US2385446A - Catalytic conversion of hydrocarbons - Google Patents

Description

Sept. 25, 1945. J; w. JEwr-:LL ETAL 6 NM ..u ARM Y Sv@ mmHo E #n for f ,N m W52 N R 2% o .6H N I U f Wp A w Y @fm a m Nwnm JG www5 k k@ m 1, v H w w RNNNAQ e .vvo w WQQ E u wb m A um, m ,w hn m m, u, .Q n Qbkmmmw A c @Qukwk .om w v M NN Qwlqs w om uw *xw cumulation of carbonaceous Patented Sept. 25, 1945 CATALYTIC CONVER CAR Joseph man, Mountain Borcherding, New

Application August 6,

6 Claims.

The presentinvention relates to improvements in process and apparatus for effecting Vcatalytic conversions. In its specific aspects, the invention is directed particularly to an improved continuous process of converting'hydrocarbons by treatment over catalytic materials which become spent or deactivated during the conversion by the acmaterial thereon, and which accordingly require periodic regeneration treatment to fit them for reuse in the conversion step. .The catalytic conversion of high boiling hydrocarbons -such as petroleum and the like into low boiling hydrocarbons within the gasoline boiling range is an example of the latter type of conversion reaction of outstanding importance.

It has been proposed, heretofore, to catalytically convert high boiling hydrocarbons such as gas oil to low boiling hydrocarbons within the gasoline boiling range by passing vapors of the high boiling hydrocarbons under suitable reaction conditions in contact with a stationary bed of a cracking catalyst disposed in a catalyst chamber. Pursuant to such processes, after the activity of the catalyst is decreased by reason of the formation of a carbonaceous deposit thereon to an extent where regeneration is necessary or desirable, the activity of the catalyst is restored by stopping the iiow of oil vapor to the chamber and passing an oxygen-containing gas into lthe gas oil` SION OF HYDRO- BONS W. Jewell, Summit, and George D. Creel- Lakes, N. J., York, N. Y., M. W. Kellogg Company, corporation of Delaware and Walter H. asslgnor's to The Jersey City, N. J., a

1941, Serial No. 405,614

(ci. 19e-52) chamber in contact with the spent catalyst, thereby regenerating it in situ by combustion of the carbonaceous deposit. Although such processes are commercially practicable they are subject to a number of inherent limitations and disadvantages which are eliminated by the present invention. Among these are the intermittent nature of the operation, variations in product quality and quantity during the reaction period and difficulty in temperature control, particularly in the regeneration operation. f

A primary object of my invention is the provision of a continuous process of eecting the catalytic conversion of hydrocarbons and analogous reactions, wherein the mentioned disadva'ntagcs of the intermittent type of operation are obviated, and which may readily be controlled and practiced in ment. Various other objects, advantages and features of the invention will be apparent from the following detailed description thereof given in connection `with the appended drawing wherein the tlgure is a diagrammatic illustration of a suitable arrangement of apparatus and process-fiowfor the practice of the invention as aprelatively inexpensive equip-` plied to the catalytic conversion of high boiling hydrocarbons such as petroleum gas oil, or the like, to low boiling hydrocarbons.

The principal units of the apparatus illustrated are: a heater l for supplying vaporized hydrocarbons at a temperature suitable for conversion, a reactor or conversion chamber 2 wherein particles of catalytic cracking material are confeed vapors undergoing cracking, a regeneration vessel or regenerator 3 where' in the particles of used or spent catalytic material are contacted with an oxygen-containing gas under conditions adapted `to cause combustion of the carbonaceous deposit thereon, a. blower 4 or other suitable meansvfor supplying an oxygencontaining gas, such as air, to the regenerator, and gas-solid separating means 5 and 6 associated respectively with the reactor and regenerator for separating suspended particles from the effluent gases derived therefrom.

