CN100491504C

CN100491504C - Partitioned catalytic conversion method for hydrocarbon material

Info

Publication number: CN100491504C
Application number: CNB200510048427XA
Authority: CN
Inventors: 石宝珍
Original assignee: Individual
Current assignee: Individual
Priority date: 2005-10-21
Filing date: 2005-10-21
Publication date: 2009-05-27
Anticipated expiration: 2025-10-21
Also published as: CN1952065A

Abstract

The invention relates to the catalytic cracking method of the alkanes. Its producing procedure includes the below catalytic cracking part and the top part of lowering temperature, reshaping and transforming; the fresh oil and recycled oil (back-refined oil, oil syrup or gasoline) undertaking the catalytic cracking reaction in the respective lift pipe; mixing the reacted oil and catalyst in the two lift pipes; aromatizing, isomerizing and hydrogen transferring the material in the same zone of transformation; making the material oil contact the catalyst at 610-650 Deg c, while the recycled oil contact the catalyst at 580-650 Deg C, lowering the temperature of the recycled oil in the steam generator to 200 Deg C and hydrocracking the material. The invention adopts the reflowing of the catalyst in the reactor to lower the contacting temperature in the material oil hydrocracking reaction; while the invention adopts direct cooling method to the lower the contacting temperature in the recycle oil hydrocracking reaction; it adopts the reflowing of the catalyst in the reactor to increase and regulate the content of catalyst in the reactor to improve the transforming effects. The invention doesn't change the recycled catalyst content which is needed to sustain the thermal balance of the reaction and it has no effect on the operating state of the other parts of the reactor; the invention can be realized by changing the lift pipes of the original hydrocracking devices. It can substantially increase the liquid yield and decrease the content of alkenes in the gasoline.

Description

A kind of partitioned catalytic conversion method for hydrocarbon material

Technical field

The invention belongs to the petroleum refining technology field, particularly a kind of catalytic cracking conversion method of hydrocarbon raw material of direct production low-alkene gasoline.

Background technology

Catalytic cracking unit is one of main device of refinery crude oil secondary processing, and the catalytic cracking reaction process realizes in riser reactor.In the conventional catalytic cracking unit, riser reactor only is a common pipe, always is about 40 meters.Stock oil after nozzle atomization by the speed about average 10～15 meter per seconds, was finished reaction through 3 seconds left and right sides time.

Over past ten years, catalytic cracking technology has been obtained very much progress.These progressive mainly giving the credit to going deep into that reaction process base reason is studied.Discover that different fractions has nothing in common with each other at the catalyzer environment therapeutic method to keep the adverse qi flowing downwardization, cracking process in the catalytically cracked stock, and also can the phase mutual interference under the common environment.At first cracking reaction mainly occurs in the zone of riser tube bottom 1/5th to 1/4th, catalyzer is rapid inactivation in this zone also, it is original 50% that its activity generally also has only in most of zone of back, and riser tube latter half efficient is very low, and the catalytic cracking effect reduces; Secondly, turning oil (recycle stock, slurry oil) is easier to gasification than other cut and is adsorbed by catalyzer, makes catalyst active center's inactivation very soon, has influenced the cracking of other cuts; And gasoline fraction forms higher olefin(e) centent.In view of the above, proposed to design the mentality of designing of reaction conditions by reaction mass character.

At first occurred the sectional scheme of riser tube, stock oil and turning oil separately enter the riser tube reaction at different positions.Normally turning oil (downstream) above stock oil enters riser tube.Make regenerated catalyst earlier with the stock oil reaction, and then with the turning oil contact reacts, avoided the influence of absorption too early of circulation slurry oil.The MED technology and the Chinese patent application 01119807.9 of domestic a large amount of uses are typical example.

Further develop in the process, people have proposed " two-stage catalytic cracking " scheme.I.e. direct two riser reactors of design make fresh feed oil and recycle stock, slurry oil respectively at different riser tube internal reactions, have solved mutual thousand problems of disturbing completely.The core of two sections designs is: (1) shortens the reaction times, and (2) press the separately reaction of reaction mass character.Advantage is to make the liquid product yield of catalytic cracking reaction improve 1～2%.

Interfere with each other problem in order to solve the reaction of stock oil, turning oil and gasoline simultaneously, Chinese patent application 0311944109,200410007518.4 has proposed to build three reactors, respectively in order to the scheme of the oil that processes raw material, turning oil and gasoline.

