GB2126495A - Fluid flow distribution system for fluidised bed reactor - Google Patents
Fluid flow distribution system for fluidised bed reactor Download PDFInfo
- Publication number
- GB2126495A GB2126495A GB08321690A GB8321690A GB2126495A GB 2126495 A GB2126495 A GB 2126495A GB 08321690 A GB08321690 A GB 08321690A GB 8321690 A GB8321690 A GB 8321690A GB 2126495 A GB2126495 A GB 2126495A
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- GB
- United Kingdom
- Prior art keywords
- plenum
- conduit
- reactor
- plate
- flow
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
-
- 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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
A flow distribution system for the plenum chamber (12) of a gas- liquid-solids fluidised bed reactor includes a baffled nozzle device (16) containing at least two baffle plates (30, 32, 34) for mixing and uniform flow distribution of gas-liquid- materials in the lower portion of the plenum (12), used in combination with a distribution grid (18) to effect a uniform flow distribution of the gas/liquid mixture upwards into a fluidised bed (20). A sparger can be provided in the plenum above the baffled nozzle for feeding additional gas-liquid mixture into the reactor. A fluid recycle pipe (24) may extend through the plenum chamber. <IMAGE>
Description
SPECIFICATION
Fluid flow distribution system for ebullated bed reactor
This invention relates to a fluid flow distributor device and a system for introducing feed and recycle fluid streams uniformly into a plenum and an ebullated catalyst bed of a reactor. It relates particularly to such a flow distribution system for handling petroleum and coal-oil slurry and gas streams for substantially uniform flow distribution into an ebullated catalyst bed.
Experience in operating pilot plant and commercial reactors used in the so-called "H-Oil" and "H-Coal" processes has shown that improper design of the inlet flow distribution in the reactor plenum can cause operational difficulties, such as coke formation in the plenum, flow maldistribution in the catalyst bed, localized catalyst bed slumping, and formation of coke in the bed. These problems have reduced catalyst utilization, and resulted in frequent reactor shutdowns and shortened periods of operation.
The prior art has apparently not provided an adequate solution to this flow distribution problem in fluidized bed catalytic reactors. For example, U.S. Patent No. 3,197,288 to Johanson shows a catalytic reactor configuration using simple conduits for introducing the inlet feed and recycle liquid into the reactor plenum chamber, and U.S. Patent No.
3,202,603 to Keith et al shows the use of dual spargers in the lower end of a reactor.
Also, U.S. Patent No. 3,540,995 to Wolk et al generally discloses operation of a coal hydrogenated process using an ebullated catalyst bed reactor in which feed and recycle liquid streams are introduced into the reactor lower end plenum below a flow distribution grid means. However, introducing such gas and liquid streams into a reactor plenum at high velocity requires more specific arrangements for the streams to achieve adequate mixing and uniform flow distribution. For this reason, we have now developed improved designs of flow distributor devices to provide desirably uniform flow patterns in the reactor plenum.
The present invention provides a fluid flow distributor device and flow distribution system for feeding hydrocarbon liquids or slurries and a gas uniformly into the plenum chamber and ebullated catalyst bed of a reactor. The invention comprises a flow distributor device for providing flow distribution of a liquid/gas mixture into an ebullated bed reactor, the flow distributor device being located in a plenum of the reactor, said plenum being formed by a distribution grid and the lower end and lower walls of the reactor below the grid.The flow distributor device comprises a baffled nozzle positioned at the inner end of a conduit entering the plenum for recycling a hydrocarbon fluid at least partially derived from a reaction within the ebullated bed, said baffled nozzle having at least two baffles spaced-apart from each other and rigidly attached to the inner end of said conduit, the innermost baffle consisting of a solid plate, and at least one other baffle having a central opening and located upstream of the solid plate baffle, whereby said baffled nozzle is adapted to mix a gas and a liquid material fed through said conduit into said plenum, and is arranged in combination with said distribution grid to effect a substantially uniform flow distribution of the gas/liquid mixture upwardly into said ebullated bed.