Pursuant to the present invention, a relatively dense concentrated phase or mass or catalytic particles is formed in the conversion zone regeneration zone, or preferably laterally in contact with the vaporousor gaseouscomponent which travels upwardly through the laterally moving catalyst at a relatively low velocity. The conversion zone and regeneration zone preferably are constituted by horizontally elongated vessels of relatively great length compared to their width and depth, or diameter in the case of cylindrical vessels. Catalytic particles undergoing contact with the vaporous or 'gaseous component are supplied at one end portion of the elongated vessel and withdrawn at the opposite end portion. In the case of the conversion zone, the rate of addition of the fresh or regenerated catalyst particles thereto and the corresponding rate of withdrawal is such as to maintain the laterally moving dense mass at the desired average degree or level of catalytic activity. In the case of the regeneration zone, used or spent catalytic particles are added thereto and withdrawn at such a rate that the catalytic particles will remain in this zone for the period -of time required to eliminate or reduce the carbonaceous deposit to the desired extent. The vaporous or gaseous component is supplied at such a rate that its upward velocity through the conversion and regeneration zone is adapted to maintain the mass of catalyst particles therein a readily flowable but relatively dense state. This condition of the mass of catalyst particles is ysuch that it resembles a liquid in its flow characteristics and the aerated mass of catalyst inthe inboiling hydrocarbon -fraction, is introduced through line 2 to heating coil 3 in furnace I wherein it is vaporized and heated to a temperature suitable for the subsequent conversion operation. From furnace I the feed vapors are passed by transfer line 4 to a suitable vapor distributing means such as manifold 5. lFrom manifold 5' a plurality of branch Valved feed catalyst contained in the system. The latter regulation may be accomplished by either adding catalyst from make up catalyst hopper I8 to the system or by withdrawing a quantity of circulated catalyst to storage as required. The level I3 is preferably maintained a substantial distance below vapor outlets II, most suitably in the lower half of the reactor as indicated, in order to provide an ample catalyst-vapor disengaging space in .the reaction zone above the dense catalyst phase. Under such conditions a relatively small portion of the circulated catalyst is carried out of the reaction zone by the vaporous reaclines 6 connect with the lowerportion of reactor 2. The quantity of feed vapors introduced through each of the branch lines may be suitably independently regulated by the individual valves 8. Lines 6 and lines 21 preferably terminate in suitable distributing means such as a perforated spider or porous plates (not shown) to provide substantial uniform horizontal distribution ofthe vapor throughout the conversion zone.

Particles of a suitable catalytic cracking material, for example an activated clay such as Super Filtrol" in finely divided or powdered condition is supplied at one end portion of reactor 2 through the catalyst inlet conduit 'I. Reactor 2, as shown, consists of a cylindrical vessel of relatively great length, or elongated horizontally relative to its diameter. Fresh catalyst may be supplied through inlet fl, but in normal operation this catalyst will consist largely of previously regenerated hot catalyst withdrawn from regenerator 3 through line 9. From line 9 the regenerated catalyst is picked up by a stream of a. suitable conveying iiuid such as steam injected through line II and conveyed through transfer line It tothe catalyst inlet l. 'I'he quantity of. the conveying fluid employed and the relative cross-sectional area of the transfer line I0 compared to the corresponding area of reactor 2 are such that the catalyst particles drop out of the stream of conveying uid into the reactor. This separation may be facilitated by a baille I2 disposed across the path of the flowing mixture of conveying fluid and catalyst particles introducedthrough inlet l.

Vapors of the hydrocarbons undergoing treatment are admitted through lines t at the base of reactor 2in such quantity that the mass of catalyst particles, the upper level of which is indicated by dotted line I3, is maintained in a readily owable but relatively concentrated or dense condition. In this state the mass of particles assumes a condition resembling that of a liquid in its flow characteristics, and is caused to ow or be positively displaced laterally through the reactor by the addition of active or regenerated catalyst at one end portion of the reaction zone through inlet l and the withdrawal of used or the lower catalyst outlet Id, which rate is controlled by valve I5. Accordingly, level I3 may be maintained at any desired height by suitable control of the rate of withdrawal of catalyst through valve I5 and regulation cf the total amount of tion products withdrawn overhead from the reactor through outlet lines I 'I. Other conditions beln'g fixed, the quantity of solid particles carried out with the vapors through lines II is dependent upon the height of level I 3. For example, if valve I 5 was completely closed level I3 would rise to an extreme limit where solid particles would be carried out through vapor lines I1 at the same rate as added through inlet 'I. Conversely, by progressively increasing the distance between the vapor outlet and the level, the quantity' of solid particles carried out overhead is progressively decreased to a' lower limiting value. Pursuant to the present process, it is greatly preferred to maintain such conditions that only a relatively small quantity of solid particles is carried out.

with the efiiuent gaseous component since the equipment for recovering of' such material from the gaseous component is thereby greatly simplified and reduced in cost.

