* GB785363 (A)

Description: GB785363 (A) ? 1957-10-30

Counterpoise suspension

Description of GB785363 (A)

PATENT SPECIFICATION

Inventar: GEOFFREY BOULSOVER Date of filing Complete Specification:

July 1, 1955.

Application Date: July 1, 1954 No 19 Complete Specifcat Ion Published:

Oct 30, 1957.

Index at acceptance: -Class 52 ( 5), B( 2 A: 4).

International Classif ication:-F 21 b.

COMPLETE SPECIFICATION

Counterpoise Suspension We, THE AMALGAMATED DENTAL COMPANY LIMITED, of

26-40, Broadwick Street, London, W 1, a British Company, do hereby

declare the invention, for which we pray that a patent may be granted

to us, and the method by which it is to be performed, to be

particularly described in and by the following statement: -

This invention relates to counterpoise suspension of the parallel

movement type, incorporating a parallelogram linkage and a

spring-loaded cross link urging the linkage to swing in one direction,

in opposition to a load carried by the suspension and counterbalanced

thereby In one position of such suspensions the leverage exerted by

the load is generally a maxmium, and displacement on either side of

this central position causes a diminution in the leverage However,

with previous arrangements, swinging of the linkage from this central

position caused a compensating diminution in spring loading only in

one direction, whilst displacement in the other direction resulted in

a continued increase in the spring thrust In other words, the

suspension was balanced only on one side of the central position.

According to the present invention, a suspension of the type referred

to incorporates a cam and follower mechanism arranged to vary the

spring thrust in response to displacement of the parallelogram

linkage, in such a way as to provide a desired counterpoise action

automatically over a predetermined range of displacement, the long

links of the parallelogram being arranged to swing to both sides of a

horizontal position, and carry a load exerting maximum leverage on the

mounting member in that position, the profile and position of the cam

being such as to cause a diminution in spring thrust as the long links

are swung to one side of the horizontal, whilst the corresponding

diminution on the other side of the horizontal is effected only by the

sliding of the cross link.

In one well known arrangement of counlPrice 3 s 6 d l 785363 U 298/54.

terpoise suspension the cross link extends from a first pivotal point

on the parallelogram linkage, to an intermediate position on the

longer of the opposite links of the 50 parallelogram, and is there

slidably constrained to that link The spring is a helical compression

spring embracing the last mentioned link, constrained between a second

pivotal point of the parallelogram 55 and the sliding end of the cross

link The link between the first and second pivotal points of the

parallelogram serves as a mounting member, and is normally fixed,

though it may be adjustable 60 On a change in configuration in the

parallelogram, relative movement of the sliding end of the cross link

occasions a change in the spring thrust According to one embodiment of

the present invention, the effect 65 of this change is supplemented by

a cam fitted adjacent the second pivotal point and fixed relative to

the mounting member, associated with a follower against which the

adiacent end of the spring abuts 70 One embodiment of the invention is

illustrated in the accompanying drawings of which: Figure 1 is a side,

partly sectional view with a cover plate removed, 75 Figure 2 is a

sectional view on the line IIII of Figure 1, Figure 3 is a sectional

view on the line III-III of Figure 1, Figure 4 is a

part-sectional-view from be 80 low of the left-hand portion of Figure

1, with part of the cover plates cut away, and Figure 5 is a view from

above of -the lefthand portion of Figure 1, with part of the cover

plates cut away 85 The suspension comprises a mounting member in the

form of a metal plate 1 formed at one end as a saddle 2 and there

connected by a vertical swivel pin 3 in the plane of the plate, to a

support 4 for swinging about a 90 vertical axis At a first pivot point

5 in plate 1, there are pivotally attached a pair of dished steel

sheets or cover plates 6 forming a sleeve, and at a second pivot point

7 vertically below the first is pivoted a bifurcated end fitting 8 of

a tubular steel strut 9, housed S within the sleeve Strut 9 and the

sleeve (plates 6) form the two long links of a parallelogram linkage,

plate 1 forms one short link and a metal plate 10 (similar to plate 1

but without the hereinafter described cam profile) connected by a

vertical swivel pin 11 to a support 12 for a load to be carried (not

shown), forms the other short link The latter is pivoted by a

horizontal pin 13 to plates 6 and by another such pin 14 to a biis

furcated end fitting 15 of strut 9.

Also pivoted at pivot point 5 is a second, flat strut 16 constituting

a cross link shorter than strut 9 and parallel thereto, housed within

plates 6 At its other end strut 16 is pivoted by a pin 17 to plates 6

and to a bearing 18 slidably engaged on strut 9 End fitting 8 is

slotted at 19 and houses a roller between its bifurcated limbs,

mounted on a pin 21 extending through the slots and yoked by straps 22

to a bearing 23 (which may be integral with the straps) sidably

engaged on strut 9 Between bearings 18 and 23 a helical compression

spring 24 is fitted, urging roller 20 against the inner end of plate 1

which is-profiled at 25 as a cam This profile is substantially

circular about pivot point 7 at its upper portion, but more sharply

curved at its lower portion 26 so that, as the sleeve formed by plates

6 is depressed below the horizontal, bearing 23 recedes relative to

the corresponding movement of bearing 18.

In this way, the thrust of spring 24 is caused to diminish whether the

sleeve is swung upwards or downwards from a horizontal position The

cam profile is arranged so that the resulting change in the thrust

exerted by the spring, together with the leverage exerted by roller 20

on strut 9, give rise to a degree of counterpoise, within a

predetermined range of displacement of the suspension balancing the

load which is carried.

For fine adjustment purposes, bearing 1 incorporates a spring abutment

27 carried by a screw-threaded sleeve 28 The outer part of bearing 18

is in the form of a split sleeve 50 formed with lugs 29 between which

strut 16 is held by the pin 17.

For use with an electric lamp, wires 30 and a switch 31 are

incorporated.

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* GB785364 (A)

Description: GB785364 (A)

No title available

Description of GB785364 (A)

PATENT SPECIFICATION

iventors: HERBERT FREDERICK RAN CE, MERRIK BURRELL BAGGALLA Yand

WILLIAM FREDERICK EDWARD ROBINSON 785364 Date of f Ping Complete

Specif Ication: July 7, 1955.

Application Date: July 8, 1954.

No 20074154.

Complete Specification Published: Oct 30, 1957.

da at acceptance:-Class 96, A 2, A 7 B( 6: 14: 15).

taternational Clasification:-D 21 f, g.

COMPLETE SPECIFICATION

Improvements in or relating to Paper Making Machines We, BERTRAMS

LIMITED, a British Company, of Saint Katherine's Works, Sciennes,

Edinburgh 9, do hereby declare the invention, for which we pray that a

patent may be granted to us, and the method by which it is to be

performed, to be particularly described in and by the following

statement: -

The invention relates to paper making machines of the kind in which

the paper, formed from pulp as a continuous web on a travelling wire

mesh and, after removal of some of the water, is transferred from the

wire to a travelling receiving surface, usually a felt.

It is an object of the invention to improve the separation of the

paper web from the wire.

The invention is based on the appreciation of the facts that if the

web is subjected to suction through the wire, water is sucked from the

web and forms a film between the web and the wire, that this water

facilitates clean removal of the web after release from the suction,

provided that such removal is effected before re-absorption of the

water is allowed to occur, and that if the web is transferred to the

felt across a gap so that there is no pressure applied between the

felt and the wire, there will be less tendency for the web to adhere

to the wire or to be marked thereby and, further, unwanted trim from

the edges of the web will not be transferred to the felt.

It is known in a machine of the above kind to remove the web from the

wire immediately after passing a perforated suctioncouch but it is

found that the perforations tend to produce shadow markings on the

paper and separation may be more difficult from the land areas between

the perforations where suction has not been applied to the web.

According to the present invention a machine of the above kind is

characterised by the features that the receiving surface is spaced

from the wire at the transfer-position lPrice 3 s 6 d l by a small

distance which is greater than the web thickness and there is

immediately prezeding the transfer position a continuous transverse

suction slot which continuously 50 draws water from the web into the

wire from substantially the whole width of the web and so facilitates

separation of the web and wire.

It is to be appreciated that in carrying out the invention the water

is drawn from the 55 whole width of the web without interruptions such

as would be caused by the land areas of a perforated couch roll.

In a preferred form of the machine according to the invention there is

included a trans 60 verse slot closely or immediately following the

suction slot for emission of compressed air to assist in separation of

the web from the wire and transfer of the web to the felt It is

further preferred that the air slot extends 65 across the full width

of the web and the arrangement may be that the air is emitted

continuously during the operation of the machine.