Though more than separate the cracking scheme by raw material and can solve, each cut long preferably and disturb low, the ropy problem of the purpose product yield that brings mutually because of the reaction times, but the measure of taking is to repeat to increase device basically, implement on the actual engineering to be restricted, what have almost can not implement.The riser tube that Chinese patent application 99213769.1,00134054.9 proposes is relay cascade reaction scheme up and down, make riser reactor be divided into two sections layouts of serial connection up and down, first section (riser reactor of bottom) is used for the stock oil cracking, reaction product is after isolating catalyzer, oil gas upwards enters second riser reactor on top, further reacts.In second riser tube, replenish new low-temp recovery catalyzer again.This has been divided into two all short riser tubes up and down to conventional riser tube with regard to equaling, and has solved the inefficient problem in conventional riser reactor top.Similar, the catalyzer that Chinese patent application 99109193.0,200410060430.9 has proposed will not react is told, and only replenishes the low-temp recovery catalyzer at the middle part, suitably improves riser tube second half section catalyst activity, improves the way of riser tube efficient.But in these inventions, the quality of reactor product is still undesirable, and especially content of olefin in gasoline is higher.

Patent CN1078094C, CN99105905.0, CN99109193.0 have proposed structurally reactor to be divided into the method reduction catalyzed reaction gasoline olefin of two reaction zones up and down, or produce propylene.Can significantly reduce the alkene of catalytic gasoline.

Patent CN1490383A has proposed stock oil in the two-stage catalytic technology and turning oil are separated reaction scheme and CN1078094C, CN99105905.0, the assembled scheme that partition scheme combines about among the CN99109193.0 both can reduce gasoline olefin, can increase liquid product yield again.But should invent each riser tube reactive moieties all by catalytic cracking and two reaction zones of catalyzed conversion, and then merge, substantially be to original two-stage catalytic and the simple merging of two kinds of technology of two district's decreasing by gasoline olefin up and down, the structure of reactor also with CN1078094C, CN99109193.0 is identical with CN99105905.0.

At existing stock oil and recycle stock, the slurry oil of making separately in the catalytic cracking technology of reaction, because recycle stock and slurry oil temperature be all more than 300 ℃, the reagent oil ratio can only reach 3～4 level, and reaction effect haves much room for improvement.

In the existing catalyst cracking method, directly contact, limited the raising of reagent oil ratio with reaction raw materials from the high temperature catalyst of revivifier, high temperature catalyst has also caused more side reaction simultaneously, produce unnecessary dry gas and coke, reduced liquid product yield, influence the benefit of device.

Summary of the invention

The object of the invention is to provide a kind of can realize the requirement of two-stage catalytic, can satisfy the catalytic cracking conversion method of hydrocarbon raw material of producing the low-alkene gasoline processing condition again, improves product yield, improves production quality.Utilize the present invention not increase, also need not transform equipment such as existing settling vessel, stripping stage.

For reaching above-mentioned purpose, the present invention adopts following technical scheme: a kind of catalytic cracking conversion method of hydrocarbon raw material, make fresh feed oil, turning oil secondary reaction raw material in riser tube separately, carry out earlier catalytic cracking reaction respectively, merge immediately then, enter the upgrading zone of transformation jointly and carry out product upgradings conversions such as aromizing, isomerization, hydrogen transference.

Reaction process is divided into the catalytic cracking of bottom and the cooling upgrading on top transforms two reactive moieties, and the catalytic cracking of bottom partly is divided into two riser reaction zone arranged side by side, and the upgrading transform portion on top is a shared reaction zone; In the catalytic cracking reaction process of bottom, fresh feed oil is at a riser tube internal reaction, and turning oil (recycle stock, slurry oil) secondary reaction raw material is at another riser tube internal reaction; After finishing the catalytic cracking reaction of requirement, two interior reaction oil gas and catalyzer of riser tube merge immediately, carry out upgrading at a upgrading conversion zone jointly and transform; The catalytic cracking reaction of bottom is high 5～20 ℃ in more conventional catalytic cracking reaction temperature, carry out under the short period of time condition of 0.8～1.5s, and the catalytic reforming zone of transformation on top then carries out reducing than the catalytic cracking zone temperature under 5～25 ℃, the long-time condition of 2.5～5.0s; The stock oil of catalytic cracking reaction part and turning oil are reduced to the catalyzer contact reacts of 610～650 ℃ and 580～650 ℃ respectively with temperature.