This invention also comprises a flow distribution system for providing a uniform flow distribution of a fluid material into an ebullated bed of a reactor, said distribution system comprising a plenum provided in the lower part of the reactor and formed by the reactor lower end and side walls and by a distribution grid located below the ebullated bed in the reactor, a conduit extending into said plenum for carrying a flowable fluid material into the plenum; and a baffled nozzle rigidly attached to the inner end of said conduit, said baffled nozzle having at least two baffles spaced-apart from each other, the innermost baffle consisting of a solid plate, and at least one other baffle having a central opening and located upstream of the solid plate baffle, whereby said baffled nozzle is adapted to mix a gas and a liquid material fed through said conduit into said plenum and is arranged in combination with said distribution grid to effect a substantially uniform flow distribution of the gas/liquid mixture into said ebullated bed.
This invention is particularly useful for handling hydrocarbon feedstreams such as petroleum and coal slurries for uniform distribution together with hydrogen gas into an ebullated catalyst bed reactor. Accordingly, the term gas/liquid mixture is understood to include also a gas/liquid slurry mixture containing fine particulate solids.
In the present invention, the fluid stream such as a mixture of coal-derived liquid slurry and hydrogen is passed through a conduit and a disc-donut type baffled nozzle distributor device into a plenum located at the lower end of a reactor. The distributor device usually contains a series of substantially parallel spaced-apart baffle plates located at an angle of 45-90" to the centreline of the conduit inner end, which device provides lateral or radially outward flow deflection within the plenum. Also, the central axis of the baffled nozzle distributor device is located at an angle of 0-60" with the centreline of the plenum and reactor vessel.The baffled inlet flow distributor device for the reactor plenum of gas-liquid solids fluidized bed reactors provides a fouling-free distributor device for dis persion of the kinetic energy of the flowing fluids fed into the plenum chamber. The distributor device prevents "jetting" of the recycle liquid and gas stream in the plenum, and disperses the liquid flow uniformly in the plenum.
Depending on the reactor operating conditions and the space available in the plenum, the flow distributor device can have various configurations. The liquid flow distributor device can consist of at least two preferably circular baffle plates located at the outlet of the recycle liquid conduit. For a central vertical nozzle location within the plenum, these baffle plates are usually equally spaced from each other. The distributor device top plate is solid, and deflects the inlet flow laterally to prevent direct impingement of liquid on the bottom surface of the grid plate. The other baffle or dispersion plates in the device have central openings sized to intercept and deflect portions of the liquid flow laterally or radially outwardly into the plenum.The flow paths of these lateral streams are directed to sweep the plenum bottom to eliminate stagnation zones and provide good mixing of gas/liquid (or gas/liquid slurry) and substantially uniform flow upwardly through openings in the flow distribution grid into the ebullated bed.
The percent of total material flowing radially outwardly from the space between each baffle plate can be varied by selecting the dimensions of the distributor device, but usually a greater percentage of the flow is emitted from the lowest space. In a typical deflector device design, about 40-45% of the inlet liquid flow is deflected by the first plate, 25-35% is deflected by the middle plate, and the remaining flow is deflected radially outwardly by the top plate. For a nozzle configuration entering the plenum from one side, the baffle plates are usually oriented at an angle varying from about 0' to about 10 with the adjacent baffle plate to provide a uniform dispersion of withe recycle gas/liquid flow within the plenum.
For small diameter reactors having inside diameters less than about 1.52m (5 feet), it is usually more convenient to mix the feed liquid and gas streams with the reactor recycle liquid external to the reactor prior to uniformly distributing the combined mixture in the reactor plenum, utilizing the distributor device of Fig.
1 as described below. For reactors having diameters larger than about 6 ft. (1 .83m), it is usually desirable to introduce the feed liquid and gas mixture into the reactor plenum through separate distrubutor devices. For example, a circular perforated sparger ring is usually located in the plenum upper portion and can be used to distribute the gas-liquid feed mixture uniformly across the reactor plenum. Uniform flow of small bubbles and liquid feed is produced by providing a pressure drop across the sparger and directing the mixed gas-liquid streams from the sparger
downwardly to substantially dissipate the
stream kinetic energy in the liquid. This ki
netic energy is utilized to increase the inten
sity of liquid backmixing in the plenum.Pres sure surf drops across the sparger ring openings usually range from 1-15 psi (0.069-1.034 bar) for typical heavy petroleum crude upgrad
ing and coal liquefaction processes.
