US2423813A - Apparatus for handling contact masses - Google Patents
Apparatus for handling contact masses Download PDFInfo
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- US2423813A US2423813A US483120A US48312043A US2423813A US 2423813 A US2423813 A US 2423813A US 483120 A US483120 A US 483120A US 48312043 A US48312043 A US 48312043A US 2423813 A US2423813 A US 2423813A
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- contact mass
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- gas
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- 239000002245 particle Substances 0.000 description 33
- 239000000463 material Substances 0.000 description 32
- 238000004140 cleaning Methods 0.000 description 26
- 239000007789 gas Substances 0.000 description 26
- 229930195733 hydrocarbon Natural products 0.000 description 13
- 150000002430 hydrocarbons Chemical class 0.000 description 13
- 239000007787 solid Substances 0.000 description 10
- 239000004215 Carbon black (E152) Substances 0.000 description 9
- 238000006243 chemical reaction Methods 0.000 description 9
- 239000003546 flue gas Substances 0.000 description 8
- 230000008929 regeneration Effects 0.000 description 8
- 238000011069 regeneration method Methods 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- 230000001172 regenerating effect Effects 0.000 description 6
- 239000012530 fluid Substances 0.000 description 5
- 239000000376 reactant Substances 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 3
- 230000001174 ascending effect Effects 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 239000004927 clay Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 238000012216 screening Methods 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 210000001217 buttock Anatomy 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000011362 coarse particle Substances 0.000 description 1
- 239000011246 composite particle Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 229910000286 fullers earth Inorganic materials 0.000 description 1
- 239000000499 gel Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000012492 regenerant Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
Images
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
Definitions
- the contact masses were composed ol? ⁇ particle form clay type materials utilized as beds-in-place alternately subjected to reaction and to a combustion regeneration ⁇ for the purpose of removing carbonaceous deposits placed peilets or granules of about 30 mesh per inch size or larger, there is a certain production of fines, as by attrition, etc.
- the contact of reagent and contact mass, or of regeneration agent and contact mass is achieved by flowing the iluid reagents or regenerant through the interstiees in the moving bed of contact mass. Fines of contact mass material give rise to trouble when present in excess amounts.
- This invention has for its object the removal of ilnes of contact mass'material from processes wherein a particle-form solid contact mass material having appreciable particle sizes, say above about 30 mesh, is cyclically moved through a re'- When the contact Amass particles are of appreciable size such as yical difficulties because of high temperatures.
- Figure 1 serves to show, dlagrammatically. the surroundings in which the invention is practised.
- Figure 2 shows in diagram form a vertical section of apparatus appropriate for its practise,
- Figure 3 shows 4a plan view of theapparatus of Figure 2
- Figures 4 and 5 show a detail therein
- Figures 6 and 7 show an optional form for that detail.
- item I0 is a reactor through which a stream of contact mass particles passes in a downward direction to be contacted with hydro-v carbon reactants introduced by pipe II and removed by pipe I2.
- Spent contact mass material passes from the reactor through duct I3 and is lelevated by elevator I4 to pass through duct I5 into the upper end of a regenerating kiln I6.
- this re'generatingixn I6 regeneration medium In this re'generatingixn I6 regeneration medium,
- ⁇ usually air, is i'ed by pipe Il through orifices I8 y lected into each of two ducts 20 and pass up-b wardly.
- kiln I6 there is a fines cleaning device composed substantially of a vertical member 2i, which is described later in more detail.
- action zone where hydrocarbon reaction is conducted, thence through a regenerating zone, and i then returned to reaction.
- Separation of ilne particles from coarse particles oi' solid may be conducted in several different ways, as by screening, use of centrifugal force, electrical precipitations, or elutriation.
- any screening method is open to many mechan- By' means of ducts 22 and dampers 23, a portion of the ilue gas is forced to ilow into cleaning column 2i, the remainder passing upwardly to enter a final separator 24 by means of ducts 2l.
- pass through ducts 26 into ducts 20 to similarly enter separator 24. These flue gases from 2i contain the fines cleaned from the contact mass material.
- All nes separatedin 24 are discharged from the system through pipe 21, clean ilus gases being discharged to atmosphere through pipe 2B.