From outlet lines II vaporous reaction products are passed by manifold Il and line Il to suitable means for recovering the residual quantity of catalyst particles remaining therein and thereafter to suitable recovery means for condensation and separation into the desired products.

From manifold I1 the vaporous reaction products may be passed by line Il to a suitable gassolids separating equipment, such as cyclones or the like, indicated diagrammatically by the numeral 6. From separator 6 thevaporous reaction products are passed by line I9 to a fractionator or similar apparatus of conventional design and hence not illustrated. Separated residual cata- -lyst withdrawn from separator 6 may suitably be returned to the catalyst stripping zone 2d in reactor 2 by catalyst return line 2i.

After passing in contact with the hydrocarbon vapors, the fluid mass of spent catalyst particles is preferably subjected to a stripping operation to remove adsorbed or entrained hydrocarbon vapors therefrom prior to the passageof these particles tothe regeneration stage. 'I'his stripping operation may suitably be eil'ected in a distinct stripping zone 20 within the reactor and defined by the space between the end of the reactor and baille 2|. Vii suitable aerating and stripping medium such as steam is supplied to the lower portion of this stripping zone by line 22 to a steam ring or other suitable distributing means 23 disposed in the lower portion of the stripping zone. The stripping medium is supplied insuch quantities that it passes through unit based upon a Gas oil feed, bbls./day

assigne the base of the reactor through a valvedcatalyst standpipe .25. standpipe 25 is preferably provided with an enlarged portion I4 at the upper end thereof to which an aerating and stripping medium may be introduced through line 26 and distributor 29 for the purpose of maintaining the withdrawn catalyst in a readily flowable condition and also to effect additional stripping action. Additional aerating fluid is preferably introduced at suitably spaced points along the length of standpipe 25 through lines 23 to maintain the catalyst therein in a readily flowable condition.

As illustrative of suitable operating conditions in the practice of the .invention as applied to the catalytic conversion of a petroleum gas oil feed stock to low boiling hydrocarbons within the motor fuel boiling range, there is given inthe following Table A suitable conditions for such a feed capacity of 10,000 bbls./ day of the gas oil feed. The catalyst for this operation consisted of an activated clay known commercially as Super Filtrol in a finely divided or powdered condition, that is, of a iineness suflicient to pass a 100 mesh screen and consisting largely of particles of indiscriminately mixed sizes smaller than 100 microns in average diameter.

Table A steam feed, iba/hr 13,0oo` Reactor dimensions (a) length, ft 50 Reactor dimensions (b) diameter,l ft 12 Feed weight ratio of catalyst to oil Oil feed temperature, F 900 Catalyst feed temperature, "F 980 Outlet temperature catalyst and vapor, F 900 Reactor pressure, lbs/sq. in 7.0 Vapor velocity, ft./sec 0.56 Ratio of weight of oil fed/hr. to wt. of catalyst in reactor (w/hr./w) 3.8 Catalyst time, seconds... 200 Catalyst concentration:

(a) Reactor, 1bs./cu. ft 25 (b) Reactor outlet, grains/cu. ft-- l Horizontal catalyst velocity, ft./sec 0.25

The regeneration operation is preferably eifected in .accordance with the same principles as the conversion stage, except that in the latter case the gaseous component contacted withv the catalytic particlesconsists of an oxygen-containing gas such as air. Also, in the regeneration stage a portion of the regenerated catalyst is preferably recycled to the regeneration zone with intervening coolingof the recycled stream of cata lyst for the purpose of temperature control within the regeneration zone. Optionally, a similar recycle stream of used catalyst may be employed if desired in connection with reactor 2 with intervening heating of this recycled stream of spent catalyst, or cooling, as desired for the purpose of temperature control within the conversion zone or for varying the average degree of catalytic activity of the catalyst mass.

Spent catalyst may be suitably introduced into regenerator 3 by catalyst standpipe 25 leading directly thereto whereby the transfer of catalyst from the reactor to the regenerator is effected entirely by gravity flow. The entering stream of spent catalyst introduced through catalyst inlet 23. An oxygencontaining gas, preferably air, is introduced at the base of the 21 and branch valved lines 21'. Air is supplied through lines 21' in such quantity that the mass of .catalyst particles thereabove is maintained in a freely ilowable this case similar to version zone the mass of relatively dense aerated catalyst resembles a liquid in its flow characteristics and is positively displaced laterally through the regeneration zone by the addition of catalyst. particles at one end portion and the withdrawal of catalyst particles at the opposite end portion.