In one construction of the machine ac 70 cording to the invention the

web-carrying wire passes over a perforated suction couch before

reaching the suction slot aforesaid and there is a sufficient distance

between the couch and the slot for local inequalities in 75 the water

content of the web caused by the couch and which might result in

shadow markings in the final product, to become sufficiently equalised

to avoid production of such markings The distance required for 80 this

purpose varies considerably with the speed of operation of the machine

and other factors such as the kind and weight of paper being made It

may for example be between three inches and two feet A distance of 85

twenity to twenty-four inches is commonly found suitable.

In another construction of the machine according to the invention the

water content of the web is reduced by one or more suction 90 boxes

having transverse suction slots over which the web passes 'before

reaching the 2 785364 aforesaid suction slot at or immediately before

the transfer position If desired both a suction box or boxes and a

suction couch roll may be used.

S By way of example of how the invention may be carried into effect

there will now be described with reference to the accompanying

drawings, a box embodying suction and compressed air slots and some

specific applications of this box to paper making machines.

In the drawings Figure 1 is a side elevation of the box, Figure 2 is a

plan view showing a part of the box, Figure 3 is a section on the line

3-3 in Figure 2, Figure 4 is a view of one of the end cover plates for

the box, Figure 5 is a diagram showing the application of the box to a

paper making machine, Figure 6 is a diagram showing the application of

the box to a modified form of machine, and Figure 7 is a diagram

showing another application of the box.

The box, shown in Figures 1-4, cornprises two longitudinal side plates

10 and 11 and an intermediate plate 12 which are separated by distance

pieces 13, 14 and define between them two longitudinal channels 16, 17

for suction and compressed air respectively.

The plates are secured together by clamping bolts 20 and at each end

are provided with flange plates 21, 22 A cover plate 23 is attached to

the flange 22 to form a closure for the ends of the channels and a

plate 24 is bolted to the flange 21 The plate 24 has pipe connections

26, 27 for suction and air respectively which lead through ports 28,

29 to the ends of the channels 16, 17.

Cover plates 30 close the mouths of the channels at each end of the

box and plates 31 screwed to the edges of the plates replace tie

distance pieces 13, 14 for a short distance at each end.

Secured to the upper edges of the plates 10, 11 and 12 there are metal

channels 33, 34, 35 which hold laminated plastic strips 36, 37, 38

defining slots 39, and 40 for the suction and air, the air slot 40

being narrower than the suction slot 39 The ends of the slots are

defined by short cross strips 42 of plastic.

SS Brackets 43 44 are secured to the side plates 10 and 11 and provide

means by which the box may be secured to the frame members of the

machine The brackets have slots for securing bolts and the brackets 44

have adjusting screws 46 by which the box may be adjusted in position

lengthwise of the machine before the bolts are tightened.

In one machine embodying the invention, see Figure 5, the web-carrying

wire 50 is 69 taken around a perforated suction couch roll 51 and then

along a downward sloping path to a lower, driving roll 52 At a

position intermediate between the couch roll 51 and the driving roll

52 there is located a suction and compressed air box 54 as above

described 70 with the suction slot ( 39) preceding the compressed air

slot ( 40) The slots extend crosswise and below the wire Immediately

opposite to the box there is a vacuum transfer roll 56 around which

there passes an upper 75 felt 57 The felt is a short distance (i e A

inch or less) from the web carried on the wire This distance is

greater than the thickness of the web but not so great as to cause

difficulties in transfer to In use some of the water is extracted from

the web into the couch roll 51 The web then passes to the suction and

air box, there being sufficient distance (e g one to two feet

depending on the speed of travel of the web) Rs between the couch roll

and the box for sufficient equalisation of the water content of the

web to avoid the production of shadow marking As the web passes over

the suction slot 39, water is extracted substantially evenly 90 over

the whole width of the web and forms a film between the web and the

wire The web then passes immediately to the compressed air slot 40 and

is readily separated from the wire by the air and blown on to the felt

57 as 95 the latter passes over the vacuum transfer roll 56 The web

then passes to a press embodying a lower felt 58 and a suction roll 59

by which further water is extracted The trim which lies outside the

ends of the suc loo tion and compressed air slots remains on tne wire

and may be removed from the wire when it passes over the driving roll

and run to a hog pit 60 from which it may be pumped back for immediate

re-use 105 In the modified form of the machine as just described,

shown in Figure 6, the upper felt 57 is replaced by a lower felt 62

which passes around a roll 63 opposite to the box, the roll not

necessarily being of the vacuum type 110 The web is blown on to the

top of the felt and runs with the felt through a plain press 64, 65.

In another example of the machine according to the invention, shown in

Figure 7, 115 the web-carrying wire 70 passes in a horizontal run

firstly over two suction boxes 71, 72 and then to the above described

combined suction and compressed air box 73 The air blows the web 74

upwardly on to a lower 120 felt 75 which passes over a roll 76 spaced

a short distance above the wire The wire then continues to a driving

roll 77 No suction roll couch is employed in this example.

The felt carries the web to a plain press 125 78 79.

The invention is particularly suitable for the use in the manufacture

of very light weight or very wet beaten papers and has the advantages

that the formation of shadow 130 2:,.

785,364

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* GB785365 (A)

Description: GB785365 (A) ? 1957-10-30

A new or improved gear control lever

Description of GB785365 (A)

PATENT SPECIFICATION

Inventor: JAMES DENNE BATTEN Date of filing Complete Specification:

Nov 4, 1955.

Application Date: Aug 5, 1954 785,365 No.22844/54 Complete

Specification Published: Oct 30, 1957.

index at acceptance:-Class 80 ( 2), D 3 C.

International Classification:-FO 6 h.

COMPL ETE SPECIFICATION

A new or improved Gear Control Lever We, HUMBER LIMITED, a British

Company, of Stoke, Coventry, Warwickshire, do hereby declare the

invention for which we pray that a patent may be granted to us, and

the method by which it is to be performed, to be particularly

described in and by the following statement: -

The invention relates to manually operable control levers for

change-speed gears (e g for motor vehicles) and is concerned with such

levers of the kind incorporating an electric switch which is operated

by a lateral force applied to the lever for the purpose of engaging or

disengaging a gear, before effective movement of the lever takes place

The switch may be employed to control a clutch or other component of a

transmission system incorporating the change-speed gears.

It is an object of the invention to provide a simple and effective

construction of such a lever in which the switch is operable in

whatever lateral direction the force is applied.

The invention provides a gear control lever for a manually operable

change-speed gear which lever is constructed of two elongated parts

nested one within the other in spaced relation, one of the parts being

arranged for manual operation to rock the lever and the other part

being arranged for connection to the gear mechanism to be changed by

such rocking movement, an annular electric contact surface on one part

surrounding a contact surface on the other part and normally separated

therefrom, the two parts being relatively movable transversely to

their length to the limited extent required to engage the contact

surfaces by pressure applied to the manually operable part in any

direction to rock the lever and a tubular spring (as herein defined)

surrounding the inner part and bearing at its opposite ends on the two

parts respectively to provide a centralising force tending to maintain

the contact surfaces disengaged, which force may readily be overcome

by pressure applied in the lateral direction to the manually operable

lPdrice 3 s 6 d) part thereby to engage the contacts as a preliminary

to a gear changing operation.

It is not essential that the contact surface should be a complete

annulus It may be 50 divided into circumferentially separated portions

provided that these portions are sufficiently close that engagement of

the contact surfaces is obtained by any direction of rocking movement

of the manually operable 55 part as aforesaid and the expression

"annular" is used herein in that sense.

The expression "tubular spring" is used herein to mean a resilient

tube, helical spring or like element which is capable of surround 60

ing the inner part and providing a restoring force when its ends are

laterally displaced in any direction by bending of the element.

Preferably the tubular spring is within the space between the parts 65

It is also preferred that the two parts are capable of relative axial

movement for the purpose of engaging and disengaging a stop or latch

limiting the movement of the lever.

One specific construction of a gear lever T according to the invention

will now be described by way of example of how the invention may be

carried into effect and with reference to the drawings herein, in

which:Figure 1 is a section through the lever and also shows the

electrical connection; and Figure 2 is an enlarged view of parts of

the lever.

In this example the features of the inven 80 tion are embodied in a

gear lever constructed as shown in Figures 1 and 2 of the drawings of

Specification No 614,658 and described in that specification, the

lever being intended to be mounted on the steering column of a 85

motor vehicle.