For improving the reaction effect of recycle stock, slurry oil, make about 350 ℃ recycle stock, slurry oil be introduced into vapour generator from separation column, release of heat evaporates the water, make recycle stock, slurry oil temperature be reduced to 180～250 ℃ after, enter the turning oil catalytic cracking riser again.The steam that produces is sent into other devices.

From upgrading conversion reaction zone top or upgrading conversion reaction zone half area the used catalyzer of partial reaction is refluxed enter fresh feed oil catalytic cracking riser below fresh feed oil admission port, make cooling catalyst, increase the agent-oil ratio of stock oil catalytic cracking reaction; The quantity of reflux of backflow catalyzer is controlled by guiding valve for 610～650 ℃ according to the temperature that contacts procatalyst with fresh feed oil.

Can also make the used catalyzer of partial reaction be back to upgrading reaction zone bottom from upgrading conversion reaction zone top,, improve the upgrading changing effect to increase the agent-oil ratio and the catalyst inventory of upgrading conversion reaction zone.

Below turning oil catalytic cracking riser regenerated catalyst admission port, be connected in series catalyst cooler, make the cooling catalyst in it, under the effect of pre-lifting medium, by the mode of catalyzer exchange, the catalyzer that makes the turning oil catalytic cracking reaction zone by with catalyst cooler in the catalyzer exchange, mixes the reduction temperature.Catalyst cooler adopts wall heat transfer type heated cooling medium, makes cooling catalyst.

Catalyst cooler can also adopt saturation steam superheated way cooled catalyst.

By establishing steam heating tube, make the temperature of the method reduction upgrading zone of transformation of saturation steam heating in the upgrading conversion reaction zone; Can also adopt at transformation of the way zone of transformation and introduce the cooling medium, direct and reactant blended method cooling, the cooling medium makes water or gasoline.

When the reaction raw materials of turning oil catalytic cracking riser was gasoline, recycle stock, slurry oil entered the fresh feed oil riser, entered after can mixing with fresh feed is oily, also can separately enter.

Gasoline and recycle stock, slurry oil can shared catalytic cracking reaction riser tubes, and fresh feed oil enters another catalytic cracking riser and carries out catalytic cracking reaction.

When not containing gasoline in the secondary reaction material, turning oil and fresh feed oil carry out catalytic cracking reaction in riser tube separately.

The present invention has realized the low contact temperature of catalytic cracking reaction at reactor itself under the prerequisite that is not changing turnover reactor catalyst global cycle amount, the high agent-oil ratio condition does not influence or change the operational condition of other links.

Because the catalytic cracking reaction below reactor partly is arranged to two riser tubes, can realize that stock oil and secondary reaction raw material (as turning oil, freshening gasoline etc.) separately carry out catalytic cracking reaction, shorten the catalytic cracking reaction time, the control respectively and the optimization of realization response condition and reaction raw materials improve transformation efficiency and purpose product yield; Reactor top is provided with the upgrading conversion reaction zone, carries out hydrogen transference and aromizing, isomerization reaction, reduces the olefin(e) centent of gasoline.The present invention had both solved long, the latter half of inefficient problem of conventional riser reactor, had reduced olefin(e) centent in the gasoline again, improved quality product, and contact temperature, the high agent-oil ratio reaction conditions also realized can increase product yield.Because the upgrading zone of transformation is that two the riser tube reaction oil gas in bottom are shared, and equipment is more simplified, and invests lower.

The simple mode of the present invention, instead-shorter riser tube, the catalytic cracking reaction of short reaction time have been realized simultaneously on the device in routine, also realized separately reaction of different material, also realized the requirement of decreasing by gasoline olefin, the catalyzer that has reduced catalytic cracking reaction zone simultaneously contacts temperature, has improved the reagent oil ratio of catalytic cracking zone and upgrading zone of transformation.Can make the agent-oil ratio of turning oil reaction improve 100%, fresh feed oil reagent oil ratio improves 30～50%, and upgrading zone of transformation catalyst inventory increases; Compare with existing similar technology and can improve light oil yield 2%, reduce dry gas yied 30%; Low temperature upgrading zone of transformation can make the content of olefin in gasoline of being produced reduce more than 15 percentage points.The catalytic amount that enters reactor equates with the catalytic amount that leaves reactor, participates in the catalyst for reaction amount and is increased at reactor self; Except that changing riser reactor, do not increase equipment (establishing settling vessel, stripping stage etc. as other), do not change the load and the operation of original device settling vessel, cyclone and stripping stage yet.