- the regenerated contact mass material flowing from the bottom of kiln I8 through duct 28 is elevated by elevator 30 and discharged through 3 duct 3
- a portion of this regenerated material is conducted by duct 34 to cleaning column 2
- the portion selected for cleaning may be taken either from the regenterial flowing through duct lli. In general.
- FIG 2 We have a detail showing the top of the regenerator kiln IB into which contact mass material has been fed by duct II and from which there extends upwardly the cleaning column 2
- a portion of the contact mass material is fed through duct 34 to the top of 2
- duct 34 termi.. nates in a feed pipe 36 below which there is positioned a distributing cone 31 so that the contact mass particles are distributed uniformly in a shower in the interior of cleaning column 2
- Flue gas from kiln I6 is introduced into cleaning column 2
- i6 is the regenerator
- I5 the feed duct therefor
- is the cleaning column
- 34 is the pipe feeding solids thereto.
- 35 the valve in that feed pipe, 4
- distributor cone 31 which, by experiment, has been found to be preferably a cone having .45 sides and a base diameter about one-third the diameter of the cleaning column 2
- the method of cleaning is by conducting a falling shower of contact ⁇ mass particles including fines with an upwardly ascending column of gases of predetermined velocity sufficient to sweep from that column of particles all particles finer than a certain predetermined size.
- the first is that of gas velocity in the This is so adjusted as to be maintained slightly above the "terminal velocity for the largest particle to be eliminated. Terminal velocity may be dened as that velocity of gas which will prevent the falling of a selected particle.
- V acosta-2- g
- V terminai velocity in cm./sec.
- a reaction zone means to introduce particle form solid contact mass material thereto and means to remove it therefrom, means to introduce hydrocarbon reactants thereto and means t0 remove hydrocarbon reaction products therefrom, a regeneration zone, means to introduce contact mass material thereto and means to remove it therefrom, means tointroduce fluid regenerating medium thereto and means to remove it therefrom, meansto transfer spent contact mass from the reactor to the regenerator,
- scrubbing means for said diverted contact mass comprising a vertical passage, means to introduce diverted contact mass to'said passage to pass 'downwardly therethrough as a showen'means to flow a gas upwardlyv through said passage at controlled velocity sufllcient to .remove finer particles of contact mass from said shower, separate exit means from said passage for fines-laden gas and' 4means tov introduce hydrocarbon reactants thereto and means to remove hydrocarbon reaction products therefrom, a regeneration zone, means to introduce contact mass material thereto and means to remove.
- means to introduce fluid regenerating medium thereto and means to remove it therefrom means to transfer spent contact mass 'from the reactor to the regenerator, means to transfer regenerated con tact mass from the regenerator to the reactor, means for cleaning less than all of the moving stream of contact mass from fines comprising a confined vertical passage, means to admit a controlled portion of the moving stream of contact mass thereto from a point between the reactor and the regenerator, means to distribute the con tact mass so admitted into a shower falling substantially uniformly through all of the horizontal f 6 cross section of such passage.
- a reaction'zone means to inv troduce particle form solid contact mass material thereto and means to remove it therefrom, means to introduce hydrocarbon reactants thereto and 6means to remove hydrocarbon reaction productsv therefrom, a regeneration zone, means to introduce contact mass material thereto and means to a0 remove it therefrom, means to introduce iluid regenerating medium thereto and means to remove it therefrom, means to transfer spent contact mass from the reactor to the regenerator, means to transfer regenerated contact mass from the lregenerator to the reactor, means todivert a portion of the moving stream of contact mass at a point between the regenerator and the reactor, scrubbing means for said diverted contact mass comprising a vertical passage, means to introduce. diverted contact mass to said passage to pass downwardly therethrough as a shower, means to flow a gas upwardly through said passage at controlled velocity sufficient to remove finer particles of contact mass from said shower,
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Description
July 8, 1947 c. H. LECIHTHALER Erm. 2,423,813,l
y APPARATUS FOR HANDLING CONTACT MASSES Filed April 15, 1943 3 sheets-sheet 2 J4 if? ,I
. 4 d'5 DusTJ'EpARATo/z "y Zossen 15 lNvENroR Jl July 8 1947- c. H. LECHTHALER E TAL 2,423,813
A PPARATUS FORfHANDLING CONTACT MASSES Filed April 15, 1943 v s' Sheets-sheet s C'f/mu fa/Music 20.1.1: LL. EL
lNvENroR 5 Patented July 8, 1947 2,423,813 APPARATUS FOR HANDLING CONTACT l MASSES Charles H. Lechthaler, Woodbury, and Russell Lee, Mantua, N. J., assignors to Socony-Vacuum New York Oil Company, Incorporated,l a corporation of Application April 15, 1943,` Serial No. 483,120
s '4 claims. (ci. zs-zss) y In the catalytic treatment of hydrocarbons, for such purposes as cracking high boiling hydrocarbons to gasollnes, and for similar purposes, recently developed processes have made use of catalytic contact masses comprising formed particles or granules of alumina-silica complexes, and similar materials, such as fullers earth, Filtrol, and other natural clays, including altered and activated natural clays, synthetic composite particles arising from gels, and the like. These solid adsorptive catalytic materials are spoken oi' broadly under the term clay type contact mass materials.