In an alternative embodiment of the inven
tion, the downcomer conduit for the reactor
recycle liquid can pass through the centre of
the distributor device, which preferably con
sists of three baffle plates. The recycled reac
tor liquid enters the reactor plenum through an an annular area between the liquid down- comer and the inlet nozzle. The central open
ings of the first and middle plates are sized to
disperse the liquid flow laterally and uniformly
radially outward across the reactor plenum,
and to sweep the plenum bottom to eliminate
any stagnant zones. The top solid plate pre
vents direct impingement of liquid on the
bottom of the grid.
This inlet flow baffled nozzle distributor de vice is used upstream and in combination with
the reactor distribution grid to provide an
improved flow distribution system for an ebul
lated catalyst bed reactor. The pressure drop
across the baffled nozzle distributor device at
rated flow is usually about 5-25% of the total
pressure drop across both the distributor de
vice and the distribution grid. Although the
distribution grid can consist of a perforated
plate, it preferably contains multiple tubes
each provided with a cap over the tube upper
end. This distribution system provides im
proved gas-liquid contacting and gas mixing
in the reactor plenum, eliminates undesired
direct impingement of the fluid streams on the
distribution grid, and minimizes coke forma
tion in the plenum and in the catalyst bed.
Reference is now made to the accompany
ing drawings, in which:
Figure 1 is a vertical cross-sectional view of I the lower portion of an ebullated bed reactor
utilizing an embodiment of the invention;
Figure 2 is a vertical cross-sectional view of
a baffled nozzle flow distributor device used in
the invention;
Figure 3 shows an alternative embodiment
of the invention in which the feed and recycle
streams are introduced through separate flow
devices; and
Figure 4 shows another embodiment of the
invention similar to Fig. 3.
The invention will be further described with
reference to Fig. 1, which shows an inlet
conduit 10 for feed liquid and gas inserted
into a plenum chamber 1 2 of a reactor 14,
which may be lined with refractory insulation 1 5. The conduit has a baffled nozzle or disc
donut flow distributor device 1 6 oriented
generally upwardly therein for feeding a liquid
and gas mixture into the plenum, then uni formly upwardly through openings 1 9 in a flow distribution grid 1 8 into an ebullated catalyst bed 20.Reactor liquid is withdrawn from above the catalyst bed downward through a central conduit 24 to a recycle pump (not shown) from which the liquid is recycled together with fresh liquid and gas feed through the inlet pipe 10 to the flow distributor 16. The plenum 12 preferably has a height equal to 5-10 times the inner diameter of the conduit 10, and the distribution grid 1 8 preferably has a diameter equal to 4-12 times the inner diameter of the conduit 10.
As shown in greater detail in Fig. 2, the flow distributor device 1 6 comprises at least one annular-shaped plate 30 having a central opening 31 located upstream of a circular solid plate 32, and all retained together by three circumferentially equally-spaced structural rods 33, which are preferably located at the baffle plate outer edges. Usually, one additional annular-shaped plate 34, having a progressively smaller central opening 35 is located intermediate plates 30 and 32 to provide a preferred distributor device configuration for further radial distribution of the flow from the conduit 10.The greater percentage of flow should preferably be emitted from the lowest space, because of its greater distance for fluid travel in the plenum 1 2 before reaching the distribution grid 1 8. For a preferred flow distributor device having three plates, the plate dimensions are preferably selected such that about 40-45 volume percent of the fluid flow is deflected radially outwardly by the first baffle 30, about 25-35 volume percent is deflected outwardly by the second baffle 34, and the remaining flow is radially deflected by the solid top plate 32.
The three spaced-apart baffle plates are located at an angle of 45-90" with the centreline of the inner end of the conduit 10.
Also, the baffled nozzle axis is located at an angle ot of 0-60" with the centreline of the plenum 1 2 and the reactor 1 4. Furthermore, if desired, each baffle plate can be oriented at an angle of 0-10" with the adjacent baffle plate to provide a uniform dispersion of the gas/liquid mixture within the plenum 1 2.