Technological process of the present invention is: the regenerated catalyst from revivifier enters fresh feed oil catalytic cracking riser reaction zone bottom through the regeneration standpipe, and the catalyst mix with refluxing from the upgrading zone of transformation forms 610～650 ℃ catalyzer; Regenerator enters turning oil catalytic cracking riser bottom from another regeneration standpipe, and the low temperature catalyst exchange with in the water cooler of below forms 580～650 ℃ catalyzer; These catalyzer (regenerator and backflow catalyzer) under the effect of pre-lifting steam or dry gas, upwards flow together, enter catalytic cracking reaction zone; Fresh feed oil and secondary reaction material enter separately riser tube as recycle stock through separately atomizing nozzle, carry out catalytic cracking reaction under the catalyzer environment; After finishing catalytic cracking reaction, two interior reaction oil gas and catalyzer of riser tube enter shared upgrading conversion reaction zone immediately jointly, this the district in once more with the catalyst mix that above the upgrading district, refluxes, increase catalytic amount, pass through heat transfer type heating steam simultaneously, or directly inject the cooling medium, make 5～25 ℃ of reactant flow coolings, catalytic cracking and heat cracking reaction are suppressed, and the alkene in the gasoline obtains transforming; Reaction oil gas and the catalyzer that enters reactor through the regeneration standpipe flow out the upgrading zone of transformation together, enter settling vessel through the common reactor outlet, after gas solid separation, reaction oil gas is sent into follow-up product separation column through gas pipeline, gasoline, diesel oil, liquefied petroleum gas (LPG) are sent as product, unconverted recycle stock completely enters the recycle stock vapour generator, enters the turning oil catalytic cracking reaction zone of reactor after the cooling again; Then behind stripping, return revivifier regeneration from the isolated catalyzer of reactor outlet, recover active.

Description of drawings

Attached number description.1 is fresh feed oil catalytic cracking riser, 12 fresh feeds oil catalytic cracking reaction zone, 14 regenerated catalysts, 15 pre-medium, 16 stock oils of promoting; 2 turning oil catalytic cracking reaction riser tubes, 22 turning oil catalytic cracking reaction zones, 24 regenerated catalysts, the 25 pre-media that promote, 26A are from the turning oil of separation column, 26 cooled turning oils; 28 catalyst coolers, 23 enter the heat-eliminating medium of water cooler, and 23A flows out the heat-eliminating medium of water cooler, 29 freshening gasoline; 3 vapour generators, 31 softening waters, 31A saturation steam, 31C superheated vapour; 4 upgrading conversion reaction zone, 46 cooling media, the catalyzer of 48 upgrading zone of transformation, 49 enter the steam of the needs heating of upgrading zone of transformation, and 49A leaves the steam after the heating of upgrading zone of transformation; 5 catalytic cracking zone catalyzer return lines, 54 backflow catalyzer; 6 upgrading zone of transformation catalyzer return lines, 64 upgrading zone of transformation backflow catalyzer; 7 reactor outlet pipes; 8 settling vessels, 81 reaction oil gas, 82 reclaimable catalysts; 9 revivifiers.

Fig. 1 to Fig. 5 is the synoptic diagram of the inventive method.

In method shown in Figure 1, turning oil 26 only is recycle stock, carries out catalytic cracking reaction in independent riser tube 1; Upgrading conversion reaction zone 4 usefulness are injected the method cooling of cooling medium 46; It is overheated separately that the steam 31A that recycle stock vapour generator 3 produces sends; Only, make catalyzer 54 return the stock oil catalytic cracking reaction zone, increase stock oil catalytic cracking reaction zone agent-oil ratio above the upgrading conversion reaction zone 4 and between the fresh feed oil catalytic cracking riser 1 catalyzer return line 5 being set.

In method shown in Figure 2, on the basis of Fig. 1 method, increase the catalyzer return line 6 of upgrading zone of transformation, catalyzer 64 is refluxed to the upgrading zone of transformation.