In the flrst commercialization of catalytic cracking, the contact masses were composed ol?` particle form clay type materials utilized as beds-in-place alternately subjected to reaction and to a combustion regeneration `for the purpose of removing carbonaceous deposits placed peilets or granules of about 30 mesh per inch size or larger, there is a certain production of fines, as by attrition, etc. With such processes employing particles of appreciable size, the contact of reagent and contact mass, or of regeneration agent and contact mass is achieved by flowing the iluid reagents or regenerant through the interstiees in the moving bed of contact mass. Fines of contact mass material give rise to trouble when present in excess amounts.
This invention has for its object the removal of ilnes of contact mass'material from processes wherein a particle-form solid contact mass material having appreciable particle sizes, say above about 30 mesh, is cyclically moved through a re'- When the contact Amass particles are of appreciable size such as yical difficulties because of high temperatures.
tremely small particles when Present in small' concentration, is not applicable to what is really a problem of size separation. 'I'his invention has applied, in a specific manner, the process of elutriation, that is, contact of a particle stream with countercurrently ilowing gases at rates designed to remove all particles smaller than a desired size.
In order to conveniently understand the invention, reference is now made to the drawings attached hereto. In these drawings, Figure 1 serves to show, dlagrammatically. the surroundings in which the invention is practised. Figure 2 shows in diagram form a vertical section of apparatus appropriate for its practise, Figure 3 shows 4a plan view of theapparatus of Figure 2, Figures 4 and 5 show a detail therein, and Figures 6 and 7 show an optional form for that detail.
In Figure 1, item I0 is a reactor through which a stream of contact mass particles passes in a downward direction to be contacted with hydro-v carbon reactants introduced by pipe II and removed by pipe I2. Spent contact mass material passes from the reactor through duct I3 and is lelevated by elevator I4 to pass through duct I5 into the upper end of a regenerating kiln I6. In this re'generatingixn I6 regeneration medium,
^ usually air, is i'ed by pipe Il through orifices I8 y lected into each of two ducts 20 and pass up-b wardly. Above kiln I6 there is a fines cleaning device composed substantially of a vertical member 2i, which is described later in more detail.
action zone where hydrocarbon reaction is conducted, thence through a regenerating zone, and i then returned to reaction.
Separation of ilne particles from coarse particles oi' solid may be conducted in several different ways, as by screening, use of centrifugal force, electrical precipitations, or elutriation. In the surroundings spoken of the application of any screening method is open to many mechan- By' means of ducts 22 and dampers 23, a portion of the ilue gas is forced to ilow into cleaning column 2i, the remainder passing upwardly to enter a final separator 24 by means of ducts 2l. Flue gases from cleaning column 2| pass through ducts 26 into ducts 20 to similarly enter separator 24. These flue gases from 2i contain the fines cleaned from the contact mass material. All nes separatedin 24 are discharged from the system through pipe 21, clean ilus gases being discharged to atmosphere through pipe 2B. The regenerated contact mass material flowing from the bottom of kiln I8 through duct 28 is elevated by elevator 30 and discharged through 3 duct 3| linto a storage hopper 32 from whence it iiows by duct 33 into reactor I0. A portion of this regenerated material is conducted by duct 34 to cleaning column 2|. The portion selected for cleaning may be taken either from the regenterial flowing through duct lli. In general. it is preferred to work with regenerated material for various reasons, such as for example, it is easier to handle in cleaning, and this choice is usually reenforced by not having to build the spent catalyst elevator I4 sufficiently great in height to give access to the top of cleaning column 2 I.