The height of the catalyst level 28 is controlled in accordance with the same principles of particles meets and is intimately mixed with the stream of cooled recycled catalyst regenerator through manifold suitably be Combined operation described for level i3, so that under preferred conditions a relatively small quantity of catalyst particles is withdrawn overhead with the regeneration gases through regeneration gasl outlets 23. y

A stripping zone 30 is provided at the catalyst outlet end of the regenerator similar to stripping zone 20 for the purpose of stripping oxygen-containing gases from the regenerated catalyst. suitable stripping medium such as steam is supplied to zone 30 through line 3i and distributing means 32. i i

The regenerated catalyst is withdrawn in two separate streams through catalyst standpipes 33 and 34. Standpipes 33 and 34 may each be provided at the upper end portion thereof with an enlarged section 35 and' 36, respectively, similar to I4 and provided with means 31 and 38 for introducing a stripping gas thereto. Standpipes 33 and 34 are further provided with lines 39 and 40, respectively, spaced at suitable points along their length for introducing steam or other aerating medium to maintain the catalyst therein in a freely ilowable condition.

From valve 39' in catalyst standpipe 34 regenerated catalyst is forwarded to the conversion zone through' transfer line I0 as previously described. -From the catalyst standpipe 33, the quantity of regenerated catalyst withdrawn is that required for temperature control Within the regeneration zone 3. Dependent upon the type of catalyst or contact materialemployed there is normally a maximum regeneration temperature which should not be exceeded, for example in the case of a cracking catalyst consisting 0f an activated clay of the Super-Filtrol type this temperature is normally 1150 F.

Recycled catalyst is fed by valve 40 from catalyst standpipe 33 into a stream of a conveying fluid, suitably air derived fromv compressor 4, through' line 4I and passed by line 42 through a heat exchanger 43 through which a cooling medium is circulated by lines 44 and 45. In exchanger 43 the stream ofv recycled catalyst is cooled to a. temperature adapted to provide the desired temperature control during the regeneration operation. A baille 43 may be provided at the outlet of catalyst inlet 26 to subserve the same purpose as baille i2..

Gaseous combustion products are'withdrawn overhead from regenerator 3 through outlets 23 and are passed to a suitable gas-solids separating system to separate catalyst particles suspended therein. The quantity of catalyst carried overhead, as in the case of the reaction zone, is preferably maintained at a relative low amount thereby greatly simplifying the recovery system necessary for the separation of this material from the gas component. The stripping medium and stripped gases existing from zone 30 may with the eiiluent gas' from but relatively dense state. In.

that prevailing in the contaken as about 1100 to'` outlets 29 by line Il. TI 1e emuent regeneration gas may be passed through a cooler or heat exchanger 48 prior to passage to the gas-solids separating system, although this cooling step may optionally be omitted. From heat exchanger I8 the gas mixture passes by line 49 to a suitable gas-solids separator 5 such as a Cottrell precipitator, a cyclone separator, or the like, wherein the small quantity of suspended solids may be suitably separated. In separator 5, the ue gas is withdrawn overhead through line 50 and the separated solids are withdrawn at the bottom through hopper 5i. e Any required amount of make up catalyst may be supplied to hopper 5l from fresh catalyst hopper IS. From hopper Si the recovered catalyst is returned by catalyst -standpipe 52 to the regenerator by transfer line 53 to which a suitable conveying fluid such as steam is supplied by line 50.

Operating conditions suitably maintained in the regeneration stage of th'e process are illustrated by the conditions tabulated in the appended Table B for a regeneration operation corresponding tothe conversion operation given in Tabled.

Table B' Spent catalyst, lbs./hr 632,840 Cooled recycled catalyst, lbs/hr 900,000

Ratio by weight recycledto spent catalyst 1.43 Inlet temperature, spent catalyst, F Y 900 Inlet temperature, recycled catalyst, F 700 Outlet temperature of catalyst and gas,

F 1,000 Regenerator dimensions:

(a) Length, ft 72 (b) Diameter, ft 20 Regenerator gas velocity, ft./sec 0.5 Air feed, lbs/hr 91,000 Catalyst concentration:

