CN1247886A

CN1247886A - Catalytic conversion process in counter-flow moving bed with several reactors

Info

Publication number: CN1247886A
Application number: CN 98117972
Authority: CN
Inventors: 袁忠勋; 罗家弼; 任建生
Original assignee: Sinopec Beijing Design Institute; China Petrochemical Corp
Current assignee: Sinopec Beijing Design Institute; China Petrochemical Corp
Priority date: 1998-09-11
Filing date: 1998-09-11
Publication date: 2000-03-22
Anticipated expiration: 2018-09-11
Also published as: CN1068899C

Abstract

The present invention relates to the catalytic conversion of hydrocarbons and especially the reaction process of catalytic reforming. The present invention features that the reactant material flows forward from the first reactor to the last one while the fresh catalyst after being regenerated flows backward from the last reactor to the first one, i. e., catalyst flows between the reactors in the direction opposite to that of reactant material. Therefore, the activity state of catalyst in individual reactor matches with the difficulty of reaction and this can improve reaction state, optimize reaction condition, increase product yield, slow down the deactivation of the catalyst and prolong the service life of catalyst.

Description

A plurality of reactor catalytic conversion process in counter-flow moving bed

The invention belongs to the hydrocarbon moving bed catalytic conversion process, particularly the reaction process of catalytic reforming process.

The moving-bed catalytic conversion process of existing several reactors, reaction mass flows to the most last reactor successively from first reactor, reacts on the catalyzer in each reactor.The travel direction of catalyzer between each reactor is consistent with reaction mass, the high activated catalyst of promptly regenerating is introduced into first reactor by the order of reactant flow, pass through second reactor, the 3rd reactor then successively up to the last reactor, the catalyst activity that comes out from the last reactor is lower, be transported in the revivifier and regenerate, the catalyzer after the regeneration rises to the circulation that first reactor is finished catalyzer again.

Contain a plurality of components in the hydrocarbon material, the conversion rate difference of each reaction is very big, and being reflected in the reactor in front of carrying out easily carried out, and the catalyzer that is in contact with it is active very high catalyzer.And carry out in the reactor that is reflected at the back that is difficult to carry out, the catalyzer that is in contact with it but is active lower catalyzer.It is irrational that this reaction requires complexity and the unmatched phenomenon of catalyst activity height, the effect of catalyzer can not be given full play to, thereby influence the yield and the life of catalyst of product.

The patent more relevant with the present invention has CN1020111C and CN1031646C.In patent CN1020111C, catalyzer is consistent with reaction mass at the travel direction of reaction interval, same reaction complexity and the unmatched phenomenon of catalyst activity height of existing can not be given full play to the effect of catalyzer, and influenced product yield and catalyst life.The catalysis conversion method of the said petroleum hydrocarbon of patent CN1031646C is to carry out in riser tube or single fluidised bed reactor, is different from a plurality of reactor catalytic conversion process in counter-flow moving bed of the present invention in essence.

Purpose of the present invention is exactly will be by changing the flow direction of catalyzer between a plurality of moving-burden bed reactors, overcome the complexity and the unmatched shortcoming of catalyst activity height of reacting in each reactor in the prior art, thereby the optimization reaction conditions improves product yield.

The technical solution used in the present invention is: in a plurality of reactors of hydrocarbon moving bed catalyzed conversion, reaction mass flows forward from first reactor, second reactor successively, finishes entire reaction course until the last reactor.Then be introduced into the last reactor through the regenerated live catalyst, oppositely move forward successively then, up to first reactor.The catalyzer that first reactor comes out is sent to revivifier regeneration because of the more activity of carbon distribution is lower, and the catalyzer after the regeneration returns the most last reactor again, constitutes the circulation of catalyzer.The flow direction of catalyzer between each reactor is opposite with the flow direction of reaction mass, being reflected on the active relatively poor catalyzer of carrying out easily in reactor in front carried out, and being reflected on the active higher catalyzer of being difficult to carry out in the reactor of back carried out.

Because the pressure difference of front and back reactor, high back, front is low, and catalyzer is finished by handling machinery to the highly compressed countercurrent flow by low pressure between each reactor, then flows from top to bottom by gravity in each reactor.

Owing to adopt above-mentioned a plurality of reactor catalytic conversion process in counter-flow moving bed, fresh material enters in the front reaction device, the reaction of on the lower catalyzer of activity, carrying out easily, make reaction unlikely too fierce: when reactant enters the reaction that the end reaction device is difficult to carry out, contact with firm high activated catalyst of regenerating, help the carrying out of driving a reaction.Thereby make in each reactor, the complexity of activity of such catalysts state and reaction adapts, overcome the disadvantage of indented material fully, thereby improved the reaction condition in each reactor widely, play the optimization reaction conditions, increase product yield, the effect that slows down catalyst deactivation and prolong catalyst life.