Turning now to Figure 2, We have a detail showing the top of the regenerator kiln IB into which contact mass material has been fed by duct II and from which there extends upwardly the cleaning column 2|. A portion of the contact mass material is fed through duct 34 to the top of 2|, the amount so fed being controlled by a sliding orifice plate or other appropriate type of valve 35. Inwardly of column 2|, duct 34 termi.. nates in a feed pipe 36 below which there is positioned a distributing cone 31 so that the contact mass particles are distributed uniformly in a shower in the interior of cleaning column 2|. Cleaned material from the bottom of 2| passes through pipe 38 into the interior of kiln-I6. this pipe terminating in a cone 39 at a point below the level of contact mass material in the kiln as designated by line 40. Flue gas from kiln I6 is introduced into cleaning column 2| by means oi' ducts 22 which lead into a pressure chamber 4| surrounding the cleaning column near its bot- Y tom, the Wall of the column being perforated by orifices 42 so that a uniform and proper distribu- .tion of gas into the cleaning column 2| may be erated material, as shown, or from the spent ma- Figure 3 is a plan view of the apparatus shown i in Figure 2, serving merely to indicate its general arrangement. In this figure, i6 is the regenerator, I5 the feed duct therefor, 2| is the cleaning column, 34 is the pipe feeding solids thereto. 35 the valve in that feed pipe, 4| the inlet gas pressure chamber, 22 and 22 the inlet gas feed ducts, 2B and 26 the outlet gas ducts, 24 the separator, 25 and 25 ducts leading flue gas thereinto and 28 the stack of the separator.
In Figures 4 and 5, which/should be read together, we find a detail of the arrangements for f introducing contact mass material in a uniform manner to the cleaning column 2|. In the column 2| the feed pipe 36 is centrally located extending therein to a depth indicated by line A,
suiiicient to permit a reasonable collection space for discharged gases above the point of contact mass introduction. Just below the end of pipe 36 there is mounted distributor cone 31 which, by experiment, has been found to be preferably a cone having .45 sides and a base diameter about one-third the diameter of the cleaning column 2|, so mounted that its apex is practically at the level A. (The slope of the cone will depend some-v what upon the nature of the solid material being handled.) Additionally, this cone is provided with certain orifices 43, the number and size of these orifices being so selected that a portion of the contact mass material flowing over the surface of the cone is discharged therethrough to provide about the same mass velocity ofcon- Aupwardly ascending stream of gas.
1 36. that pipe is divided into several pipes 44. each with its own cone 45, these pipes and cones being so arranged as to secure a substantially uniform distribution over the entire area of cleaning column 2|.
In this cleaning column, the method of cleaning is by conducting a falling shower of contact `mass particles including fines with an upwardly ascending column of gases of predetermined velocity sufficient to sweep from that column of particles all particles finer than a certain predetermined size.
In application to the present operation in which this method of cleaning is applied, wherein we are circulating a stream of contact mass particles continuously through two zones, in one of which they are contaminated by reaction and in the other of which they are regenerated by combustion, we segregate a relatively quite small portion of the circulating stream of contact mass material, scrub it with a portion of the flue gases from regeneration, return the scrubbed 'stream of contact mass material to cycle and discharge the flue gases, after separating and discarding iines therefrom, to the atmosphere.
There are two fundamental controls for this operation. The first is that of gas velocity in the This is so adjusted as to be maintained slightly above the "terminal velocity for the largest particle to be eliminated. Terminal velocity may be dened as that velocity of gas which will prevent the falling of a selected particle.