In the present construction the outer end of the tubular hand lever is

of increased diameter and is spaced away from the internal rod 12

(which corresponds to the rod 90 shown at 12 in the drawings of

Specification

No 614,658) Furthermore the interior of the bore of the knob 13 is of

enlarged diameter to permit lateral movement of the knob in relation

to the hand lever 10 The support 14 for the inner end of the internal

rod is also arranged to permit, by pivotal movement around the bearing

15 in the support, such lateral movement of the knob.

Within the outer end of the hand lever 10 there is a thin-walled brass

tube 16 which surrounds the internal rod 12 and extends about half way

to the bearing 15 for the inner end of the rod This tube, which

constitutes the aforesaid tubular spring, is supported at its outer

end by a bush 17 of electrically insulating material fitted betveen

the tube 16 and the mouth of the hand lever 10 At its inner end the

tube is lined with a similar bush 18 which is a sliding fit on the rod

12.

The bushes may for example be of the material known under the trade

names "Tufnol" (Registered Trade Mark) and "Nylon".

At the outer end the mouth of the tube 16 is arranged to constitute an

annular contact surface 20 which may make an electric connection with

the rod 12 but is normally spaced therefrom The rod 12 is "earthed"

and an electric connection 22 is taken from the tube 16 to the coil 23

of a solenoid for operating a clutch or to the coil of a relay which

controls the clutch solenoid.

In use the tube 16 serves to maintain the rod 12 in a central position

out of contact with the contact surface 20 of the tube If a lateral

force is applied to the knob in any direction, the effect is to move

the rod laterally into engagement with the contact surface of the

tube, at the same time causing a lateral deflection of the inner end

24 of the tube and so creating a restoring force The resistance to the

movement of the rod which is offered by the tube, is less than the

resistance to movement of the lever and consequently the contact is

made before the operation of engaging or disengaging a gear has begun

This result is achieved by a suitable selection of the thickness of

the walls of the tube and of the unsupported length of the tube

between the two bushes.

The arrangement described in the above example has the advantages that

there is no interference with the axial movement of the knob and rod

required to release the reverse.

stop, any spark which may occur between the contact surfaces is masked

by the lever and knob and that there is no risk of electric shock to

the operator.

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* GB785366 (A)

Description: GB785366 (A) ? 1957-10-30

Improvements relating to the transference of solid particles between systems

at different pressures

Description of GB785366 (A)

COMPLETE SPECIFICATION Illr-lnprosreeam relating to zone

lEransfeLeLas:e or of Solid Particles

between Systems R LfiFereEat pressures

We, GULF OIL CORPORATION, a Corpora tion organized under the Laws of

the State of

Pennsylvania, and doing business at Gulf

Building, Pittsburgh, Pennsylvania, United

States of America, do hereby declare the invention, for which we pray

that a patent may be granted to us, and the method by which it is to

be performed, to be particularly described in and by the following

statement:

This invention relates to a valve apparatus which will permit the flow

of solid particles therethrough without substantial passage of gas

therethrough. The inevntion also includes the inclusion of such valve

apparatus in a system for circulating solid particles.

The control of flow of solid particles such as during the introduction

into and removal of solid particles from a high pressure system is a

problem which has been frequently encountered but has not been

oompletely solved. Solid particles can be suspended in a liquid to

form a slurry and then passed through valves or the lisle. However,

there is a limit to the amount of solids that can be suspended and

still have a liquid, flowing mix- ture. Also wear of apparatus takes

place and it is frequently undesirable to wet the solid particles with

a liquid. Also, solid particles can be suspended in a gas to resemble

a fluid and passed through ordinary gate or compression valves.

However, the moving parts of such valves are rapidly destroyed by the

abrasive action of the solid particles. It has been proposed in a

system for cracking petroleums with the aid of a fluidized catalyst to

utilize a densely packed column of solid particles as a means for

flowing solid particles while preventing flow of gas between two

systems having a pressure differential. In this particular operation

the pressure differential within the system in which the catalyst

particles are circulated is relatively small.

Tests indicate that this procedure is satisfactory for small pressure

differentials only. For instance, a densely packed column of solid

partides of one typical fluid craclting catalyst 3 feet high is blown

out of the vertical conduit in which it is contained when the pressure

differential is 10 pounds per square inch.

Similarly a densely packed column 26 feet high is blown out of the

supporting vertical conduit when the pressure differential is 29

pounds per square inch by gauge. It is evident that exceedingly long

packed columns would be required for high pressure differentials.

Also, even with low pressure differentials there is some leakage of

gas from the high pressure end of the column to the low pressure end

of the column. In other words, the particles are not a complete

stopper or plug. This leakage of gases cannot be tolerated in certain

operations.

This invention has for its object to provide apparatus whereby the

foregoing difficulties can be overcome.

Another object is to provide apparatus which will permit controlled

passage of solid particles therethrough but which will not permit

substantial gas flow therethrough.

Another object is to provide apparatus for removal of solid particles

from a high pressure system to a low pressure system without

substantial loss of gas from the high pressure system into the low

pressure system.

A still further object is to provide an apparatus for introducing

solid particles into a high pressure system and removing solid

particles from the high pressure system without substantial leakage of

gas during such transfer.

Other objects will appear hereinafter.

It has hitherto been proposed in apparatus for conducting catalytic

reactions in a continuous cyclic system to provide means for releasing

fluid from the catalyst discharged from a treating chamber comprising

a conduit through which catalyst is discharged from said chamber, an

enlarged depressuring chamber at an intermediate point in said

conduit, means in said catalyst-discharge conduit for keeping that

portion of said conduit above the depres suring chamber filled with

catalyst and for accumulating a mass of catalyst in the bottom of said

depressuring chamber, said depressuring chamber being so formed as to

provide a substantial space above the mass of catalyst accumulated

therein; and a fluid outlet in the top of said depressuring chamber,

the bottom of said depressuring chamber communicating with the

remainder of said discharge conduit

According to the present inevntion, we provide apparatus for use in

effecting a substantially gas-tight seal between spaced zones between

which there exists a pressure differential and which are in

inter-communication for the transference of solid particles

therebetween comprising conduit means interconnecting said zones and

providing said intercommunication, at least a length of said conduit

means being substantially vertical, supporting means at or below the

lower end of said conduit length adapted to support solid particles to

establish a compact column of solid particles within said conduit

length, at least one gas vent communicating with said conduit length

intermediate the ends thereof, means associated with said vent to

prevent substantial flow of solid particles through the vent, and

means for controlling the flow of solid particles through said conduit

length.

Also, according to the present invention, we provide a manufacturing

process including a method of effecting a substantially gas-tight seal

between spaced zones between which there exists a pressure

differential and which are communicatively interconnected for the

transference of solid particles therebetween, said method comprising

forming the particles into a movable vertical compact column the ends

of which are exposed to the different pressures, venting gas leakage

from the high pressure zone at a point intermediate the ends of said

column, and preventing leakage of solid particles with the vented gas.

In the following examples and description are set forth several of the

preferred embodiments of the invention but it is to be understood that

these are given by way of illustration and not in limitation thereof.

The accompanying drawings illustrate apparatus embodying the

principles of the invention. Referring to these drawings:

Figure 1 is a diagrammatic elevation in section of apparatus for

removing solid particles from a high pressure system to a lower

pressure system in accordance with the invention;

Figure 2 is an enlarged diagrammatic vertical section showing details

of the filtering means utilized in Fie 1;

Figures 3 and 4 are enlarged diagrammatic elevations in section of

alternative apparatus for controlled removal of solid particles from

the base of the vertical column of solids;

Figure 5 is a graph illustrating the manner in which the gas pressure

and the solids pressure varies throughout the length of the vertical

compact column of solids;

Figure 6 is a diagrammatic elevation, partly in section, of suitable

apparatus for carrying out a complete and continuous high pressure

operation in which solids are continuously introduced and removed from

the high pressure chamber in which the operation is carried out; and

Figure 7 is a diagrammatic elevation of continuous apparatus similar

to that illustrated in Figure 6 except that the necessity for long

loops of conduit at the top of certain of the vertical columns of

solid particles is avoided.

Figure 8 is a diagrammatic elevation, partly in section, of suitable

apparatus for carrying out a high pressure operation in which solids

are continuously introduced into and removed from a high pressure

chamber in which the operation is carried out.

The basic feature of the invention will be readily understood by

referring to Figure 1.

In this figure numeral 10 indicates a high pressure chamber in which

an operation utilizing solid particles in fluidized form is carried

out.

For convenience, a hydrocracking or destructive hydrogenation

operation will be described.

