDFInfo
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- CN204111687U CN204111687U CN201420474738.7U CN201420474738U CN204111687U CN 204111687 U CN204111687 U CN 204111687U CN 201420474738 U CN201420474738 U CN 201420474738U CN 204111687 U CN204111687 U CN 204111687U
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 28
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 28
- 239000003054 catalyst Substances 0.000 claims abstract description 182
- 238000002407 reforming Methods 0.000 claims abstract description 118
- 238000006243 chemical reaction Methods 0.000 claims abstract description 85
- 238000012958 reprocessing Methods 0.000 claims description 24
- 238000000034 method Methods 0.000 claims description 22
- 230000008569 process Effects 0.000 claims description 21
- 239000000463 material Substances 0.000 claims description 3
- 230000000694 effects Effects 0.000 abstract description 21
- 230000008859 change Effects 0.000 abstract description 6
- 238000010438 heat treatment Methods 0.000 description 28
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 24
- 239000000428 dust Substances 0.000 description 14
- 230000008929 regeneration Effects 0.000 description 14
- 238000011069 regeneration method Methods 0.000 description 14
- 239000000047 product Substances 0.000 description 13
- 229910052757 nitrogen Inorganic materials 0.000 description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 10
- 229910052799 carbon Inorganic materials 0.000 description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 6
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 230000002411 adverse Effects 0.000 description 5
- 230000005484 gravity Effects 0.000 description 5
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 4
- 239000000571 coke Substances 0.000 description 4
- 125000004122 cyclic group Chemical group 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- 238000004517 catalytic hydrocracking Methods 0.000 description 2
- 238000006356 dehydrogenation reaction Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 150000001924 cycloalkanes Chemical class 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 238000007363 ring formation reaction Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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Abstract
The utility model discloses a kind of hydro carbons continuous reformer, this device comprises at least two reforming reactors and at least one catalyst regenerator, it is characterized in that: connected by reaction mass Tandem between each reforming reactor; Be connected in parallel by catalyst transport passage between each reforming reactor and revivifier, namely each reforming reactor is independently to the reclaimable catalyst conveying of revivifier, and revivifier is also independently to the regenerated catalyst conveying of each reforming reactor.In the utility model, all reactors can use fresh high activated catalyst and carry out independence on demand and regulate and change catalyst flow, can give full play to the activity of catalyzer, 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 all reactors can use fresh high activity regenerated catalyzer, and can regulate independently as required and change the catalyst recirculation amount in each reactor, 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 hydro carbons continuous reformer, this device comprises at least two reforming reactors and at least one catalyst regenerator, it is characterized in that: connected by reaction mass Tandem between each reforming reactor, and be connected in parallel by catalyst transport passage between each reforming reactor and revivifier.
Preferably, described hydro carbons continuous reformer, it is characterized in that: this device is set to: be opportunity independent controlled from reforming reactor described in each to the operational throughput of the reclaimable catalyst of described revivifier and/or conveying, and from described revivifier to the operational throughput of the regenerated catalyst of reforming reactor described in each 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 RCTS and reclaimable catalyst reprocessing and distribution system WCTS; The catalyst inlet of RCTS and the catalyst outlet UNICOM of revivifier, the catalyst inlet UNICOM of the catalyst outlet of RCTS and each reforming reactor; The catalyst outlet UNICOM of the catalyst inlet of WCTS and each reforming reactor, the catalyst outlet of WCTS and the catalyst inlet UNICOM of revivifier.
Preferably, described hydro carbons continuous reformer, it is characterized in that: the catalyst outlet of each reforming reactor is communicated with the catalyst inlet of reclaimable catalyst reprocessing with distribution system WCTS by the catalyst transport passage being provided with reclaimable catalyst lifting blower fan, reclaimable catalyst reprocessing is communicated with the catalyst inlet of revivifier by tremie pipe with the catalyst outlet of distribution system WCTS, and described WCTS is divided into low pressure area, top and high pressure area, bottom; The catalyst inlet of each reforming reactor is communicated with the catalyst outlet of regenerated catalyst reprocessing with distribution system RCTS by catalyst transport passage, and the catalyst outlet of revivifier is communicated with the catalyst inlet of regenerated catalyst reprocessing with distribution system RCTS by the catalyst transport passage being provided with regenerated catalyst lifting blower fan.
Preferably, described hydro carbons continuous reformer, is characterized in that: the position of the catalyst outlet of reclaimable catalyst reprocessing and distribution system WCTS is higher than the position of the catalyst inlet of revivifier; The position of the catalyst outlet of regenerated catalyst reprocessing and distribution system RCTS is higher than the position of the catalyst inlet of each reforming reactor.