For catalyst particles ranging in size from 14 to mesh (Tyler scale) in flue gas at 800-l100 F. and atmospheric pressure, terminal velocity is expressed by the Allen-Glazebrook equation as:
V: acosta-2- g Where: V=terminai velocity in cm./sec.,
( :the critical radius of the particle above which Stokes Law is not obeyed, 9 v2 l a =radius of the particle in cm.,
v =kinematc viscosity ofl the fluid, in Stokes,
Reduced to concrete terms in an example, to remove particles of 35 mesh and finer having a specific gravity of 1.45, when the fluid supporting medium is flue gas at 900 F. and atmospheric pressure, the velocity should be 8.2 feet per second. With this velocity, the separated catalyst nes will be found to be of all sizes up to and includirig 35 mesh, the bulk of them being below y circulating may be increased or decreased by in-4 creasing or decreasing the proportion subjected to cleaning. Greatest efficiencies of removal are obtained when the amount of material subjected to cleaning does not exceed 1 ton/hr. per sq. ft. of cleaning column cross sectional area. The actual amount so subjected is found to be quite small. For example, in a unit circulating 100 tons per hour, only 5 tons per hour need be subjected to cleaning in order to have the whole substantially free of lines, when the contact mass particles have the resistance to attrition ordinarily characteristic of pelletted clays. This figure will vary, of course, with the resistance of the contact mass to attrition, since less resistant particles will give rise to more fines and will require that a greater proportion be subjected to cleaning to secure equal freedom from lne particles.
We claim:
l. In a system for the conversion of hydrocarbons in the presence of a particle form solid contact mass material a reaction zone, means to introduce particle form solid contact mass material thereto and means to remove it therefrom, means to introduce hydrocarbon reactants thereto and means t0 remove hydrocarbon reaction products therefrom, a regeneration zone, means to introduce contact mass material thereto and means to remove it therefrom, means tointroduce fluid regenerating medium thereto and means to remove it therefrom, meansto transfer spent contact mass from the reactor to the regenerator,
means to transfer regenerated contact mass from the regenerator to the reactor, means to divert a portion of the moving stream of contact mass at a point between the regenerator and the reactor,
scrubbing means for said diverted contact mass comprising a vertical passage, means to introduce diverted contact mass to'said passage to pass 'downwardly therethrough as a showen'means to flow a gas upwardlyv through said passage at controlled velocity sufllcient to .remove finer particles of contact mass from said shower, separate exit means from said passage for fines-laden gas and' 4means tov introduce hydrocarbon reactants thereto and means to remove hydrocarbon reaction products therefrom, a regeneration zone, means to introduce contact mass material thereto and means to remove. it therefrom, means to introduce fluid regenerating medium thereto and means to remove it therefrom, means to transfer spent contact mass 'from the reactor to the regenerator, means to transfer regenerated con tact mass from the regenerator to the reactor, means for cleaning less than all of the moving stream of contact mass from fines comprising a confined vertical passage, means to admit a controlled portion of the moving stream of contact mass thereto from a point between the reactor and the regenerator, means to distribute the con tact mass so admitted into a shower falling substantially uniformly through all of the horizontal f 6 cross section of such passage.. means near the bottom of such passage to admit a gas substantially uniformly to all portions of the cross section of such passage, means to control the amount 5 of gas so admitted to give a gas velocity countercurrent to said shower sufnciently great to float and remove therefrom particles of less size than a selected minimum size, exit means for finesladen gas near the top of said passage, and means l0 for returning only the cleaned contact mass ma- 15 troduce particle form solid contact mass material thereto and means to remove it therefrom, means to introduce hydrocarbon reactants thereto and means to remove hydrocarbon reaction products therefrom, a regeneration zone, means to introduce contact mass material thereto and means to remove it therefrom, means to introduce fluid regenerating medium thereto and means to remove it therefrom, means to transfer spent contact mass from the reactor to the regenerator, means to transfer regenerated contact mass from the regenerator to the reactor, means for cleaning less than all of the moving stream of contact mass from fines comprising a confined vertical passage, means to admit acontrolled minor portion vof o the moving stream of contact mass thereto from a point between the reactor and the regenerator, means to distribute the contact mass so admitted into a shower falling substantially uniformly through all of the horizontal cross section of such passage, means to admit gas to flow upwardly through said passage at rates substantially uni.-V form across the cross section thereof, means to control the amount of gas so admitted to give a gas velocity countercurrent to said shower suf- 40 flciently great to float and remove therefrom particles of less size than a selected minimum size, exit means for fines-laden gas near the top of said passage, a gas-solid separator for removing fines from said fines-laden gas, means to direct said fines-laden gas from said exit means to said separator, a gas outlet from said separator, an outlet for withdrawal of said fines from said separator to a location outside of said system and means for returning cleaned contact massA material to the cycle.