This operation would be conducted in this reactor by introducing

hydrogen and vapors of a hydrocarbon to be hydrocracked through

conduit 12 and under high pressure. The hydrogen and vapors maintain

the solid particles in reactor 10, which in this instance would be a

hydrogenating catalyst, in a fluidized condition in which there is a

lower dense phase and an upper light phase. The hydrogen and the

hydrocarbon products are separated from the solid particles in cyclone

separator 14 and flow out of the system through conduit 16. Solid

particles in a fluidized condition, i.e., suspended in the hydrogen,

settle into the top of vertical conduit 18 by gravitational force. The

upper part of column 18 serves as a scrubbing section, the

hydrocarbons and the hydrogen associates with the solid particles

being removed by a scavenging gas such as high pressure steam

introduced through conduit 20. The passage of gas through conduit 20

is at a rate such that the solid particles slowly settle through the

upflowing current of gas and finally become lodged in the portion of

the conduit 18 below conduit 20. The solids in this column settle into

a vertical compact column which is supported by a cup-shaped member 22

positioned at the base of the column and within hopper 28 which is at

a substantially lower pressure; i.e., in the case under consideration

about atmospheric. A certain amount of gas introduced as scavenging

gas will pass through the interstices between the particles in the

upper part of column 18 below 20. Due to the resistance to flow of gas

through the compact column the pressure of the gas will progressively

decrease during such passage. These gases are vented at relatively low

pressure through vent 24 which is provided with means for preventing

flow of solid particles from the column 18 through the vent. The

pressure of the gas and/or solid particles at the base of the column

is therefore relatively low and the accumulation of a small pile of

catalyst in cup 22 prevents the uncontrolled flow of catalyst

particles from the column.

Catalyst particles contained in cup 22 are continuously or

intermittently blow therefrom by gas passing through nozzle 26. Upon

such removal the solid particles in column 18 flow downwardly to

replace those which have been removed. If these are permitted to

accumulate a small pile of catalyst again forms around the base and

will prevent further flow until removed by the action of nozzle 26.

This removed catalyst is conveyed by the current of gas into hopper 28

and thence into the conduit 30 where it is picked up and transported

to any desired location by low pressure transport gas passed through

conduit 30.

Referring to Figure 2, numeral 18 designates the vertical conduit of

Figure 1 containing the compact solid particle column.

Numeral 32 designates a plurality of conduits connected to conduit 18

the ends of which are covered with wire cloth filters 34. These wire

cloth filters are held in place by pipe nipples 36 and pipe couplings

38. The ends of nipplies 36 connect to reducers 40 and conduits 42

which may be connected to any suitable gas disposal or recovery

system. The wire cloth filters 34 should have a sufficiently fine mesh

to prevent substantial flow of the solid particles therethrough. This

filter effectively vents the gas passing downwardly through the upper

portion of the compact column in 18 and at the same time prevents

substantial passage of solid particles through the vent. The screen or

means for preventing passage of solid particles is important since the

rate of flow of gas at this point will in most cases be sufficient to

transport the solid particles and cause a blowout through the compact

column and the vent unless such filtering means or the like is

provided.

Any device which will prevent substantial flow of solid particles

through the vent can be used. For instance, a graduated bed of pieces

of solid which increase in size as the vent is approached could be

used to prevent the flow of solid particles through the vent. It is

not necessary, as far as the operation of the vertical compact column

is converned, to prevent all of the solid particles from passing into

the vent. A small amount of particles passing through the vent will

not upset the sealing action of the compact column. However, such

passage may be undesirable for other reasons, such as abrasion of

apparatus beyond the vent or loss of solid particles and for such

reasons the passage through the vent is kept as low as possible and

usually at about a zero value.

If the vent between the upper and lower parts of the conduit 18 were

not used the high pressure gas contained in the chamber 10 would pass

downwardly through the compact column and if these was a material

pressure differential between the top and bottom of the column this

passage of gas would be at a suffi- cient rate to transport catalyst

at the bottom of the column. This would result in a blw-out of the

entire column and nullify the purpose of the column. Of course this

could be avoided by utilizing an exceedingly long column. How- ever,

as indicated above, impractically high columns would be required for

material pressure discferentials. By means of the present invention a

compact column 6 feet high is adequate to operate with a pressure

differential of 101B pounds. A column 27 feet high is entirely

adequate for a pressure differential of 960 pounds. Without the vent a

column approximately 200 feet high would be required for a pressure

differential of 100 pounds per square inch gauge.

Figures 3 and 4 illustrate other methods for controlled removal of

solid particles from the base of the column. Referring to Figure 3,

numeral 42 designates a cup-like container or support at the base of

the column 18, which container is positioned in closed receptacle 44.

Receptacle 44 is connected to transport conduit 46 at its lower

extremity. Cup 4d2 is supported by a shaft 48 which can be moved

upwardly or downwardly by means of screw 50.

Movement of the cup up or down adjusts the rate of flow of catalyst or

solid particles from the base of the column 18. The pile of solid

particles builds up in cup 42 and overflows the upper edge thereof. If

the cup is raised the pile of catalyst will rise above the lower edge

of vertical conduit 18 and plug up the lower end of the column and

thus prevent further flow of catalyst or solid particles. If the cup

42 is lowered the solid particles will at some point begin to overflow

the edge of the cup and the lower the cup is positioned the greater

the rate of flow. The removed solid particles flow into conduit 46

where they are picked upoby transport gas introduced through conduit

52.

Referring to Figure 4, numeral 54 indicates a cuike member positioned

below vertical conduit 18 in which a pile of solids is permitted to

accumulate under the end of the column 18. Numeral 56 designates a

conduit connected to the lower part of cup 54 and provided with a

slide valve 58. Numeral 60 designates a conduit for removal of solid

particles by means of transport gas introduced through conduit 62. The

rate of flow of the catalyst from cup 54 is determined by the setting

of slide valve 58. If the slide valve is closed the solid particle

pile will build up in cup 54 and plug the end of the column and

prevent further flow. Opening the slide valve permits catalyst to flow

from around the base of the column which initiates flow of solids from

the column.

Mechanical removal means may be used instead of the devices

illustrated in Figures 3 and 4. For instance, an endless conveyor belt

run at controlled speed under the end of the column may be used to

obtain controlled removal of the solid particles. Similarly a screw

conveyor for the solid particle removal could be used.

Figure 5 illustrates the manner in which the pressure of the gase and

the pressure of the solid particles (the vertical pressure) varies

down the length of a column when the pressure differential is

approximately 900 pounds and the height of the column is roughly 23

feet, with the vent at the mid point It will be noted that the gas

pressure (solid line) falls to zero at the vent and that there is no

gas pressure between the vent and the lower end of the column. On the

other hand, the pressure of the solids as determined at any point in

the column (shown by the doted line) reaches a maximum point in the

neighborhood of the vent. This pressure is dissipated against the

walls of the column. The pressure at the base of the column is

negligible due to the absence of solids pressure as well as gas

pressure at the base of the column. Therefore very little support for

the column of solid particles, other than that due to the weight of

the solids, is required and the removal of the catalyst under these

conditions is a relatively simple matter.

It is preferable to employ a vent at approximately the mid point of

the column. However, the position of the vent can be varied

considerably as long as sufficient column length of compact solid

particles is provided below and above the vent to dissipate the gas

and solid pressure so that it will not upset the lower part of the

column. A plurality of vents may be employed and these may be spaced

at intervals up and down the column if desired.

The filter for preventing flow of solid particles through the vent

must permit adequate flow of gas. The gas flowing through the fore

part of the column preferably should be permitted to escape freely

through the vent rather than to be largely compelled to flow through

the after part of the column. Any solid particle removing means mav be

used.

It is desirable, although not necessary, to have the solid particles

in fluidized condition when they are fed into the column and prior to

the time when they fonn the compact column. This results in even

distribution of the solid particles in the column and avoids

possibility of formation of cakes or gobs of particles which might

bridge across the column and result in uneven feeding through the

column. The size of the particles can vary to a considerable extent.

Also, th particles need not be unifcrm in size. In general a mesh size

of between about 100 and 400 mesh can be utilized. The larger meshes

will require longer vertical columns.

The diameter of the column is of course determined by the volume of

solid particles that must pass through it. The compact column will

under most conditions move at least 50,000 lb./hr./sq. ft. of fluid

type catalyst. The catalyst flow rate does not appreciably affect the

gas flow through the column.