Preferably, described hydro carbons continuous reformer, is characterized in that: be provided with process furnace in the described reaction mass passage of the material front end of each reforming reactor.
Preferably, described hydro carbons continuous reformer, is characterized in that: this device comprises 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.
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 entering each reactor be just regenerated high reactivity " fresh " catalyzer, reclaimable catalyst rises to regeneration system rapidly from the independent parallel connection of each reactor, make the catalyzer from each 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 all reactors 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, thus improve reforming conversion and product yield, increasing gasoline yield and hydrogen, increase the benefit.
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 and uses novel further understanding to this, 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 (is anti-) 4 second reaction heating furnaces
5 second reforming reactor (two is anti-) 6 the 3rd reaction heating furnaces
7 tri-reforming device (three is anti-) 8 the 4th reaction heating furnaces
9 the 4th reforming reactor (four is anti-) 10 1 anti-top hoppers
11 2 anti-top hopper 12 3 anti-top hoppers
13 4 anti-top hopper 14 revivifiers
15 regenerated catalyst reprocessing and distribution system (RCTS)
16 reclaimable catalyst reprocessing and distribution system (WCTS)
17 reclaimable catalysts promote blower fan 18 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 hydro carbons continuous reformer, this device comprises at least two reforming reactors and at least one catalyst regenerator, it is characterized in that: connected by reaction mass Tandem between each reforming reactor, and be connected in parallel by catalyst transport passage between each reforming reactor and revivifier.
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, described hydro carbons continuous reformer can also comprise a regenerated catalyst reprocessing and a distribution system RCTS and reclaimable catalyst reprocessing and distribution system WCTS; The catalyst inlet of RCTS and the catalyst outlet UNICOM of revivifier, the catalyst inlet UNICOM of the catalyst outlet of RCTS and each reforming reactor; The catalyst outlet UNICOM of the catalyst inlet of WCTS and each reforming reactor, the catalyst outlet of WCTS and the catalyst inlet UNICOM of revivifier.Described regenerated catalyst reprocessing and distribution system RCTS 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.Described reclaimable catalyst reprocessing and distribution system WCTS may be used for mixing reclaimable catalyst, dust elutriation and locking transformation, are then delivered to revivifier by tremie pipe and regenerate.By arranging RCTS and WCTS, pipage control and further process can be carried out to regenerated catalyst or reclaimable catalyst better.
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 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 reaction heating furnace 8, anti-top hopper 10, two anti-top hopper 11, three anti-top hopper 12, four anti-top hopper 13, regenerated catalyst reprocessing and distribution system RCTS15, reclaimable catalyst reprocessing and distribution system WCTS16, reclaimable catalyst lifting blower fan 17 and regenerated catalyst lifting blower fan 18.As shown in Figure 3.
According to a kind of 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.First, second, third and fourth reforming reactor 3, 5, 7, the catalyst outlet of 9 is connected with WCTS16 by the catalyst transport pipeline being provided with reclaimable catalyst lifting blower fan 17, WCTS16 is connected with revivifier 14 by 1 tremie pipe, revivifier 14 is connected with RCTS15 with the catalyst transport pipeline being provided with regenerated catalyst lifting blower fan 18 by 1 tremie pipe successively, RCTS15 by 4 tremie pipes respectively and be positioned at first, second, third and fourth reforming reactor 3, 5, 7, 9 catalyst inlets one anti-, two is anti-, three anti-and four anti-top hoppers 10, 11, 12, 13 are connected.
According to another embodiment of the present utility model, described WCTS 15 can be 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, reaction product is left reactor 9 and is separated with reaction feed heat exchange and then to follow-up tripping device in reaction feed/product exchanger 1.Reaction mass 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 18 nitrogen by regenerated catalyst and rises to RCTS15 from revivifier 14.In RCTS15, 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 18 as the use of regenerated catalyst lifting nitrogen circulation.The pressure of RCTS15 is higher than anti-top hopper 10 and first reforming reactor 3, and the catalyzer after reduction enters each reactor top hopper 10,11 by gravity respectively by 4 tremie pipes, 12,13, finally enter corresponding reactor 3 by gravity again, 5,7, carry out chemical reaction in 9.Used in each reactor is 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.Blower fan 17 nitrogen is promoted by reclaimable catalyst respectively from each reforming reactor 3 with reclaimable catalyst, 5,7,9 promote the low pressure area, top being delivered to WCTS16, the working pressure of low pressure area, WCTS16 top is lower than the 4th reforming reactor 9, promoting conveying from each reactor to the catalyzer of WCTS is independently, and to promote operational throughput be controlled, can change the lifting operational throughput of reclaimable catalyst as required.In the low pressure area, top of WCTS16, 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 17 as the use of reclaimable catalyst lifting nitrogen circulation, catalyzer after removing dust carries out locking transformation again, catalyzer after boosting enters the high pressure area, bottom of WCTS16 again, the working pressure of high pressure area is higher than revivifier 14, catalyzer after boosting is delivered to revivifier 14 by tremie pipe and regenerates, the pressure of revivifier 14 is higher than RCTS15, the catalyzer leaving revivifier is promoted to RCTS, 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.Reaction feed (petroleum naphtha and hydrogen mixture) is 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 the 4th reforming 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 is about 0.56MPa (g), the second reforming reactor 5 inlet pressure is about 0.49MPa (g), tri-reforming device 7 inlet pressure is about 0.42MPa (g), the 4th reforming reactor 9 inlet pressure is about 0.35MPa (g).