(a) Regenerator, lbs/cu. it 23 (b) Outlet gas, grains/cu. ft 20l Wt. percent of coke produced based on oil feed 5.0 Coke percent by wt on spent catalyst-- 1.3 Carbon percent by wt. on regenerated catalyst 0.7 Catalyst contact time, seconds 615 Pressure in regenerator, lbs/sq. in 7 Horizontal catalyst velocity, ft./sec 0.12

Certain variable operating conditionsin the practice of the process may follow and be controlled pursuant to conventional practice in the art with respect to the particular conversion or treating reaction involved. For example in the application ofthe process to the vapor phase catalytic cracking of high boiling hydrocarbons to low boiling hydrocarbons within the motor fuel boiling range, such factors as the selection of suitable charging stock, catalytic material, conversion temperatures, pressures, and the like, may be determined in accordance with conventional practice in this particular art.

The rate of fresh catalyst feed is dependent upon the desired average catalytic activity of the regeneration zone.

of catalyst in the reactor by the catalyst feed rate per minute.

The weight of catalyst in the reactor is dependent upon the concentration of the dense phase and the height of the upper level of this phase. In the application of the process to the catalytic cracking of high boiling hydrocarbons it is preferred to maintain the ratio of the weight of oil fed per hour to the weight of catalyst inthe reaction zone (w/hr./w) within the range of about 1.0 to 25.0 and preferably within the more restricted range of about 2.5 to 10.0. Also, in this case it is preferred to utilize a catalyst to oil feed rate ratio within the range of 0.5:1 to 20:1 and preferably within the more restricted range of 2:1 to 8: 1.

The yvelocity of the gaseous component preferably maintained in the practice of the process is dependent upon the character of the catalytic particles employed with respect to such factors as their individual size, shape and density. The gaseous component should be maintained at a velocity of sulcient magnitude to aerate the mass of catalyst particles to an extent suillcient to maintain them in a readily owable condition. Further, the maximum velocity must not be in excess of that velocity below which a relatively dense or concentrated phase of the catalyst particles is produced in the solids-vapor contact zone. At relatively high vertical gas velocities the cata# lyst particles may be suspended in the stream of gas and carried along therewith at a velocity approaching that of the gas particles. At relatively low vertical gas velocities the eiect of the phenomenon known as slip" becomes pronounced and in the zone of such low velocities the solid catalytic particles accumulate, thereby producing a relatively dense or concentrated phase. In the practice of the present process lateral internal recycle is avoided. The avoidance of such recycling is provided by the horizontally elongated conguration of the conversion and regeneration zones, and the relative thinness of the bed of catalyst compared to its length. Under these conditions, it is apparent that the carbonaceous content of the lateralLv moving bed is progressively increased inthe direction of flow in the conver sion zone, and that the converse is true in the Accordingly, the quantities of the gaseous component admitted through each of the valved lines 6 and 2l may be adjusted with respect to the carbon concentration of the catalyst above the individual gas inlets.

Since reactor 2 and regenerator 3 are of unir form diameter the average lateral velocity of the particles therethrough will be substantially uniform. This velocitymay be varied to advantage in certain instances by modifying the cross-sectional area in various parts of the reaction vessel, forexample, by gradually increasing this area in the direction of lateral ilow the velocity of the catalyst particles will be progressively lower in the direction of flow. Likewise the thickness of the catalyst bed may be varied in diierent parts of the reaction zone by suitably contouring-the bottom of the reaction vessel. This same effect may also be -produced by inclining the reaction vessel whereby the bed' will be so disposed that it gradually increases or decreases in thickness in the direction of flow dependent upon whether the inlet end of the reaction vessel is made higher or lower than the outlet end.