In general the length of the column will depend upon how much gas can

be permitted to flow through the vent and the location of the vent If

a large amount of gas passing through the vent can be tolerated a

large vent and a shorter column can be used. On the other hand, a

longer column would be necessary i. minimum vent gas is desired. The

location of the vent about at the mid point gives optitnum results.

However, it can be located o centre to any desired extent but in such

case the column must be of sufficient length between the high pressure

zone and the vent to appreciably lower the pressure by the resistance

opened by the solid particles to the flow of gas between the high

pressure end and the vent and between the vent and the low pressure

end. The vent must be far enough from the low pressure end of the

column to prevent gas flowing from the end at a sufficientt high

velocity to blow out the catalyst acting as a plag or seal.

Specifically, the length of the pressure seal leg, is determined bp

the allowable amount of total gas leakage, that is, the longer the leg

the less the total gas leakage. This total leakagis the sum ofI-

(1) leakage through the vents (the great majority of the. gas leakage

occurs at this point), and

(2) the leakage from the bottom of the cslurun. Once the total gas

leakage is decided upcn, the mimmurn operable length of the column may

be determined by the following formula -

S' -p,'

L=O.0235

G

Where = > column length in feet

Pi=inlet pressure in pounds per

square inch

Pro =outlet pressure in pounds per

square inch

6=total gas leakage based on cross

sectional area of the column

lb./hr./sq. ft.

k this point in the calculations the length of the column and the

total gas leakage have been determined. However, nothing is known

concerning the distribution of the gas leakage, i.e.-what part of the

gas goes through the vents and what part leaves the bottom of the

column. The gas leakage through the vent or vents is a function of: -

(1) the cross-sectional area of the vents and

(2) the depth of the catalyst on the vent retaining screens. These two

variables are related by the following formula:

Ab Aa -= (0.647 G-1)

Lb L

Where Aa=area of the column in sq. ft.

Ab=vent area in sq. ft.

Lb=thickness of layer of solids on the

vent retaining screens in ft.

The other symbols are defined as in the first formula above.

The above equations wilt serve as general guides, but it is to be

noted that they are determined for a case involving an inert gas, a

solid particle of 2501 mesh and atmospheric temperature. Suitable

adjustments for other materials and conditions must be made.

A column designed by the above formulas would be in the direction of

the minimum length which should be used and that greater lengths would

reduce the total amount of gas leakage. Therefore in the final

analysis while the above formulas would be used as a guide in

determining the length of the column and the vent requirements the

final sizing of the column would be determined by economic

considerations, for example, it might be found desirable to make the

column somewhat longer than the length given by the formula and reduce

the gas leakage, etc.

As previously indicated, the invention includes a complete system for

introducing and removing solid particles and specific embodiments

thereof now will be described.

Referring to Figure 6, a high pressure vessel in which a destructive

hydrogenation operation is carried out in the presence of a fluidized

hydrogenation catalyst is indicated by numeral 70. A hydrocarbon to be

destructively hydrogenated is introduced in vapor form together with

hydrogen through conduit 72 connected to the lower part of reactor 70

which is at a high pressure for instance of about 10O pounds per

square inch by gauge. The finely divided solid catalyst in reactor 70

is maintained in a fluidized condition by this passage of gas and

vapor and results in destructive hydrogenation of the hydrocarbon

passing into contact with or through it. The converted hydrocarbon

vapors and hydrogen are separated from the solid catalyst particles by

cyclone 74 and then pass from the reactor through conduit 76.

The catalyst particles require regeneration due to accumulation of

colre-like materials thereon. This is accomplished by withdrawing

catalyst and circulating it to a regenerator; at the same time

replacement with fresh catalyst must take place. Catalyst particles to

be regenerated settle into the vertical conduit 78 which is adapted to

form a compact substantially vertical column in accordance with the

principles of this invention. Before the solid particles settle into

the compact column, any hydrocarbon absorbed thereon is removed by a

scavenging gas under high pressure introduced into the top of conduit

78 through conduit 80. Scavenging gas leating through the column is

yented through combination vent and screen 82 and then passes from the

compact column through conduit 84. The compact solid column is

supported by cup 86 in hopper 88 and the solid catalyst is removed

from cup 86 by gas introduced through conduit 90 at a rate controlled

by valve 91. Controller 95 and valve 92 constitute a flow control

safety device to prevent biowout through the column as a result of too

rapid removal of solid particles or other causes. When the flow of gas

through valve 95 becomes excessive it automatically closes controller

92 so that removal of particles from cup 86 ceases. This allows the

column of solid particles to be reestablished. When reestablished, gas

flow through 95 is lowered causing controller 92 to open and gas to

flow through conduit gD.

The catalyst removed from support 86 is suspended in the removing gas

and flows into conduit 94 where it is picked up by a low pressure

transport gas flowing through conduit 96 and is thus conyeyed to low

pressure regenerator 98 which is at a pressure of about 25 pounds per

square inch by gauge. Here the catalyst is regenerated in known manner

by combustion of the contaminating carbonaceous material on the

catalyst. The combustion gas is introduced through conduit 99.

This gas also serves to maintain the catalyst particles in a fluidized

condition. Combustion products are separated from the catalyst

particles by cyclone 100 and then flow from the regenerator through

conduit 1(12. fluidized catalyst in the regenerator accumulates in

vertical conduits 1C4 and 106 provided respectively with vents and

screens 108 and 110 supporting cups 112 and 114 and gas jets 116 and 1

118. These columns operate in accordance with the invention to remove

catalyst from the regenerator and deliver it to catalyst transport

line 117 in the case of vertical conduit 104 and 119 in the case of

vertical conduit 106. Low pressure transport gas conveys this

regenerated catalyst through lines 117 and 119 into vertical conduits

120 and 122 provided respectivelv with vents and solid removal devices

124 and 126 and low pressure gas transport lines 128 and 130. Vents

124 and 126 are pro.

vided with valves 125 and 127 respectively.

These valves are closed during transport of solid particles and are

open when the particles in columns 122 and 120 are in a static or

packed condition.

Transport gas introduced through conduits 128 and 130 at the base of

vertical conduits 120 and 122 serve to break up the compact column in

these conduits and open them up for transport of catalyst

therethrough. Transport gas introduced through conduits 117 and 119

conveys the catalyst particles upwardly through vertical conduits 120

and 122, through the extended loops at the top thereof and thence into

regenerated catalyst hoppers 132 and 1!34 respectively. Transport of

catalyst through vertical conduits 104 and 106 is intended to take

place alternately so that catalyst will be flowing at a substantially

constant rate but will be flowing only into one hopper at any given

time. Assuming that hopper 132 is receiving catalyst from vertical

conduit 104, valve 125 and valve 136 supplying fluidizing gas to

hopper 132 will be closed and valve 137 will be open to vent the gas

present in the fluidized catalyst. The catalyst will be deposited in

hopper 132 and vent gas only will pass through filter 138, conduit 140

and valve 137

While hopper 132 is filling hopper 134 will be filled with a mass of

solid particles and will be operated so as to introduce these solid

particles into reactor 70. This is accomplished by dosing valve 152

and openng valve 142 to bring the pressure in hopper 134 to

approximately the pressure in reactor 70. Valve 142 is then closed.

Fludizing gas is then introduced by opening valve 144 which is

connected to nozzle 148 positioned near the lower end of vertical

conduit 150, the lower end of which terminates below the body of solid

particles of catalyst in hopper 134 and preferably near the base of

hopper 134, as illustrated.

Vertical conduit 150 is provided with a vent 154 which operates in

accordance with the invention. This vent is connected to conduit 150

by a pipe provided with valve 156. This valve is closed during the

introduction operation. The fluidizing gas introduced through nozzle

148 causes the catalyst in the column 150 to break up and to become

fluidized. The fluidizing gas is introduced at a somewhat higher

pressure than exists in reactor 70. Only a small pressure differential

such as about 40 pounds per square inch is required. As a consequence

of this gas introduction the compact solid column of catalyst

particles in vertical conduit 150 breaks up and becomes fluidized and

is transported upward into conduit 158 and thence into reactor 70. At

the same time catalyst in hopper 134 gravitates to the base and is

similarly transported into reactor 70.

When hopper 134 has been about emptied the passage of gas through

nozzle 148 is terrain- ated and the suspension of solid particles in

gas contained in column 150 is permitted to settle to form a compact

column of such length that the vent 154 is effective, as previously

described, i.e., the settled catalyst must occupy sufficient space

above this vent to dissipate the pressure. At this point valves 152

and 156 are opened. The high pressure in reactor 70 is effectively

prevented from passing through conduit 150 by the compact solid column

in conduit 150 in accordance with the principles of the invention.