In method shown in Figure 3, on the basis of Fig. 2 method, set up the steam superheating measure in the upgrading conversion reaction zone, make the cooling of upgrading zone of transformation with the way of heating steam.The saturated vapor 31A that steam can use the recycle stock vapour generator to produce is heated into superheated vapour 31C.

Method shown in Figure 4 is that in the catalytic cracking reaction zone, gasoline uses a riser tube separately, recycle stock and the shared riser tube of fresh feed oil.

Method shown in Figure 5, the shared catalytic cracking reaction zone of gasoline and recycle stock, fresh feed oil carries out catalytic cracking reaction zone separately.

Embodiment

After regenerator 14 enters catalytic cracking riser 1 back and is mixed into 610～650 ℃ with the catalyzer 54 that reflux through return line 5, under the effect of pre-lifting medium 15, upwards flow, 200～250 ℃ stock oil 16 contacts with mixed catalyst (14 add 54), the limit coronite upwards flows, and finishes catalytic cracking reaction in the time of 500～540 ℃ temperature, 0.8～1.2s; After regenerator 24 enters turning oil catalytic cracking riser 2, the water cooler 28 that is connected on the below is cooled to 580～650 ℃, under the effect of pre-lifting medium 25, upwards flow, recycle stock 31 about 350 ℃ enters vapour generator, after making near 180～250 ℃ of temperature, enter turning oil catalytic cracking reaction riser tube 2 again, contact, in the time of 500～540 ℃ temperature, 0.8～1.5s, finish catalytic cracking reaction with catalyzer 24; After finishing catalytic cracking reaction, oil gas and catalyzer in two riser tubes enter upgrading zone of transformation 4 immediately jointly, under 490～520 ℃ of conditions, finish upgrading through 2～5s time and transform, last and leave reactor with the catalyzer of

regenerator

14 and 24 equivalent, enter settling vessel 8.For further strengthening the effect in upgrading district, part catalyzer 64 is turned back in the upgrading zone of transformation from top, upgrading district, upgrading zone of transformation catalyst recirculation amount 48 has increased by 64 part at this moment.

Can also can use the way cooling of superheated vapour by injecting 46 coolings of cooling medium in the upgrading conversion reaction zone.

Embodiment.One cover amount of finish 100 * 10 ⁴T/a is to produce the catalytic cracking unit of gasoline and diesel oil.Use method shown in Figure 1.Stock oil 125t/h, 200 ℃ of preheating temperatures, recycle stock 40t/h, 350 ℃ of temperature are cooled to 210 ℃ through vapour generator; Stock oil is in a riser tube, and recycle stock carries out catalytic cracking reaction in another turning oil riser tube; 510 ℃ of stock oil catalytic cracking reaction temperature, 515 ℃ of recycle stock cracking reaction temperature; 630 ℃ of catalyst temperatures in the stock oil riser tube before the reaction, 620 ℃ of the catalyst temperatures in the turning oil riser tube before the reaction, the 1.0s during reaction of stock oil catalytic cracking zone, recycle stock catalytic cracking reaction time 1.2s; 492 ℃ of shared upgrading zone of transformation temperature of reaction, reaction times 3.5s, upgrading zone of transformation water is as the cooling medium.

Oil gas mean flow rate 9.0m/s in the gas phase mean flow rate 10m/s in the stock oil catalytic cracking riser, recycle stock catalytic cracking riser, the gas phase mean flow rate 4.0m/s of upgrading conversion reaction zone.

Only establish a catalytic cracking reaction zone catalyzer return line, used catalyst is introduced stock oil catalytic cracking riser bottom from upgrading zone of transformation top during partial reaction.

Catalyst recirculation amount 14 through the incoming stock oil riser reactor of regeneration standpipe is 900t/h, the catalyst recirculation amount 24 that enters the recycle stock riser reactor through the regeneration standpipe is 300t/h, and the catalytic amount 54 that turns back to the stock oil catalytic cracking riser through return line 5 is 450t/h; The catalytic amount that participates in the stock oil catalytic cracking reaction is 1350t/h, and participating in upgrading zone of transformation catalyst for reaction amount is 1650t/h, and the catalytic amount that enters settling vessel cyclonic separator, stripper and revivifier through reactor outlet still is 1200t/h.Settling vessel 8 working pressure 0.30MPa (a), revivifier 9 working pressure 0.38MPa (a).