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) substantially, promotes blower fan 18 nitrogen rise to RCTS15 from revivifier 14 by regenerated catalyst.First the dust elutriation of catalyzer is carried out in RCTS15, then reduce to the catalyzer after removing dust with hot hydrogen in RCTS15, the nitrogen after removing dust is delivered to regenerated catalyst and is promoted blower fan 18 as the use of regenerated catalyst lifting nitrogen circulation.Working pressure 0.01 ~ 0.08MPa, than the revivifier 14 low 0.01 ~ 0.08MPa higher than the first reforming reactor working pressure of RCTS.Catalyzer after reduction enters reactor top hopper 10,11,12,13 by gravity respectively after 4 tremie pipes leave RCTS, and then enters corresponding reforming reactor 3,5,7 by gravity from reactor top hopper, carries out chemical reaction in 9.Used in each reactor is all just regenerated highly active catalyzer.
Promote blower fan 17 with reclaimable catalyst reclaimable catalyst nitrogen promoted from each reforming reactor 3,5,7,9 to be respectively delivered to low pressure area, WCTS16 top, the working pressure of low pressure area than the low 0.01 ~ 0.08MPa of the 4th reforming reactor 9, lower than all reactors.Promote conveying from each reactor to the catalyzer of WCTS independently to carry out, the catalyzer that can change each reactor as required promotes operational throughput, also can promote conveying separately to the reclaimable catalyst in single or multiple reactor, the circulation conveying of catalyzer can be carried out flexibly.In low pressure area, WCTS16 top, first carry out the mixing of catalyzer, and then carry out the dust elutriation of catalyzer, the nitrogen after removing dust is delivered to reclaimable catalyst and is promoted blower fan 18 as the use of reclaimable catalyst lifting nitrogen circulation.Catalyzer after removing dust carries out locking transformation again, and the catalyzer after boosting enters the high pressure area, bottom of WCTS16 again, and the working pressure of high pressure area, bottom is than revivifier 14 height about 0.01 ~ 0.08MPa.The reclaimable catalyst of high pressure area is delivered to revivifier 14 by tremie pipe and regenerates, and the working pressure of revivifier is about 0.65MPa (g), and the catalyzer after regeneration promotes and is delivered to RCTS15, completes the circulation of catalyzer.
Reaction mass carries out reacting all making carbon deposit on catalyst surface in the reactor, leave coke content on the catalyzer of reactor than the height entering reactor, for the process of series connection conveying, carbon deposited catalyst will continue the reactor entered below, therefore, its coke content also can constantly accumulate, coke content more toward rear catalyst is higher, activity also constantly reduces, existing continuous reformer adopts this series connection mode of movement exactly, its catalyst recirculation makes the catalyst activity in downstream reactor lower than the reactor of upstream, the activity of catalyzer can not give full play to.Continuous reformer of the present utility model adopts the mode of catalyzer parallel circulating conveying, and make the catalyzer entering each reactor be just regenerated " fresh " catalyzer, the average coke content of reactor is low, and the effect of catalyzer more can be not fully exerted.Enter the catalyst exposure that reaction in each reactor is higher with just regenerated activity, bed medial temperature about 5 ~ 10 DEG C can be reduced, thus can the negative reactions such as hydrocracking be reduced, product yield about 1% can be increased compared with existing industrialized CONTINUOUS REFORMER technology, and the carbon deposit that can reduce on catalyzer, the life-span of extending catalyst.
Table 1 to list in the working process of embodiment respectively according to the utility model (conveying of catalyzer parallel circulating) and conventionally (conveying of catalyzer following current series circulation) carry out the test-results of three groups of controlled trials of hydro carbons CONTINUOUS REFORMER
Table 1
Continuous reformer described in the utility model has the following advantages compared with existing industrialized continuous reformer from the results shown in Table 1:
1, continuous reformer described in the utility model enters the catalyzer of each reactor is all the just regenerated live catalyst not containing carbon deposit, activity is the highest, at identical reaction severity conditions (reaction product reaches identical RON value), compared with existing industrialized CONTINUOUS REFORMER, the temperature in of four reactors declines 5 DEG C.