Hopper 134 is now refilled with catalyst.

This is accomplished by closing valve 127 and introducing transport

gas through conduit 130 at low pressure to break up and fluidize the

compact column in conduit 122. When this is accomplished flow through

conduit 130 is termated and gas flow through conduit 118 is initiated

by opening the valve connected thereto. Fluidized catalyst then flows

through vertical conduit 122 into hopper 134 to again fill it with a

mass of solid particles. When sufficient solid partides have been

transported into 134 the flow of catalyst is terminated by closing

flow through conduits 118 and 119 and opening valve 127. The solid

catalyst in conduit 122 is thus permitted to settle to form a vertical

column of compact solid particles which forms an effective seal

against backilow of gas from hopper 134 during the introduction

operation previously described.

izile the introduction of the contents of hopper 134 into reactor 70

is taking place hopper 132 is fling with solid catalyst to be

subsequently introduced into reactor 70, as indicated previously.

Filling of hopper 132 is accomplished by introducing gas through

conduit 128 at the base of column 120, valve 125 being dosed, to

fluidize the solid particles in the column and then terminating flow

through conduit 128 and initiating flow through conduits 116 and 117

Catalyst is thus removed from column 104 and transported through

conduits 117 and 120 into hopper 132 which retains the solid particles

and vents the gas through conduit 140 and valve 137, as previously

described in connection with hopper 134. When hopper 132 has been

filled the flow of catalyst is terminated by terminating the flow of

transport gas through conduits 116 and 117. The solid particles in

vertical conduit 120 then settle therein to form a vertical compact

column vented at the mid portion by vent 124.

The catalyst in hopper 132 is then intro duced into reactor 70. This

introduction operation is accomplished as described in connection with

hopper 134; i.e., valves 136, 137 and 160 are closed and valves 125

and 172 opened. When hopper 132 reaches about the pressure in reactor

70 valve 172 is closed and valve 136 is opened. The fluidizing gas

flow ing through valve 136 and nozzle 164 causes the catalyst to

become fluidized in vertical conduit 166 and this fluidized catalyst

with the high pressure gas flows through conduit 158 into reactor 70.

Upon termination of this operation valve 136 is dosed and the catalyst

in column 166 is permitted to settle to form a compact vertical

column. Valve 160 is then opened and this causes the compact vertical

column of solids in conduit 166 to act as a pressure seal to prevent

gas from leaking from reactor 70 into hopper 132. Refilling of hopper

132 at low pressure is then re-started. In the interim hopper 134 has

been refilled and emptying into reactor 70 is started.

It is to be noted that when hoppers 132 and 134 are pressured up

through valves 142 and 172 backilow of high pressure gas through lines

120 or 122 is prevented by the compact vented columns of solid

particles in lines 120 and 122. Similar backflow from lines 117 and

119 into regenerator 98 during flow of gas from lines 128 and 130 is

prevented by vented compact vertical columns of solid particles in

conduits 104 and 106. These last mentioned columns need not have as

great a height because the pressure differential is much smaller.

It is thus possible to continuously remove catalyst from high pressure

reactor 70, to continuously regenerate it at a low pressure, such as

about atmospheric pressure, and to then continuously introduce it back

into the reactor 70. Although the introduction through hoppers 132 and

134 takes place intermittently they are complementary so that

introduction is continuous.

It will be noted that vertical conduits 120, 122, 150 and 166 are of

unusual length and necessitate loops to return the elevated catalyst

to the hoppers or reactors as the case may be.

This is necessary in the embodiment illustrated in Figure 6 in order

to have sufficient catalyst in the vertical conduit to form a seal

against backflow of gas when the solids settle into a compact column.

It is this factor which determines the height of the vertical conduit.

It will be evident that when the lower part of these vertical conduits

contains a compact column of solid particles the top of this compact

column should be at a sufficient distanoe above the vent that the gas

and solid particle pressure will be dissipated as previously

described.

The necessity for such high vertical columns for charging catalyst

into the introduction hopper is avoided by the apparatus illustrated

in Figure 7. Referring to this figure, numeral 180 designates a high

pressure reactor containing a fluidized bed of catalyst particles.

Numeral 182 designates a vertical conduit pro- vided with a vent and

solid removal means 184. Numeral 186 designates a conduit connected to

the lower end of vertical conduit 182 and to the upper part of a low

pressure regenerator 188. Numeral 190 indicates a vertical conduit

provided with a vent and solid filter means 192, the lower end of

which conduit is connected with a conduit 194 which leads to hopper

196. Hopper 196 is provided with a vertical conduit 198, valve 200 and

vent and solid filter means 202. Numeral 204 designates means for

introducing fluidizing gas into hopper 196.

During operation of is apparatus a reaction such as destructive

hydrogenation of a hydrocarbon in the presence of a fluidized

hydrogenation catalyst is carried out in known manner in reactor 180.

Solid catalyst particles in reactor 180 settle into vertical column

182 continuously. These solid particles are continuously removed by

low pressure transport gas passing through conduit 186 and are thus

conveyed into low pressure regenerator 188 where they become

regenerated. Leakage of high pressure gas from reactor 180 is

prevented by maintaining a compact column of catalyst particles in

conduit 182 at all times and venting through 184 which is proyided

with a solid particle filter.

The solid particles in regenerator 188 accumulate in vertical column

190 and are partially removed therefrom intermittently by intermittent

passage of low pressure transport gas through conduit 194. When hopper

196 contains the required amount of solid particles, passage of solid

particles is terminated by closing the valve connected to conduit 194.

Hopper 196 is then pressured up to approximately the pressure existing

in reactor 180 and high pressure transport gas is introduced through

conduit 204 into the lower portion of hopper 196. Valve 200 is closed

and as a consequence the compact column in 198 is fluidized and

conveyed by the high pressure gas flowing from conduit 24 into reactor

180.

This transport operation is then terminated by closing the valve on

conduit 204. The catalyst in vertical conduit 198 settles to form a

compact solid and valve 200 is opened. At this stage the compact

column 198 acts as a pressure seal between hopper 196 and reactor 180.

While high pressure exists in hopper 196 during the period that

catalyst is flowing therefrom into reactor 180 leakage of this gas

into regenerator 188 is prevented by the valve action of the compact

column of solid particles in vertical conduit 190. Thus the high

pressure in 196 is exerted through conduit 194 against the base of

vertical conduit 190 but this gas and the high pressure is. dispersed

through vent 192 and against the walls of the vertical conduit as

previously described.

The operation of the apparatus illustrated in

Figure 7 would be intermittent. However, by providing a plurality of

hoppers as illustrated in Figure 6 operation could be made continuous.

It will be noted that the base of vertical columns 120 and 122 in

Figure 6 and the base of vertical columns 182 and 190 in Figure 7 do

not necessitate any particular supporting means for the column of

solid. It has been found that an ordinary pipe elbow or T will be

sufficient to retain a pile of catalyst which will act as a support

for the column above it.

When transport gas is passed through this elbow or T the pile of

catalyst is transported away and consequently in the case of columns

182 and 190 the compact solid starts to flow from the column into the

transport gas and is thus further removed until termination of flow of

the transport gas. The gas used to introduce catalyst through vertical

conduits 150 and 166 of Figure 6 and conduit 198 of Figure 7 should

preferably be one which is used in the reaction. In this instance

hydrogen would be advantagersus. In any event the gas should be one

which will not interfere viith the reaction in the reactor. A normally

gaseous substance need not be used. A vapor is satisfactory if the

temperature oE the column, etc., is above the boiling point.

While the apparatus illustrated in Figure 7 eliminates only the use ol

long introduction conduits for charging into the hopper, the use of

long introduction conduits for charging into the reactor can also be

avoided. Thus vertical conduit 198 can be connected to reactor 180 at

a point which is below the expanded bed level of catalyst in reactor

180 to allow conduit 198 to fill with catalyst from the reactor at the

time the upward flow of catalyst is discontinued. In the absence of

such a mo ifi- cation conduit l98 should be of sfflcient height to

hold enough expanded catalyst to form a compact column seal when the

caLalyst therein is permitted to settle.

Bleed gas from the vents of the vertical columns can be collected and

reused. For instance, if the bleed gas from the column connected to

the reactor contains hydrogen it can be collected and reused by

pumping back into the high pressure reactor. The specific construction

illustrated in Figure 2 would permit this, i.e., conduits 42 could be

connected to a suitable storage system from which the vented gas could

be withdrawn for reuse.