' Any of the various known types of crackingv silica-alumina. or silica-magnesio. type adapted to oxygen-containing gas at the bottom of said reproduce a satisfactory yield of high octane gasoseneration zone and flowing the sas upwardly line. Either silica-alumina catalyst consisting of therethrough in contact with .the mass 'of said activated clay prepared by the acid treatment of laterally flowing catalytic particles under condinaml clays for example the commercial prod- 5 tions to cause Combustion 0f the car- .uct SupebFlltreln er a synthetloally prepared bonaceous deposit and at a velocity adapted to rate, vapor velocity and amount of catalyst pressllleeqelumlna catalyst such as those dlsolosod maintain said mass in an aerated readily flowable in copendinz applications of Robert Ruthrun', but dense state, withdrawing the gaseous regenserlel Nes. 305,472 and 305,473, both md Novem.. eration products overhead from said regeneraber 2l, 1939' may be employed. The catalyst, ls lo tion zone. withdrawing the regenerated particles preferably-employed in ilnely divided or pow- 'of catalyst from said regeneration zone in a ered condition, for exemple Wlth particles rang, stream separate from the gaseous regeneration me mm about 1 to loo mlerons However, eranproducts, and re-introducing said regenerated ular catalyst articles may be employed, and in Catalyst in to Said Cracking Zonel thisinstance al.J mixture of granular and powdered 2- In a Process for the caoalytlc oraokm 0f eetelyue material lspreferred. hydrocarbons wherein particles of a' catalytic From the aiicve description of the process it moons manif-1&1 are Conlmuously Passed wm be apparent that it fully accomplishes the prl through a. cracxing zone 1n contact with the vamary object of the invention, namely the provipors undergoing crackmg. thereby accumulating sion of a continuous process which eliminates the a. deactivating deposit of carbonaceous material various defects of an intermittent operation and thereon' one motnoo of rogonerat'mg the Spent' which may be readily and eeetlvely controlled catalyst for reuse 1n said cracking process, which 1 xpensive e Matus. comprises introducing the particles of spent catanecgggwfya; process ispthat it -lytic cracking material into a regeneration zone,.

flowing the particles laterally through said zone, introducing an oxygen-containing gas at the botent in the conversion and regeneration zones. A tom of said regeneration Zone and nowng the gas upwardly therethrough in contact with the mass mo; 'ga xgaggyldstu 'of said laterally ilowingv catalytic particles under ui mene Powder conditions adapted'to cause combustion of the gssoesfmnissggoxlgrelivsly 10W and the 3o carbonaceous deposit and at avelocity adapted to maintain said mass in an aerated readily flowable process Permits the satisfactory use of relatively but dense state withdrawing the gaseous regen- Snnple and inexpensive gos'sonos recovery equip' eration products overhead from said regeneration ment. i h

While the method has been described particucfmhlgstwlgmwmg t' e regenerated particles m 'd r t` larly in connection with the catalytic conversion sa egenera um Zone m o o! high` boiling hydrocarbons to low boiling reduets hydr b 'thi th asoline boiling range p i om. ons W1 n o g d 3. A continuous cyclic process of catalytically for which purpose 'the method 1s especlo'uy-a lconverting high boiling hydrocarbons into low vantageols t Wm be apparent to those S-knleo 40 boiling hydrocarbons within thc motor fuel bcnallows independent adjustment of catalyst feed 25 stream separate from the gaseous regeneration in the art that one moohoo may be' oppnod to ing range which comprises introducing particles` Other types 0f catalytic hyofocorbon confefon or an active catalytic cracking material into one reactions Soon oo the Catal-loc reformmg of end portion of a cracking zone, introducing vanaphth fractions oder oonoltloos suon as oo' pors of the hydrocarbons undergoing conversion scribed in Belchetz application Serial No, 348,605, at the bottom of seid Zone and owiog the vapors and to chemical reactions ono treating opera' upwardly therethrough in contact with the mass nous gonornny involving the Step of contacting of catalytic particles thus introduced at a velocity vapors with powdered or commimlted S01d5 adapted to maintain said mass ln a condition These and various other modifications in the ilapproximating e llquld ln its flow characteristics lusn'ativo embodiments of tno invention do 50 withdrawing the vaporous cracked products overoneo in one foregoing Win oo apparent to those head rfrom said reaction zone withdrawin s nt skilled in the art, and the scope of die invention catalytic particles from sai g pe d reaction zone at an is accordingly not to be restricted except as ree d ortl osi th in quired by the claims appended hereto. n p on opp be e po t of mtroductmn and in a stream separate from said vaporous e We claim! V reaction products, introducing the particles of 1. A Continuous o yolo ProoeSS 0f oatglytoauy spent catalytic material into a regeneration zone, converting high b011m$ hydrocarbons milo 19W owing the particles laterally through said zone, boiling hydrocarbons Within the motor: fuel bollintroducing en oxygen-containing gas at the boting range, which comprises introducing particles tom of said regeneration zone and flowing the or an active catalytic cracking motoriol into a co gas upwardly therethrough inl contact with the cracking zone, flowmg the Partloles laterally mass of said laterally flowing catalytic particles through said zone. I Iitrodllcmg vapors of the hyunder conditions adapted to cause combustion of drocarbons undergolng oonVeISlon of the bottom the carbonaceous deposit and at a velocity adaptof said Zone and flowing the vapors upwardly ed to maintain said mass in a condition approxitherethrough 111 contact Wlh the moss Of vSald- 05 mating a liquid in its flow characteristics, withlaterally flowing oatalyti Particles al'- 8' Velocity drawing the gaseous regeneration products overadapted to maintain said mass in an aerated,V lhead from said regeneration zone, withdrawing readily ilowable but relatively dense state, wlththe regenerated particles of catalyst from said `drawing the vaporouS cracked Drofllots overhead regeneration zone at an end portion opposite the from said reaction zone, withdrawing spent catapoint of introduction and in a stream separate lytic partidos from Said reaction Zone in a Stream from the gaseous regeneration products, and reseparate from said vaporous reaction products, introducingsaid regenerated catalyst into said mtg-inging the particles of spent catalytic macracking zone. l