2, under identical reaction severity conditions, continuous reformer described in the utility model declines than existing industrialized continuous reformer average reaction temperature, makes the average carbon deposit rate on catalyzer reduce by 30 ~ 40%, C
5 +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, adopt continuous reformer described in the utility model compared with the existing continuous reformer of employing, annual increasing gasoline yield 0.7 ~ 1.1 ten thousand ton, increase income about 2100 ~ 3,300 ten thousand yuan, volume increase hydrogen 720 ~ 1700 tons, increases income about 720 ~ 1,700 ten thousand yuan.
In above-mentioned comparative example, 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. a hydro carbons continuous reformer, this device comprises at least two reforming reactors and at least one catalyst regenerator, it is characterized in that: connected by reaction mass Tandem between each reforming reactor, and be connected in parallel by catalyst transport passage between each reforming reactor and revivifier.
2. hydro carbons continuous reformer according to claim 1, it is characterized in that: this device is set to: be opportunity independent controlled from reforming reactor described in each to the operational throughput of the reclaimable catalyst of described revivifier and/or conveying, and from described revivifier to the operational throughput of the regenerated catalyst of reforming reactor described in each and/or conveying opportunity be independent controlled.
3. hydro carbons continuous reformer according to claim 1, this device also comprises a regenerated catalyst reprocessing and a distribution system RCTS and reclaimable catalyst reprocessing and distribution system WCTS; The catalyst inlet of RCTS and the catalyst outlet UNICOM of revivifier, the catalyst inlet UNICOM of the catalyst outlet of RCTS and each reforming reactor; The catalyst outlet UNICOM of the catalyst inlet of WCTS and each reforming reactor, the catalyst outlet of WCTS and the catalyst inlet UNICOM of revivifier.
4. hydro carbons continuous reformer according to claim 3, it is characterized in that: the catalyst outlet of each reforming reactor is communicated with the catalyst inlet of reclaimable catalyst reprocessing with distribution system WCTS by the catalyst transport passage being provided with reclaimable catalyst lifting blower fan, reclaimable catalyst reprocessing is communicated with the catalyst inlet of revivifier by tremie pipe with the catalyst outlet of distribution system WCTS, and described WCTS is divided into low pressure area, top and high pressure area, bottom; The catalyst inlet of each reforming reactor is communicated with the catalyst outlet of regenerated catalyst reprocessing with distribution system RCTS by catalyst transport passage, and the catalyst outlet of revivifier is communicated with the catalyst inlet of regenerated catalyst reprocessing with distribution system RCTS by the catalyst transport passage being provided with regenerated catalyst lifting blower fan.
5. hydro carbons continuous reformer according to claim 3, is characterized in that: the position of the catalyst outlet of reclaimable catalyst reprocessing and distribution system WCTS is higher than the position of the catalyst inlet of revivifier; The position of the catalyst outlet of regenerated catalyst reprocessing and distribution system RCTS is higher than the position of the catalyst inlet of each reforming reactor.
6. hydro carbons continuous reformer according to claim 1, is characterized in that: be provided with process furnace in the described reaction mass passage of the material front end of each reforming reactor.
7. according to the hydro carbons continuous reformer in claim 1 ~ 6 described in any one, it is characterized in that: this device comprises four reforming reactors and a revivifier, i.e. the first reforming reactor (3), the second reforming reactor (5), tri-reforming device (7), the 4th reforming reactor (9) and revivifier (14).
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| CN201420474738.7U CN204111687U (en) | 2014-08-21 | 2014-08-21 | Hydro carbons continuous reformer (one) |
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| CN201420474738.7U CN204111687U (en) | 2014-08-21 | 2014-08-21 | Hydro carbons continuous reformer (one) |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106905995A (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 |
| CN106906000A (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 |
| CN106905994A (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 |
| WO2021071535A1 (en) * | 2019-10-07 | 2021-04-15 | Saudi Arabian Oil Company | Systems and processes for catalytic reforming of a hydrocarbon feed stock |
-
2014
- 2014-08-21 CN CN201420474738.7U patent/CN204111687U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106905995A (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 |
| CN106906000A (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 |
| CN106905994A (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 |
| WO2021071535A1 (en) * | 2019-10-07 | 2021-04-15 | Saudi Arabian Oil Company | Systems and processes for catalytic reforming of a hydrocarbon feed stock |
| US11028328B2 (en) | 2019-10-07 | 2021-06-08 | Saudi Arabian Oil Company | Systems and processes for catalytic reforming of a hydrocarbon feed stock |
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