Fig. 3 shows an alternative configuration of the fluid flow distribution system of this invention, wherein the flow distributor device 1 6 for recycle liquid is centrally located in the bottom of the plenum chamber 1 2 below the distribution grid 18, and extends above the bottom of the plenum by a distance equal to 1.0-2.5 times the inside diameter of the inlet conduit. The flow distribution grid 1 8 preferably contains multiple vertical tubes 26 having an inner diameter of 0.75-1.5 inches (1.91-3.81 cm) and which extend below the grid by a distance equal to 4-10 times the tube inner diameter. The tubes 26 extend above the grid by a distance equal to about 1.5-4 times the tube inner diameter.Above the upper end of each tube 26, a cylindricalshaped cap 28 is provided which is spaced away from the tube and is rigidly supported from the tube by suitable structural members (not shown). The cap 28 is oriented so as to prevent entry of catalyst solid particles from the ebullated bed 20 into the tubes 26 whenever there is no upward fluid flow through the tube, such as may occur during operational upsets or at process shutdown. A circular sparger ring 40 having uniformly spaced openings 41 on its lower side is provided above the flow distributor device 1 6 to uniformly distribute feed gas and liquid flow in the upper portion 1 2a of the plenum chamber. The sparger 40 encircles the downcomer conduit 24, and is particularly useful for large diameter reactors, such as those exceeding about 8 feet (2.44m) inside diameter.The openings 41 are sized to provide a uniform pressure drop and are located to direct the flow downwardly so as to substantially dissipate its kinetic energy and increase the backmixing action of gas and liquid in the plenum.
A downcomer 24 to a recycle pump is provided as in Fig. 1.
In another embodiment of the invention as shown by Fig. 4, a downcomer conduit 44 to a recycle pump passes through the centre of a baffled flow distributor device 46. The distributor device consists of three annular-shaped plates supported from the conduit 44 and to which fluid flow from a recycle liquid inlet is provided by an annular conduit 45. An upper solid plate 47 is rigidly attached, such as by welding, to the conduit 44 and located substantially perpendicular to the conduit 44. An intermediate plate 48 is attached to the plate 47 by three equally-spaced rods 53 and has an annular opening 49. A lower plate 50 has an annular opening 51 somewhat larger than the opening 49 in the intermediate plate 48.
Thus, the flow distributor device 46 operates similarly as for the distributor device 1 6 of
Fig. 1, whereby a portion of the total upward fluid flow passes radially outwardly through the spaces between the plates. A circular sparger 60 for feed liquid and gas is also provided in the plenum chamber 1 2 and is centrally located above the flow distribution device 46, similarly as for the Fig. 3 configuration.
The effectiveness of using the inlet flow distributor device configuration is illustrated by the following examples, which should not be regarded as limiting the scope of the invention.
EXAMPLES
In a coal hydrogenation plant using the H
Coal Process for coal liquefaction and having an ebullated bed catalyst reactor with 5 ft.
(1.52m) inside diameter (200 tons/day (203 t/day) Catlettsburg H-Coal Pilot Plant Reactor), the feed coal slurry and gas were mixed with the recycle ebullation liquid flow external to the reactor. The total combined stream was then distributed through a side-entering nozzle equipped with three inclined baffle plates, as described in the Fig. 1 embodiment of this invention. Following installation of the distributor nozzle in the plenum, coking in the reactor ebullated catalyst bed due to flow maldistribution therein was substantially eliminated.
In a commercial H-Coal (18,000 tons/day or 1 8288 t/day) Plant reactor design, having 11 ft (3.35m) inside diameter, the plenum contains a side-entering nozzle equipped with three inclined baffle plates for dispersion of the recycle liquid slurry flow and a circular sparger ring for distributing the feed liquid slurry and gas. In a commercial H-Oil (35,000 bbl/day) Plant reactor design having 10 ft.
(3.05m) inside diameter, the inlet flow distribution system in the reactor plenum consists of a vertical nozzle equipped with three horizontal plates for dispersion of the recycle ebullating liquid flow and a sparger ring for distribution of the feed-stream liquid and gas.