terlal into a regeneration zone, nowing the par- 4. In a process for the treatment of hydrocartlcles laterally through said zone, introducing an 'u bon vapors with solid contact agents wherein Particles ofthe solid contact agent are continuously passed through a treating zone in contact with the vapors undergoing treatment, thereby accumulating a deactivatlng deposit of carbonaceous material thereon, the method of regenerating the particles under conditions adapted to cause combustion of the carbonaceous deposit and at a velocity adapted to maintain said mass in a readily iiowable but dense condition approximating a liquid in its iiow characteristics, withdrawing thegaseous regeneration products overhead from said regeneration zone, and withdrawing the regenerated particles of contact agent from said regeneration zone in a stream separate from the gaseous regeneration products whereby said mass is caused to flow laterally through the regeneration zone.

5. A continuous cyclic process of treating hydrocarbon vapors with solid contact agents wherein the contact agent accumulates a combustible deactivating deposit incident to such treatment, which comprises introducing particles of an active contact material into a treating zone, flowing the particles laterally through said zone, introducing vapors of the hydrocarbons undergoing treatment at the bottom of said zone and iowing the vapors upwa` .ily therethrough in contact with the mass of said laterally flowing particles at a velocity adapted to maintain said mass in a readily owable but relatively dense state, withdrawing the vaporous treated products overhead from said treating zone, withdrawing deactivated particles from said treating zone in a stream separate from said Vaporous'treated products, introducing the particles oi deactivated material into a 'regeneration zone, iiowing the particles laterally through said zone, introducing an oxygen-containing gas at the bottom of said regeneration zone and ilowing the gas upwardly therethrough in contact with the mass of said laterally flowing particles under conditions adapted to cause combustion of the deactivating deposit thereon and at a velocity adapted to maintain said mass in a readily iiowable but relatively dense state, withdrawing the gaseous regeneration products overhead from said regeneration zone, withdrawing the regenerated particles oi' contact material from said regeneration zone in a stream separate from the gaseous regeneration products. and re-introducing said particles regenerated into said treating zone.

6. A continuous cyclic process of treating vapors with solid contact agents wherein the contact agen-t accumulates a combustible deactivating deposit incident to such treatment, which comprises introducing particles of an active contact material into a treating zone, flowing the particles laterally through said zone, introducing the vapors undergoing treatment at the bottom of said zone and flowing the vapors upwardly therethrough in contact with the mass of said laterally owing particles at a velocity adapted to maintain said mass in a readily iowable hut relatively dense state, withdrawing the vapor-ous treated products overhead from said treating zone, withdrawing deactivated particles from said treating zone in a stream separate from said va porous treated products, introducing the pary ticles of deactivated material into a regenera-` tion zone, iiowing the particles laterally through said zone, introducing an oxygen-containing gas at the bottom of said regeneration zone and flowing the gas upwardly therethrough in contact with the mass of said laterally flowing particles under conditions adapted to cause combustion of the deactivating deposit thereon and at a velocity adapted to maintain said mass in a readily owable but relatively dense state, withdrawing the gaseous regeneration products overhead from said regeneration zone, withdrawing the regenerated particles of contact material from said regeneration zone in a stream separate from the gaseous regeneration products, and re-introducing said particles regenerated into said treata ing Zone.

JOSEPH W. JEWELL. GEORGE D. CREELAEAN. WALTER H. BORCHERDING.

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