The catalyst in locks 132 and 134 of Figure 6 and in lock 196 of

Figure 7 is not in an aerated state during the time that the high

pressure fluidizing gas is introduced at the base. This gas flows

upwardly through the column and aerates the solid particles in the

column only. It would appear that brealiing up of a compact column of

particles after it had been subjected to a high pressure at one end

and a low pressure at the other end would be a difficult problem.

Actually no difficulty is encountered in this connection. As soon as

the pressure in the hopper approximates that in the reactor the

introduction of the gas at the base of the column causes the column to

break up into a fluidized condition which is readily transported. When

this has taken place the pile of catalyst in the hopper falls down

into the gas stream flowing up the vertical column and is transported

with it.

It will be apparent that the invention has wider application than in

the specific operations described. For instance it is of value in

connection with fluidized catalytic cracking of petroleum products,

fluidized hydroforming of petroleum products and the synthesis of

hydrocarbons from carbon monoxide and hydrogen using a fluidized

catalyst. Destructive hydrogenation of powered coal or

hydrodesulfurization of powdered coal may also be carried out

utilizing this invention to introduce the coal powder and remove the

ash or residue. This invention is also applicable to non-catalytic

operations such as the coking of coal and the adsorption of gases or

vapors on a solid adsorbent at elevated pressure followed by

desorbtion at lower pressure.

The apparatus illustrated in Figure 8 and its operation can best be

described in connection with a destructive hydrogenation of a

hydrocarbon ai an elevated pressure in the presence of a fluidized

hydrogenation catalyst of small particle size. tn this operation

catalyst gradually becomes inactive due to deposition of tar and coke

thereon and it is desirable to remove the catalyst from the reactor,

regener ate it by burning a tne tar and coke at a lower pressure, such

as armospheric pressure, and return the regenerated catalyst to the

high pressure reactor. The apparatus includes a high pressure chamber

206 in which destruc tive hydrogenation of a hydrocarbon oil is

carried out in the presence of a fluidized catalyst. The hydrogen and

hydrocarbon vapors to be destructively hydrogenated are introduced

into the base of the reactor through conduit 208. The reactor is

partially filled witn a mass of the hydrogenation catalyst The

hydrogen and hydrocarbon vapors pass upwardly through the catalyst and

cause the catalyst particles to be suspended therein as in

conventional fluidized operation. The hydrogen and reaction products

are separated from the catalyst particles by cyclone 210 and the

hydrogen and reaction products flow from the reactor through conduit

212.

Fluidized catalyst settles by gravity into the top of vertical conduit

14 and is purged with hydrogen introduced through conduit 216. The

purged catalyst then settles in vertical conduit 214 to form a compact

column.

This column is vented in accordance with the invention, by vent 218.

Catalyst is intermittently or continuously removed from the base of

vertical conduit 214 by low pressure transport gas introduced through

conduit 220 at a rate controlled by valve 222.

This catalyst is gradually or slowly removed from the base or the

compact column by the gas stream and transported through conduits 220

and 221 into lower pressure chamber 224 which, in the case under

consideration, is a regenerator operating at about atmospheric

pressure. The catalyst is regenerated therein by suitable combustion

gas introduced through conduit 226. This gas maintains the catalyst in

the regenerator in a fluidized condition during the regeneration.

Catalyst particles are separated from the combustion gases by cyclone

228 and the combustion gases then flow from the regenerator through

conduit 230.

Regenerated catalyst settles in the upper part of vertical conduit

232. As the catalyst settles it is purged with steam or inert gas

introduced through conduit 234 and then settles in conduit 232 in the

form of a compact column. This column is vented by combination vent

and solid particle filter 236 in accordance with the principles

described above. The catalyst in conduit 232 is intermittently removed

from the lower end thereof by low pressure transport gas introduced

through conduit 238 at a rate controlled by valve 240. This removed

catalyst passes upwardly through conduit 242 into hopper 244.

Hopper 244 is provided with a conduit 246 which is provided with

cyclone 247 and valve 248. Numeral 250 designates a vertical conduit

connected to hopper 244 which conduit is provided with a vent 252 and

valve 253. The lower part of vertical conduit 250 terminates in line

254 for introduction of high pressure transport gas at a rate

controlled by valve 256.

Conduit 254 communicates with high pressure reactor 206.

The manner in which catalyst is removed from high pressure chamber 206

and introduced into low pressure chamber 224 is evident from the

foregoing description. Catalyst in low pressure chamber 224 is

introduced into high pressure chamber 206 by opening valve 240 to

transport catalyst from the base of vertical column 232 into hopper

244 until it is filled with a mass of settled or quiescent catalyst

particles. During this operation valve 248 is opened to permit egress

of the transport gas. When hopper 244 has been filled valve 240 is

closed and the catalyst in vertical column 232 assumes a static

compact column condition. Gas under high pressure then is introduced

through conduit 246 into hopper 244 until the pressure therein

approximates the pressure in high pressure reactor 206. Valve 248 is

closed and valve 256 is opened and gas under a somewhat higher

pressure than exists in reactor 206 is introduced through conduit 254

to remove catalyst from the base of vertical conduit 250 and transport

it into reactor 206. Valve 253 is closed during this stage of the

operation. This gas passes out of the reactor 206 through conduit 212

with the reaction products and hydrogen. It is preferably hydrogen so

as to avoid contamination of the hydrogen used in reactor 206. The

catalyst in hopper 244 settles in vertical column 250 at a rate

corresponding to the rate of removal from the base thereof. During

this operation the high pressure in hopper 244 is prevented from

blowing back into regenerator 224 by the sealing effect of the compact

column of catalyst in vertical conduit 232, i.e., the high pressure at

the base of conduit 232 is dissipated through vent 236 as described

preivously.

When the transfer of catalyst from hopper 244 into reactor 206 has

been substantially completed it is terminated by closing valve 256 and

opening valve 248 to the atmosphere or to a pressure approximating the

pressure in regenerator 224 after opening valve 253 connected to vent

252. Valve 240 then is opened again to transport catalyst from verti-

cal column 232 into hopper 244 as previously described. It is to be

noted that emptying of hopper 244 should be terminated while vertical

conduit 250 is still filled with a compact column of catalyst so that

it will prevent bacltilow of gas from reactor 206 into hopper 244 when

hopper 244 is at low pressure and being filled.

The operation of the apparatus illustrated in Fig. 8 is necessarily

intermittent. However, it is possible to obtain approximately or

completely continuous operation by utilizing a plurality of hoppers

instead of a single hopper and emptying one of the hoppers into

reactor 206 while other hopper or hoppers are being filled from

regenerator 224 or being pressured up, etc. The utilization of a pair

of hoppers alternately in this manner is described in the

above-mentioned application.

Three hoppers would allow the most desirable time cycle. Each

additional hopper would require an additional feed column similar to

column 232 and of course an additional introduction column similar to

column 250.

It will be noted that the base of vertical conduits 214, 232 and 250

do not necessitate any particular supporting means for the column of

solid. While the supporting and removing means specifically described

in Figs. 1, 3 and 4 can be used at the base of these columns it has

been found that an ordinary pipe elbow or T will be sufficient to

retain a pile of catalyst which will act as a support for the column

above it When transport gas is passed through this elbow or T the pile

of catalyst is transported away and consequently the corn pact solid

starts to flow into the transport gas and is thus further removed

until termination of flow of the transport gas. The gas used for

transport of catalyst should be one which will not interfere with the

reaction in the reactor. A normally gaseous substance need not be

used. A vapor is satisfactory if the tem- perature of the column etc.,

is above the boiling point.

Also it will be noted that vertical conduits 232 and 250 of Fig. 8

operate on the same basic principles as vertical conduits 214, of

Fig. 8, and 18, Fig. 1, that is, the principle of venting most of the

gas at some point intermediate the ends of the vertical column rather

than allowing most of the gas to flow completely through the column is

the same in each case. However, conduits 232 and 250, Fig 8, involve

the additional discovery that the low pressure end of the column

(upper end) need not be ernersed in a bed of rigidly supported

catalyst to avoid upward catalyst flow provided that the gravity

effect of the body of catalyst above the vent is sufficient to offset

the static gas pressure existing at the vent.

This static gas pressure is determined by the pressure drop through

the vent.

Bleed gas from the vents of the vertical columns can be collected and

reused. For instance, if the bleed gas from the column connected to

the reactor contains hydrogen it can be collected and reused by

pumping back into high pressure reactor. The specific construe tion

illustrated in Fig. 2 would permit this, i.e., conduits 42 could be

connected to a suitable storage system from which the vented gas could

be withdrawn for reuse.