Claims (21)
1. A flow distributor device for providing a flow distribution of a liquid/gas mixture into an ebullated bed of a reactor, said flow distributor device being located in a plenum of said reactor, said plenum being formed by a distribution grid and the lower end and lower walls of said reactor below said grid, said flow distributor device comprising a baffled nozzle positioned at the inner end of a conduit entering said plenum for recycling a hydrocarbon fluid at least partially derived from a reaction within said ebullated bed, said baffled nozzle having at least two baffles spaced apart from each other and rigidly attached to the inner end of said conduit, the innermost baffle consisting of a solid plate, and at least one other baffle having a central opening and located upstream of the solid plate baffle, whereby said baffled nozzle is adapted to mix a gas and a liquid material fed through said conduit into said plenum, and is arranged in combination with said distribution grid to effect a substantially uniform flow distribution of the gas/liquid mixture into said ebullated bed.
2. A flow distributor device as claimed in claim 1, wherein said spaced-apart baffles are oriented at an angle of 45-90" with the centreline of the inner end of said conduit.
3. A flow distributor device as claimed in claim 1 or 2, wherein said baffled nozzle device axis is located at an angle of 0-60" with the centreline of said plenum and said reactor.
4. A flow distributor device as claimed in any of claims 1 to 3, wherein said device consists of three circular baffle plates, the lower first plate having a central opening, th.
intermediate second plate having a central opening smaller than that in said lower first plate, and the upper third plate being solid.
5. A flow distributor device as claimed in claim 4, wherein said lower first plate central opening has a diameter 0.6-0.75 times the conduit inner diameter, and said intermediate plate central opening has a diameter of 0.4-0.5 times the conduit inner diameter.
6. A flow distributor device as claimed in any of claims 1 to 5, wherein said baffle plates are spaced-apart by a distance equal to 0.3-0.5 times the conduit inner diameter.
7. A flow distributor device as claimed in any of claims 1 to 6, wherein each baffle plate is oriented at an angle of 0-10" with the adjacent baffle plate.
8. A flow distributor device as claimed in any of claims 1 to 7, wherein the fluid pressure drop across the distributor device is 5-25% of the total fluid pressure drop across the device and said distribution grid.
9. A flow distribution system for providing a uniform flow distribution of a fluid material into an ebullated bed of a reactor, said distribution system comprising:
(a) a plenum provided in the lower part of the reactor and formed by the reactor lower end and side walls and by a distribution grid located below the ebullated bed in the reactor;
(b) a conduit extending into said plenum for carrying a flowable fluid material into the plenum; and
(c) a baffled nozzle rigidly attached to the inner end of said conduit, said baffled nozzle having at least two baffles spaced-apart from each other, the innermost baffle consisting of a solid plate, and at least one other baffle having a central opening and located upstream of the solid plate baffle, whereby said baffled nozzle is adapted to mix a gas and a liquid material fed through said conduit into said plenum and is arranged in combination with said distribution grid to effect a substantially uniform flow distribution of the gas/liquid mixture into said ebullated bed.
10. A flow distribution system as claimed in claim 9, wherein the spaced-apart baffles are oriented at an angle of 45-90' with the axis of the inner end of said conduit.
11. A flow distribution system as claimed in claim 9 or 10, wherein the baffled noule axis is located at an angle of 0-60 with the centreline of said plenum and said reactor.
1 2. A flow distribution system as claimed in any of claims 9 to 11, wherein said nozzle consists of three circular baffle plates, the lower first plate having a central opening, the intermediate second plate having a central opening smaller than that of said lower first plate, and the upper third plate being solid.
1 3. A flow distribution system as claimed in any of claims 9 to 12, wherein said lower first plate central opening has a diameter 0.6-0.75 times the conduit inner diameter, and said intermediate plate central opening has a diameter 0.4-0.5 times the conduit inner diameter.
14. A flow distribution system as claimed in any of claims 9 to 13, wherein said baffle plates are spaced-apart by a distance equal to 0.3-0.5 times the conduit inner diameter.
1 5. A flow distribution system as claimed in any of claims 9 to 14, wherein an annularshaped sparger is provided in said plenum below said distribution grid and above said baffled nozzle.
1 6. A flow distribution system as claimed in any of claims 9 to 15, wherein said baffled nozzle extends above the bottom of the reactor plenum by a distance equal to 1.0-2.5 times the inside diameter of said conduit.
1 7. A flow distribution system as claimed in any of claims 9 to 16, wherein said plenum has a height equal to 5-10 times the inside diameter of said conduit.