Product is respectively: gasoline 42%, and diesel oil 31.0%, liquefied petroleum gas (LPG) 12%, dry gas adds loss 3%, coke 9%, slurry oil 3.0%.Content of olefin in gasoline 30% (v).

Comparative Examples 1.Use the method for CN99109193.0.Different with the present invention is, recycle stock and fresh feed oil carry out catalytic cracking reaction at a common catalytic cracking zone, reaction medium directly with about 690 ℃ regenerated catalyst contact reacts.Compare with Comparative Examples 1, liquid yield has increased by 2.9 percentage points, and gasoline olefin reduces by 3 percentage points, and diesel oil 16 alkane values increase by 4 percentage points.

Comparative Examples 2.Use the method for CN1490383A.Different with the present invention is, reaction medium directly with about 690 ℃ regenerated catalyst contact reacts, the catalytic amount of each reaction zone equals the regeneration dosage that enters through the regeneration standpipe, the recycle stock about 350 ℃ directly enters reactor.Compare with Comparative Examples 2, liquid yield has increased by 1.1 percentage points, and diesel oil 16 alkane values increase by 4 percentage points.

Table 1, embodiment scheme and prior art contrast

Claims

1, a kind of hydrocarbon raw material catalytic cracking reaction method, it is characterized in that, reaction process is divided into the catalytic cracking of bottom and the cooling upgrading on top transforms two reactive moieties, the catalytic cracking of bottom partly is divided into two riser reaction zone arranged side by side, the upgrading transform portion on top is a shared reaction zone, in the catalytic cracking reaction process of bottom, fresh feed oil is at a riser tube internal reaction, recycle stock, the such turning oil secondary reaction raw material of slurry oil is at another riser tube internal reaction, after finishing the catalytic cracking reaction of requirement, two interior reaction oil gas and catalyzer of riser tube merge immediately, carry out aromizing at a upgrading zone of transformation jointly, isomerization, hydrogen transfer reactions realizes that the product upgrading transforms, the catalytic cracking reaction of bottom is high 5～20 ℃ in more conventional catalytic cracking reaction temperature, 0.8 carry out under the short period of time condition of～1.5s, the catalytic reforming zone of transformation on top is then reducing by 5～25 ℃ than the catalytic cracking reaction zone temperature, 2.5 carry out under the long-time condition of～5.0s, the catalyzer contact reacts that the stock oil of catalytic cracking reaction part and temperature are reduced to 610～650 ℃, turning oil and temperature are reduced to 580～650 ℃ catalyzer contact reacts.

2, the method for claim 1, it is characterized in that recycle stock, slurry oil about 350 ℃ are introduced into vapour generator, release of heat evaporates the water, after making recycle stock, slurry oil temperature be reduced to 180～250 ℃, enter the turning oil riser tube again and carry out catalytic cracking reaction.

3, the method for claim 1, it is characterized in that, react used catalyzer from upgrading conversion reaction zone top or upgrading conversion reaction zone half area extension, return in the fresh feed oil catalytic cracking riser from below, fresh feed oil-in through return line, make cooling catalyst, increase the agent-oil ratio of stock oil catalytic cracking reaction; The quantity of reflux of backflow catalyzer is controlled by guiding valve for 610～650 ℃ according to the temperature that contacts procatalyst with fresh feed oil.

4, method as claimed in claim 3, it is characterized in that, make the used catalyzer of partial reaction be back to upgrading conversion reaction zone bottom from upgrading conversion reaction zone top,, improve the upgrading changing effect to increase the agent-oil ratio and the catalyst inventory of upgrading conversion reaction zone.

5, the method for claim 1, it is characterized in that, below turning oil catalytic cracking riser regenerated catalyst admission port, be connected in series catalyst cooler, make the cooling catalyst in it, and under the effect of pre-lifting medium,, make the cooling catalyst of turning oil catalytic cracking reaction zone by the mode of catalyzer exchange, catalyst cooler adopts wall heat transfer type heated cooling medium, makes cooling catalyst.

6, method as claimed in claim 5 is characterized in that, catalyst cooler adopts saturation steam superheated way cooled catalyst.

7, the method for claim 1 is characterized in that, the upgrading conversion reaction zone is provided with steam heating tube, adopts the method cooling that makes the saturation steam heating; Can also adopt at transformation of the way zone of transformation and introduce the cooling medium, direct and reactant blended method cooling, the cooling medium makes water or gasoline.