# US 11,298,671 B2 · Bulk catalyst withdrawal system and methods for the use thereof

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- Number: US 11,298,671 B2
- Document ID: US11298671B2
- Status: Granted
- Kind: B2
- Application number: 16/609,905
- Filed: 2018-05-03
- Published: 2020-02-20
- Granted: 2022-04-12
- Earliest claimed: 2017-05-05
- Assignees: Dow Global Technologies LLC
- Applicants: Dow Global Technologies LLC
- Inventors: Matthew T. Pretz
- Web page: https://patentgrep.com/patent/US11298671B2

## CPC

- B01J 8/0055: {using cyclones}
- B01J 8/26: with two or more fluidised beds, e.g. reactor and regeneration installations
- B01J 8/0025: {by an ascending fluid}
- B01J 8/003: {in a downward flow}
- B01J 8/005: {Separating solid material from the gas/liquid stream (separation processes per se B01D)}
- B01J 8/1827: {the fluidising gas being a reactant}
- B01J 8/1863: {followed by a downward movement outside the reactor and subsequently re-entering it}
- B01J 8/388: {externally, i.e. the particles leaving the vessel and subsequently re-entering it}
- B01J 38/30: in gaseous suspension, e.g. fluidised bed
- C07C 5/333: Catalytic processes
- C10G 11/18: according to the "fluidised-bed" technique
- B01J 2208/00008: Controlling the process
- B01J 2208/00017: Controlling the temperature
- B01J 2208/00672: Particle size selection
- B01J 2208/00769: Details of feeding or discharging
- B01J 2208/00805: Details of the particulate material
- B01J 2208/00955: Sampling of the particulate material, the reactants or the products
- B01J 2219/00247: Fouling of the reactor or the process equipment
- B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- C07C: ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES

## Abstract

A method for processing a chemical stream includes contacting a feed stream with a catalyst in a reactor portion of a reactor system causing a reaction which forms a product stream. The method includes separating the product stream from the catalyst, passing the catalyst to a catalyst processing portion of the reactor system, processing the catalyst in the catalyst processing portion, and passing a portion of the catalyst from the catalyst processing portion of the reactor system into a catalyst withdrawal system that includes a catalyst withdrawal vessel and a transfer line coupling the catalyst withdrawal vessel to the catalyst processing portion. Each of the catalyst withdrawal vessel and the transfer line include an outer metallic shell and an inner refractory lining. The method further includes cooling the catalyst in the catalyst withdrawal vessel from greater than or equal to 680° C. to less than or equal to 350° C.

## Claims

### Claim 1

A method for processing a chemical stream, the method comprising:
contacting a feed stream with a catalyst in a reactor portion of a reactor system, wherein the reactor system comprises the reactor portion and a catalyst processing portion and the contacting of the feed stream with the catalyst causes a reaction which forms a product stream comprising a product and a spent catalyst;
passing the spent catalyst to the catalyst processing portion of the reactor system;
processing the spent catalyst in the catalyst processing portion of the reactor system, wherein the processing of the spent catalyst comprises raising the temperature of the spent catalyst, removing coke deposits from the spent catalyst, contacting the spent catalyst with one or more reactive gases, or combinations of these to produce a combusted catalyst;
passing at least a portion of the combusted catalyst from the catalyst processing portion of the reactor system into a catalyst withdrawal system comprising a catalyst withdrawal vessel and a transfer line coupling the catalyst withdrawal vessel to the catalyst processing portion, each of the catalyst withdrawal vessel and the transfer line comprising an outer metallic shell and an inner refractory lining;
cooling the combusted catalyst in the catalyst withdrawal vessel from a temperature of greater than or equal to 680° C. to a temperature of less than or equal to 350° C.; and
withdrawing the combusted catalyst from the catalyst withdrawal vessel after the combusted catalyst has been cooled to the temperature of less than or equal to 350° C., wherein the withdrawing of the combusted catalyst from the catalyst withdrawal vessel removes the combusted catalyst from the reactor system.

### Claim 2 (depends on 1)

The method of claim 1, wherein the inner refractory lining of the catalyst withdrawal vessel, the transfer line, or both is a thermal shock resistant refractory material having a coefficient of linear thermal expansion (CTE) of less than or equal to 2.7×10−6° K−1, according to ASTM E831-14.

### Claim 3 (depends on 2)

The method of claim 2, wherein the thermal shock resistant refractory material comprises at least one of fused silica, vitreous silica, cordierite, or a combination of these.

### Claim 4 (depends on 1)

The method of claim 1, wherein the inner refractory lining of the catalyst withdrawal vessel, the transfer line, or both is a thermal shock resistant refractory material having a strength loss of less than or equal to 25% according to the modulus of rupture standard described in ASTM C-1171.

### Claim 5 (depends on 1)

The method of claim 1, wherein the catalyst withdrawal vessel is close coupled to the catalyst processing portion of the reactor system such that an outer wall of the catalyst withdrawal vessel is within 50 feet of the catalyst processing portion of the reactor system.

### Claim 6 (depends on 1)

The method of claim 1, wherein at least a portion of the combusted catalyst is withdrawn from the catalyst processing portion of the reactor system into the catalyst withdrawal system batch-wise or semi-continuous during operation of the reactor system.

### Claim 7 (depends on 1)

The method of claim 1, further comprising passing a fluid through the catalyst withdrawal vessel and the combusted catalyst in the catalyst withdrawal vessel.

### Claim 8 (depends on 7)

The method of claim 7, wherein the fluid comprises nitrogen, argon, air, steam, or combinations thereof, and wherein the fluid has a temperature less than 350° C.

### Claim 9 (depends on 1)

The method of claim 1, further comprising:
passing the combusted catalyst removed from the catalyst withdrawal vessel to a classifier;
classifying the combusted catalyst into a smaller particle-size catalyst and a larger particle-size catalyst, wherein the larger particle-size catalyst has an average particle size greater than the smaller particle-size catalyst;
passing the smaller particle-size catalyst back to the reactor system;
re-impregnating the larger particle-size catalyst with a catalytically active material to form a re-impregnated catalyst; and
passing the re-impregnated catalyst back to the reactor system.

### Claim 10 (depends on 1)

The method of claim 1, wherein the reaction comprises dehydrogenation.

### Claim 11 (depends on 1)

The method of claim 1, wherein:
processing the spent catalyst comprises contacting the spent catalyst with one or more reactive gases; and
the one or more reactive gases comprises air.

### Claim 12 (depends on 1)

The method of claim 1, wherein:
wherein processing the spent catalyst comprises raising the temperature of the spent catalyst; and
raising the temperature of the spent catalyst comprises combusting a supplemental fuel in the presence of the spent catalyst.

### Claim 13 (depends on 1)

The method of claim 1, wherein the inner refractory lining of the catalyst withdrawal vessel, the transfer line, or both is a thermal shock resistant refractory material having a coefficient of linear thermal expansion (CTE) of less than or equal to 1.8×10−6° K−1, according to ASTM E831-14.

### Claim 14 (depends on 1)

The method of claim 1, wherein the inner refractory lining of the catalyst withdrawal vessel, the transfer line, or both is a thermal shock resistant refractory material having a strength loss of less than or equal to 15% according to the modulus of rupture standard described in ASTM C-1171.