1 8. A flow distribution system as claimed in any of claims 9 to 17, wherein said distribution grid has a diameter equal to 4-12 times the inside diameter of said conduit.
19. A flow distribution system for providing a uniform flow distribution of a fluid material into an ebullated bed of a reactor, said distribution system comprising:
(a) a plenum provided in the lower part of the reactor and formed by the reactor lower end and side walls and by a distribution grid located below the ebullated bed in the reactor;
(b) a downcomer conduit passing vertically through said distribution grid and plenum for recycling a fluid from said ebullated bed to said plenum;
(c) a conduit extending into said plenum for carrying a flowable fluid material into the plenum; and
(d) a baffled nozzle rigidly attached to the inner end of said conduit, said baffled nozzle having at least two baffles spaced-apart from each other, the innermost baffle consisting of a solid plate, and at least one other baffle having a central opening and located upstream of the solid plate baffle, whereby said baffled nozzle is adapted to mix a gas and a liquid material fed through said conduit into said plenum and is arranged in combination with said distribution grid to effect a substantially uniform flow distribution of the gas/liquid mixture into said ebullated bed.
20. A flow distribution system as claimed in claim 19, wherein said downcomer conduit is centrally located in said plenum and passes vertically through said grid and plenum, and wherein said baffled nozzle is located external to and concentric with the downcomer conduit.
21. A flow distributor device substantially as hereinbefore described with reference to and as shown in the accompanying drawings and/or the Examples.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US41642882A | 1982-09-09 | 1982-09-09 |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| GB8321690D0 GB8321690D0 (en) | 1983-09-14 |
| GB2126495A true GB2126495A (en) | 1984-03-28 |
| GB2126495B GB2126495B (en) | 1986-07-09 |
Family
ID=23649937
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB08321690A Expired GB2126495B (en) | 1982-09-09 | 1983-08-11 | Fluid flow distribution system for fluidised bed reactor |
Country Status (11)
| Country | Link |
|---|---|
| JP (1) | JPS5966340A (en) |
| AU (1) | AU565712B2 (en) |
| CA (1) | CA1229058A (en) |
| DE (1) | DE3329683A1 (en) |
| FI (1) | FI73606C (en) |
| FR (1) | FR2540402B1 (en) |
| GB (1) | GB2126495B (en) |
| IT (1) | IT1170468B (en) |
| MX (1) | MX157751A (en) |
| SE (1) | SE461017B (en) |
| ZA (1) | ZA835908B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2553300A1 (en) * | 1983-10-14 | 1985-04-19 | Hydrocarbon Research Inc | METHOD FOR UNIFORMING AN INCREASED CURRENT OF GAS AND LIQUID IN A FLUIDIZED BED REACTOR AND A FLOW DISTRIBUTION GRID FOR THE ITS IMPLEMENTATION |
| EP0319368A1 (en) * | 1987-11-30 | 1989-06-07 | Institut Français du Pétrole | Apparatus for injecting a hydrocarbon charge into a reactor |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7578669B2 (en) * | 2006-12-14 | 2009-08-25 | Texaco Inc. | Hybrid combustor for fuel processing applications |
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| GB845655A (en) * | 1957-04-18 | 1960-08-24 | Atomic Energy Commission | Multistage fluidized bed reactor |
| GB919359A (en) * | 1959-04-13 | 1963-02-27 | Svenska Skifferolje Ab | Fluidized bed reactor |
| GB1014205A (en) * | 1963-05-31 | 1965-12-22 | Basf Ag | Fluidisation reactor |
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| US3479146A (en) * | 1966-10-28 | 1969-11-18 | Exxon Research Engineering Co | Fluid flow distributor |