Be described in further detail embodiments of the invention below in conjunction with accompanying drawing.

Fig. 1 is the schematic flow sheet of a plurality of reactor catalytic conversion process in counter-flow moving bed of the present invention.

Embodiment:

With the catalytic reforming is example, C6～C10 hydro carbons carries out the cycloalkanes dehydrogenation in hydrogen environment, the cyclization of paraffins dehydrogenation, reactions such as isomerizing hydrogenation cracking, reaction conditions is pressure 0.3～0.8MPa, 400～550 ℃ of temperature, as shown in Figure 1, the mixture of reaction mass petroleum naphtha and hydrogen by 2 heating of first process furnace, enters first reactor 3 then after interchanger 1 heat exchange.Because the endothermic heat of reaction temperature reduces, enter second reactor 5 after sending into 4 heating of second process furnace, then successively by the 3rd process furnace 6, the 3rd reactor 7, the 4th process furnace 8 and the 4th reactor 9, and then in interchanger 1, carry out removing subsequent reactions thing separating device after the heat exchange with charging, constitute the technical process of reactant.

Live catalyst after regeneration Continuous Flow in reaction process is crossed each reactor, after rising to hopper 11, handling machinery 10 enters the 4th reactor 9 successively, rise to hopper 13 by handling machinery 12 successively then and enter the 3rd reactor 7, rise to hopper 15 by handling machinery 14 and enter second reactor 5, rise to hopper 17 by handling machinery 16 and enter first reactor 3, rise to hopper 19 by handling machinery 18 again and enter dirt device 20 again, live catalyst after the regeneration arrives handling machinery 10 again, constitutes the circulation of catalyzer.

Carbon deposition quantity is zero on the catalyzer after the regeneration, and activity is the highest, progressively rise by carbon deposition quantity behind each reactor, and activity progressively descends, and last carbon deposition quantity reaches about 5%, and is active minimum.

Reaction mass mainly carries out speed of reaction cycloalkanes dehydrogenation reaction faster in the front reaction device, though the catalyst activity that is in contact with it is lower, and can be not influential to finishing reaction; On the contrary, owing to do not resemble the prior art fiercely in this dehydrogenation reaction of carrying out, the reactor upper and lower temperature difference reduces, and the effect of catalyzer more can be not fully exerted.Reaction mass mainly carries out reactions such as cyclization of paraffins dehydrogenation and isomerization in the reactor of rear end, speed of reaction is lower, the bed temperature of reaction is higher, contact with firm active higher catalyzer of regenerating, can reduce about 10～15 ℃ of temperature of reaction, thereby can reduce side reactions such as hydrocracking, it is about 1% to increase product yield (reformate), and can reduce carbon distribution on the catalyzer, prolongs life of catalyst.

Claims

1. hydrocarbon moving bed catalytic conversion process with a plurality of reactors is characterized in that:

(1) reaction mass flows forward from first reactor, second reactor successively, finish entire reaction course until the last reactor, then be introduced into the last reactor through the regenerated live catalyst, oppositely reach successively then is up to first reactor;

The catalyzer that (2) first reactors come out is sent to revivifier regeneration because of the more activity of carbon distribution is lower, and the catalyzer after the regeneration returns the most last reactor again, constitutes catalyst recirculation.

(3) flow direction of catalyzer between each reactor is opposite with the flow direction of reactant, being reflected on the active relatively poor catalyzer of carrying out easily in reactor in front carried out, and being reflected on the active higher catalyzer of being difficult to carry out in the reactor of back carried out.

2, the hydrocarbon moving bed catalytic conversion process with a plurality of reactors as claimed in claim 1 is characterized in that for catalytic reforming unit its technical process is:

(1) reaction mass, for example the mixture of petroleum naphtha and hydrogen passes through interchanger (1), first process furnace (2) successively, first reactor (3), second process furnace (4), second reactor (5), the 3rd process furnace (6), the 3rd reactor (7), the 4th process furnace (8), the 4th reactor (9) enters later separation equipment after entering interchanger (1) again.

(2) enter the 4th reactor (9) after the regeneration rear catalyst rises to hopper (11) with handling machinery (10), then successively by handling machinery (12), hopper (13), the 3rd reactor (7), handling machinery (14), hopper (15), second reactor (5), handling machinery (16), hopper (17), first reactor (3), handling machinery (18), hopper (19), revivifier (20), arrive handling machinery (10) again, constitute catalyst recirculation.

3, the hydrocarbon moving bed catalytic conversion process with a plurality of reactors as claimed in claim 1 or 2, it is characterized in that because front and back reactor pressure difference, high back, front is low, catalyzer is finished by handling machinery during to the high pressure countercurrent flow by low pressure between each reactor, then flows from top to bottom by gravity in each reactor.