. 4. In a system for the conversion of hydrocarbons in the presence of a particle form solid contact mass material a reaction'zone, means to inv troduce particle form solid contact mass material thereto and means to remove it therefrom, means to introduce hydrocarbon reactants thereto and 6means to remove hydrocarbon reaction productsv therefrom, a regeneration zone, means to introduce contact mass material thereto and means to a0 remove it therefrom, means to introduce iluid regenerating medium thereto and means to remove it therefrom, means to transfer spent contact mass from the reactor to the regenerator, means to transfer regenerated contact mass from the lregenerator to the reactor, means todivert a portion of the moving stream of contact mass at a point between the regenerator and the reactor, scrubbing means for said diverted contact mass comprising a vertical passage, means to introduce. diverted contact mass to said passage to pass downwardly therethrough as a shower, means to flow a gas upwardly through said passage at controlled velocity sufficient to remove finer particles of contact mass from said shower,
76 means to divert a portion of the regenerator ef.
REFERENCES CITED The following references are of record in the le of this patent:
UNITED STATES PATENTS Name Date VDegnen July 21, 1942 Number Number Number Name v Date Kuhl Nov. 24,1942 Kassel July 27, 1943 Keranen Aug. 3, 1943 Barnard Nov. 1, 1892 Balcom May 3, 1910 Peebles Sept. 28. 1943 Degnen et a1 June 6, 1944 Hemminger Nov. 7, 1944 FOREIGN PATENTS Country' Date Sweden Oct. 21, 1937
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US483120A US2423813A (en) | 1943-04-15 | 1943-04-15 | Apparatus for handling contact masses |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US483120A US2423813A (en) | 1943-04-15 | 1943-04-15 | Apparatus for handling contact masses |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2423813A true US2423813A (en) | 1947-07-08 |
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| US483120A Expired - Lifetime US2423813A (en) | 1943-04-15 | 1943-04-15 | Apparatus for handling contact masses |
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Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2489863A (en) * | 1946-06-06 | 1949-11-29 | Lummus Co | Process and apparatus for regenerating catalyst material |
| US2494794A (en) * | 1948-01-05 | 1950-01-17 | Gulf Oil Corp | Process of hydrocarbon treatment and regeneration |
| US2561331A (en) * | 1951-07-24 | Catalyst regeneration | ||
| US2563086A (en) * | 1947-06-27 | 1951-08-07 | Shell Dev | Process for segregating powdered materials into fractions of different particle size |
| US2609332A (en) * | 1948-08-25 | 1952-09-02 | Lummus Co | Hydrocarbon conversion |
| US2631981A (en) * | 1948-07-10 | 1953-03-17 | Sinclair Refining Co | Rejection of inactive material from a fluidized catalyst regenerator |
| US2664387A (en) * | 1945-05-22 | 1953-12-29 | Houdry Process Corp | Process and apparatus for catalyst classification in a moving bed catalyst conversion process for hydrocarbons |
| US2685560A (en) * | 1950-11-21 | 1954-08-03 | Phillips Petroleum Co | Means and method for converting hydrocarbons |
| US2712476A (en) * | 1950-04-24 | 1955-07-05 | Happel John | Method of conveying granular solids |
| US2713949A (en) * | 1951-02-24 | 1955-07-26 | Houdry Process Corp | Solids transfer leg |
| US2729330A (en) * | 1951-04-18 | 1956-01-03 | Houdry Process Corp | Elutriation system |
| US2772223A (en) * | 1951-06-22 | 1956-11-27 | Socony Mobil Oil Co Inc | Method and apparatus for continuously removing fines from a moving bed conversion system |
| US2786800A (en) * | 1951-06-26 | 1957-03-26 | Houdry Process Corp | Make-up catalyst addition in a hydrocarbon conversion process |
| US2809922A (en) * | 1952-03-21 | 1957-10-15 | Union Oil Co | Catalytic conversion process and apparatus with improved temperature control of the reaction |