| US3552033A (en) * | 1968-09-03 | 1971-01-05 | Dorr Oliver Inc | Diffusion nozzle for solids fluidizing apparatus |
| US3540995A (en) * | 1968-11-14 | 1970-11-17 | Us Interior | H-coal process:slurry oil system |
| US3785779A (en) * | 1971-08-02 | 1974-01-15 | Exxon Research Engineering Co | Gas liquid inlet distributor |
| US3772211A (en) * | 1971-11-26 | 1973-11-13 | Cities Service Res & Dev Co | Process for semi-continuous regeneration of catalyst with wash liquid in a closed system |
| JPS5134385A (en) * | 1974-09-18 | 1976-03-24 | Nippon Denki Sylvania Kk | |
| JPS5436993A (en) * | 1977-08-29 | 1979-03-19 | Sumitomo Electric Ind Ltd | Oil leakage detecting element |
| US4233269A (en) * | 1978-11-09 | 1980-11-11 | Exxon Research & Engineering Co. | Gas liquid distributor |
-
1983
- 1983-08-11 ZA ZA835908A patent/ZA835908B/en unknown
- 1983-08-11 GB GB08321690A patent/GB2126495B/en not_active Expired
- 1983-08-12 AU AU17938/83A patent/AU565712B2/en not_active Ceased
- 1983-08-17 DE DE3329683A patent/DE3329683A1/en not_active Withdrawn
- 1983-08-26 JP JP58155172A patent/JPS5966340A/en active Granted
- 1983-09-06 IT IT48932/83A patent/IT1170468B/en active
- 1983-09-06 MX MX19861A patent/MX157751A/en unknown
- 1983-09-07 FI FI833189A patent/FI73606C/en not_active IP Right Cessation
- 1983-09-08 CA CA000436282A patent/CA1229058A/en not_active Expired
- 1983-09-09 SE SE8304855A patent/SE461017B/en not_active IP Right Cessation
- 1983-09-09 FR FR838314428A patent/FR2540402B1/en not_active Expired - Lifetime
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB845655A (en) * | 1957-04-18 | 1960-08-24 | Atomic Energy Commission | Multistage fluidized bed reactor |
| GB919359A (en) * | 1959-04-13 | 1963-02-27 | Svenska Skifferolje Ab | Fluidized bed reactor |
| GB1014205A (en) * | 1963-05-31 | 1965-12-22 | Basf Ag | Fluidisation reactor |
| GB1100862A (en) * | 1965-07-20 | 1968-01-24 | Hydrocarbon Research Inc | Reactor |
| GB1402543A (en) * | 1971-06-21 | 1975-08-13 | Boland K M V | Methods for passing gases through discrete solids and through liquids |
| GB1558969A (en) * | 1977-06-10 | 1980-01-09 | Apollo Heat Ltd | Fluidised beds |
| GB2012032A (en) * | 1978-01-05 | 1979-07-18 | Foster Wheeler Dev Corp | Fluidised bed start-up apparatus and method |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2553300A1 (en) * | 1983-10-14 | 1985-04-19 | Hydrocarbon Research Inc | METHOD FOR UNIFORMING AN INCREASED CURRENT OF GAS AND LIQUID IN A FLUIDIZED BED REACTOR AND A FLOW DISTRIBUTION GRID FOR THE ITS IMPLEMENTATION |
| EP0319368A1 (en) * | 1987-11-30 | 1989-06-07 | Institut Français du Pétrole | Apparatus for injecting a hydrocarbon charge into a reactor |
Also Published As
| Publication number | Publication date |
|---|---|
| FI833189A0 (en) | 1983-09-07 |
| FI73606C (en) | 1987-11-09 |
| FR2540402B1 (en) | 1992-07-31 |
| SE461017B (en) | 1989-12-18 |
| CA1229058A (en) | 1987-11-10 |
| JPH0420654B2 (en) | 1992-04-06 |
| SE8304855L (en) | 1984-03-10 |
| GB8321690D0 (en) | 1983-09-14 |
| DE3329683A1 (en) | 1984-07-12 |
| IT1170468B (en) | 1987-06-03 |
| SE8304855D0 (en) | 1983-09-09 |
| AU1793883A (en) | 1984-03-15 |
| MX157751A (en) | 1988-12-13 |
| AU565712B2 (en) | 1987-09-24 |
| FR2540402A1 (en) | 1984-08-10 |
| JPS5966340A (en) | 1984-04-14 |
| FI833189A (en) | 1984-03-10 |
| FI73606B (en) | 1987-07-31 |
| ZA835908B (en) | 1984-05-30 |
| GB2126495B (en) | 1986-07-09 |
| IT8348932A0 (en) | 1983-09-06 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PCNP | Patent ceased through non-payment of renewal fee |
Effective date: 19940811 |