It will be apparent that the invention has wider application than in

the specific op era- tions described. For instance it is of value in

connection with fluidized catalytic cracking of petroleum products,

fluidized hydroforming of petroleum products and the synthesis of

bydrocarbons from carbon monoxide and hydrogen using a fluidized

catalyst Destructive hydrogenation of powdered coal or

hydrodesulfurization of powdered coal may also be carried out

utilizing the invention to introduce the coal powder and remove the

ash or residue. The invention is also applicable to noncatalytic

operations such as the coking of coal and the adsorption of gases or

vapors on a solid adsorbent at elevated pressure followed by

desorption at lower pressure.

What we claim is:

1. Apparatus for use in effecting a substantially gas-tight seat

between spaced zones between which there exists a pressure

differential and which are in intercommunication for the transference

of solid particles therebetween comprising conduit means

interconnecting said zones and providing said intercommunication, at

least a length of said conduit means being substantially vertical,

supporting means at or below the lower end of said conduit length

adapted to support solid particles to establish a compact column of

solid partides within said conduit length, at least one gas vent

communicating with said conduit length intermediate the ends thereof,

means associated with said vent to prevent substantial flow of solid

particles through the vent, and means for controlling the flow of

solid particles through said conduit length.

2. Apparatus as claimed in Claim 1, in which said flow-controlling

means comprises controlled gas inlet means adjacent said supporting

means for the introduction of gas to disperse solid particles from

said supporting means thereby to allow solid particles to flow from

said conduit length.

3. Apparatus as claimed in Claim 1, in which said flow-controlling

means comprises screw means for effecting vertical adjustment of said

supporting means.

4. Apparatus as claimed in Claim 1, in which said supporting means

comprises a receptacle for solid particles communicating with the

lower end of said conduit length and having an outlet conduit, the

flow of solid particles through said outlet conduit being controlled

by sliding valve means provided therein.

5. Apparatus as claimed in Claim I, in which the supporting means

comprises a gas conduit branching from the lower end of said conduit

length to feed transport gas to or across said lower end and valve

means is pTb vided in said gas conduit to control the transport gas

flow and thus the flow of solid particles through said conduit length.

-6. Apparatus as claimed in Claim 1 or 5, in which means is provided

for effecting intermittent transference of solid particles through

said conduit length, valve means being provided for closing the gas

vent effectively to break the gas-tight seal during the transference

periods.

7. Apparatus as claimed in Claim 1, when used for effecting a

substantially gas-tight seal between each of the components of a

system comprising a high pressure chamber, a low pressure chamber and

at least one hopper for introducing solid particles into said high

pressure chamber.

8. Apparatus as claimed in Claim 7, in which the hopper communicates

with both of said chambers, means is provided for alternately feeding

so

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* GB785367 (A)

Description: GB785367 (A) ? 1957-10-30

Improvements in or relating to disc brakes

Description of GB785367 (A)

PATENT SPECIFICATION

Inventor: LEONARD REDMAYNE 785,367 Date of filing Complete

Specification: Sept 6, 1955.

Application Date: Sept 7, 1954 No.25887154 Complete Specification

Published: Oct301957.

Index at acceptance:-Class 103 ( 1), E 2 NIA( 1: 2: 4 A 1: 5: 6 A), E

2 NICI, E 2 N 1 D( 2 B: 6 A: 6 B: 6 C 1:

6 C 3).

International Chassification:-F 06 d.

COMPLETE SPECIFICATION

Improvements in or relating to Disc Brakes We, GIRLING LIMITED, a

British Company, of Kings Road, Tyseley, Birmingham 11, do hereby

declare the invention, for which we pray that a patent may be granted

to us, and the method by which it is to be performed, to be

particularly described in and by the following statement: -

This invention relates to improvements in disc brakes and refers more

particularly to a disc brake which is intended for use on aircraft

wheels but is also applicable to other vehicles.

In a disc brake according to our invention a flat brake ring mounted

on or in a wheel is straddled from the inside by a U-shaped housing

mounted on a stationary part adjacent to the wheel and friction pads

which are adapted to be urged into engagement with opposite faces of

the brake ring by a piston or pistons working in an hydraulic cylinder

or cylinders located in one limb of the housing are keyed to flat

backing plates which are of substantially greater length in a

circumferential direction than the pads, and there is formed in each

backing plate at each end thereof a semi-circular recess engaging

slidably with a corresponding torque-taking pin removably mounted in

the housing with its axis parallel to the axis of the brake ring.

These pins can be inserted after the brake is assembled so that the

pads and their backing plates can be fitted into the housing from the

outer side, and assembly and maintenance are considerably facilitated.

When the friction pads are worn and have to be replaced the wheel is

removed, the torque-taking pins are withdrawn, and the worn pads and

their backing plates are withdrawn radially outwardly from the

housing, new pads are fitted, and the pins are replaced.

The friction pads preferably have the form of segments of a ring of

substantially the same diameter and radial width as the brake ring.

If the friction pads are applied by a piston fr.ce >' or pistons

working in an hydraulic cylinder or cylinders in one limb only of the

housing the brake ring may be splined or otherwise slidably keyed at

its outer edge to a wheel, 50 one pad being applied to one face of the

ring by the piston or pistons of the hydraulic cylinder or cylinders

and the other pad being mounted on the inner face of the opposite limb

55 If there are two or more brake rings further friction pads will be

arranged between the rings.

There may be two or more angularly spaced brake assemblies operating

on the O same brake rings.

A practical brake in accordance with our invention for an aeroplane

wheel is illustrated by way of example in the accompanying drawings in

which: 63 Figure 1 is a longitudinal section of the wheel and brake on

the line 1-1 of Figure 2.

Figure 2 is an end view of the brake with a portion of one brake

housing or caliper in section on the line 2-2 of Figure 1 T O Figure 3

is a fragmentary view of one caliper looking in the direction of the

arrow A in Figure 2, the brake rings being omitted.

In Figure 1 10 is an aeroplane wheel mounted to rotate on spaced ball

bearings 11, 7 i 12 on a stationary hollow shaft 13 The internal

surface of the wheel rim at one end is formed with angularly spaced

axially extending splines 14 with which engage complementary notches

15 in the peripheral 80 edges of two flat brake rings or discs 16, 17

so that the rings, are slidably keyed in an axial direction to the rim

The splines 14 may be formed by steel bars or strips of rectangular

cross section secured by rivets to the wheel 85 rim as shown at the

bottom of Figure 1.

A housing or caliper 18 of U outline which may be a casting or forging

straddles the brake rings from the inside and has at one point an

integral inwardly projecting arcuate 90 flange 19 which is secured by

bolts 20 to a member 21 fixed on the shaft 13.

Kmrf One limb of the housing is extended and bored to form an

hydraulic cylinder 22 in which works a piston 23 The outer end of the

bore is closed by two discs 24 having peripheral O ring seals 25, the

discs being retained by a spring ring or circlip 26 located in an

annular groove in the bore.

A friction pad 27 carried by a backing plate 28 is located between the

piston 23 and the adjacent brake ring 17 and a similar pad carried by

a backing plate is located between the other ring 16 and a flat

abutment face on the other limb of the housing Two friction pads 29

are located between the rings and are mounted on opposite faces of a

common backing plate 30 The friction pads may simply be bonded to the

backing plates but preferably each pad has on its face remote from the

brake ring a spigot portion 31 which is received in a recess in the

backing plate.

Each backing plate is of a considerably greater length in the

circumferential direction than the friction pads and is of the outline

shown in Figure 2 The plate has at each end an inwardly projecting

horn 32 which fits over a complementary portion 33 of the housing and

has in its inside edee a semicircular notch engaging slidably with the

outer side of a pin 34 mounted in the housing These pins are parallel

to the axis of the wheel and are located axially by circlips received

in annular grooves in the ends of the pins which project from the

housing.

When the brake is applied the piston 23 forces the friction pad 27

with which it engages against the adjacent brake ring 17 which moves

axially on the splines in the wheel and through the pads 29 urges the

other brake ring 16 against the other end pad 27 which in turn is

urged against the inner face of the other limb of the housing, so that

each brake ring is gripped between two friction pads.

The torque on the friction pads is taken through the backing plates by

the pins 34.

The major part of the torque will be taken by one or other of the pins

according to the direction of rotation of the wheel, the other pin

taking any part of the torque tending to cause angular movement of the

backing plates about the first pin.

It will be appreciated that in the construction illustrated there are

two diametrically opposed brake assemblies operating on the same brake

rings but as the two assemblies are identical only one has been

described.

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