| US2872390A (en) * | 1954-06-07 | 1959-02-03 | Exxon Research Engineering Co | Classification of particulate solids in fluid coking |
| US4276062A (en) * | 1976-05-21 | 1981-06-30 | The United States Of America As Represented By The Administrator Of The U.S. Environmental Protection Agency | Fluidized bed systems |
| US4720473A (en) * | 1986-03-10 | 1988-01-19 | Cri International, Inc. | Production of improved catalyst-type particles using length and density grading |
| US5082552A (en) * | 1986-03-10 | 1992-01-21 | Cri International, Inc. | Hydrotreating with catalyst particles using length and density grading |
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| US485525A (en) * | 1892-11-01 | barnard | ||
| US957138A (en) * | 1909-06-21 | 1910-05-03 | Nella C Balcom | Coffee-cleaning apparatus. |
| US2290580A (en) * | 1938-04-02 | 1942-07-21 | Kellogg M W Co | Method for converting hydrocarbon oils |
| US2350730A (en) * | 1938-04-02 | 1944-06-06 | Kellogg M W Co | Method for converting hydrocarbon oils |
| US2325136A (en) * | 1939-01-23 | 1943-07-27 | Universal Oil Prod Co | Process for effecting catalyzed reactions |
| US2303083A (en) * | 1939-10-21 | 1942-11-24 | Standard Catalytic Co | Catalytic reforming of hydrocarbon oils |
| US2330793A (en) * | 1940-07-31 | 1943-09-28 | Golden State Company Ltd | Classifying apparatus |
| US2362270A (en) * | 1940-11-01 | 1944-11-07 | Standard Oil Dev Co | Viscosity reducing |
| US2325611A (en) * | 1940-12-23 | 1943-08-03 | Standard Oil Co | Catalytic treatment of hydrocarbon oils |
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2561331A (en) * | 1951-07-24 | Catalyst regeneration | ||
| US2664387A (en) * | 1945-05-22 | 1953-12-29 | Houdry Process Corp | Process and apparatus for catalyst classification in a moving bed catalyst conversion process for hydrocarbons |
| US2489863A (en) * | 1946-06-06 | 1949-11-29 | Lummus Co | Process and apparatus for regenerating catalyst material |
| US2563086A (en) * | 1947-06-27 | 1951-08-07 | Shell Dev | Process for segregating powdered materials into fractions of different particle size |
| US2494794A (en) * | 1948-01-05 | 1950-01-17 | Gulf Oil Corp | Process of hydrocarbon treatment and regeneration |
| US2631981A (en) * | 1948-07-10 | 1953-03-17 | Sinclair Refining Co | Rejection of inactive material from a fluidized catalyst regenerator |
| US2609332A (en) * | 1948-08-25 | 1952-09-02 | Lummus Co | Hydrocarbon conversion |
| US2712476A (en) * | 1950-04-24 | 1955-07-05 | Happel John | Method of conveying granular solids |
| US2685560A (en) * | 1950-11-21 | 1954-08-03 | Phillips Petroleum Co | Means and method for converting hydrocarbons |
| US2713949A (en) * | 1951-02-24 | 1955-07-26 | Houdry Process Corp | Solids transfer leg |
| US2729330A (en) * | 1951-04-18 | 1956-01-03 | Houdry Process Corp | Elutriation system |
| US2772223A (en) * | 1951-06-22 | 1956-11-27 | Socony Mobil Oil Co Inc | Method and apparatus for continuously removing fines from a moving bed conversion system |
| US2786800A (en) * | 1951-06-26 | 1957-03-26 | Houdry Process Corp | Make-up catalyst addition in a hydrocarbon conversion process |
| US2809922A (en) * | 1952-03-21 | 1957-10-15 | Union Oil Co | Catalytic conversion process and apparatus with improved temperature control of the reaction |
| US2872390A (en) * | 1954-06-07 | 1959-02-03 | Exxon Research Engineering Co | Classification of particulate solids in fluid coking |
| US4276062A (en) * | 1976-05-21 | 1981-06-30 | The United States Of America As Represented By The Administrator Of The U.S. Environmental Protection Agency | Fluidized bed systems |
| US4720473A (en) * | 1986-03-10 | 1988-01-19 | Cri International, Inc. | Production of improved catalyst-type particles using length and density grading |
| US5082552A (en) * | 1986-03-10 | 1992-01-21 | Cri International, Inc. | Hydrotreating with catalyst particles using length and density grading |
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