CA1251198A - Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type - Google Patents
Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous typeInfo
- Publication number
- CA1251198A CA1251198A CA000548066A CA548066A CA1251198A CA 1251198 A CA1251198 A CA 1251198A CA 000548066 A CA000548066 A CA 000548066A CA 548066 A CA548066 A CA 548066A CA 1251198 A CA1251198 A CA 1251198A
- Authority
- CA
- Canada
- Prior art keywords
- lower chamber
- chamber
- fluid medium
- return tube
- granular mass
- 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.)
- Expired
Links
- 238000001311 chemical methods and process Methods 0.000 title claims abstract description 7
- 239000012530 fluid Substances 0.000 claims abstract description 85
- 238000009826 distribution Methods 0.000 claims abstract description 50
- 238000000034 method Methods 0.000 claims description 16
- 230000008569 process Effects 0.000 claims description 11
- 239000008187 granular material Substances 0.000 abstract description 23
- 239000000463 material Substances 0.000 abstract description 5
- 238000013461 design Methods 0.000 abstract description 4
- 239000007787 solid Substances 0.000 abstract description 2
- 238000012546 transfer Methods 0.000 abstract description 2
- 239000002245 particle Substances 0.000 abstract 1
- 238000007790 scraping Methods 0.000 description 6
- 238000010276 construction Methods 0.000 description 5
- 230000002411 adverse Effects 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 4
- 238000005452 bending Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 125000006850 spacer group Chemical group 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D13/00—Heat-exchange apparatus using a fluidised bed
-
- G—PHYSICS
- G01—MEASURING; TESTING
- G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
- G01N33/00—Investigating or analysing materials by specific methods not covered by groups G01N1/00 - G01N31/00
- G01N33/0091—Powders
Landscapes
- Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Physics & Mathematics (AREA)
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Food Science & Technology (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- Medicinal Chemistry (AREA)
- Analytical Chemistry (AREA)
- Biochemistry (AREA)
- General Health & Medical Sciences (AREA)
- General Physics & Mathematics (AREA)
- Immunology (AREA)
- Pathology (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
A B S T R A C T
This invention relates to apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger (10) of the continuous type, comprising a large number of vertical heat exchanger tubes (18)mounted between a lower chamber (17) and an upper chamber (16) within a jacket (15) Within the tubes (18) small solid particles are kept in a fluidized condition by the fluid medium passing up from the lower chamber (17) through the tubes (18), so as to achieve a good heat transfer, whereas also any deposit will be removed from the inner tube walls. For the downward flow of the granular mass at least one return tube (21) is provided. Downward circulation of the fluid medium through the return tube (21) should be minimal, however, which can be achieved by an increase of the pressure difference between the upper and lower chamber (16; 17), which increase of the pressure difference can be achieved by fitting several distribution plates (24; 42) at a level above the return tube (21) outlet into the lower chamber (17), preferably so that the apertures in the various distribution plates (24; 42) of the multiple design are not vertically in line.
The second distribution plate (42) also serves to minimise excessive wear of the material of the jacket (15) due to the eddying motion of the granules.
This invention relates to apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger (10) of the continuous type, comprising a large number of vertical heat exchanger tubes (18)mounted between a lower chamber (17) and an upper chamber (16) within a jacket (15) Within the tubes (18) small solid particles are kept in a fluidized condition by the fluid medium passing up from the lower chamber (17) through the tubes (18), so as to achieve a good heat transfer, whereas also any deposit will be removed from the inner tube walls. For the downward flow of the granular mass at least one return tube (21) is provided. Downward circulation of the fluid medium through the return tube (21) should be minimal, however, which can be achieved by an increase of the pressure difference between the upper and lower chamber (16; 17), which increase of the pressure difference can be achieved by fitting several distribution plates (24; 42) at a level above the return tube (21) outlet into the lower chamber (17), preferably so that the apertures in the various distribution plates (24; 42) of the multiple design are not vertically in line.
The second distribution plate (42) also serves to minimise excessive wear of the material of the jacket (15) due to the eddying motion of the granules.
Description
5~
This is a division of Canadian Application No. 458,992 filed July 16, 1984.
The invention relates to apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type, comprising a bundle of parallel vertical riser tubes, an upper chamber, a lower chamber, upper and lower tube plates for open connection of the tube bundle with the upper and lower chambers respectively, a granular mass that can be kept in a fluidised condition, at least in the riser tubes, by a fluid medium flowing during operation upwardly through the lower chamber, the riser tubes and the upper chamber, a distribution pla-te for the granular mass in the lower chamber, and at least one return tube opening below the distribution plate for return of an overflow of granulax mass above the upper tube plate from the upper chamber to the lower chamber, wherein each riser tube is provided with an inflow element extending in the lower chamber, from the lower tube plate to a level above the distri-bution plate through which the return tube or return tubes projects or project, and wherein the lower chamber is provided with a device which prevents granules from reaching the lower chamber inlet for the fluid medium during standstill.
'~2~
An apparatus of this type is known from an article by D. G. Klaren in "Fouling Prevention Research Digest", Vol.
5, No. 1 pp. III-XVII (March 1983). The known heat exchanger that because of the presence of the fluidised bed has a high efficiency as a result of breakage of the fluid film along the inner surface of the riser tubes is primarily of interest, if, from the fluid medium on the inner surface of the riser tubes, a layer of material can be deposited that impedes heat transfer through the riser tube walls. This impeding layer is not deposited in the known apparatus due to the abrasive action of the granules. Therefore the known apparatus is ideal for application iJl e.g. the food industry.
On the other hand the presence of the granular mass brings its disadvantages. One disadvantage of the ~nown apparatus is that it is never completely certain that the downward flow of the granular mass will occur only in the return tube or the return tubes that are intended for the purpose. To achieve a correct desiqn and to ensure an even distribution of both the fluid medium and the granular mass across all riser tubes it is of utmost importance that only tubes that are intended for the purpose serve as return tubes. The situation where one or more riser tubes will still start to function as return tubes can occur in particular if insufficient care is exercised at start-up of the heat exchangerO It is then possible that the fluidised granules inside several riser tubes reach the top enas thereof earlier th2n the granules in other riser tubes, 5~
which causes the granules issuing from the former riser tubes to flow through the upper chamber into the adjoining riser tubes that are not yet completely filled with fluidised granules.
The result is disturbance of the pressure balance between the various tubes causing a downward flow of fluid medium and granules into one or several tubes that were not originally intended for such a downward flow.
The invention eliminates this first objection by means of a constriction at the ends of the riser tubes that open into the u?per chamber.
In this constriction the velocity of the fluid medium is increased to such an extent that the granules cannot drop from the upper chamber back into a riser tube. With the constriction correctly dimensioned, even a high irregular distribution of the granular mass across the riser tubes w th startup of the heat exchanger cannot cause one or several riser tubes to start acting as return tubes.
An advantageous construction of the apparatus is characterised by an upper pipe plate ?rovided with apertures for the riser tibes having smaller cross-sections than the riser tubes themselves.
The sranular mass circulates in the upward direction through the riser tubes and in the downward direction through the return tube. During this circulation, particularly in operation, sranules are in eddying motion also in the lower chamber tha. apparently are the source of very severe wear of the heat exchanger jacket, especially of the material at the junction of the bottom cover and the cylindrical wall which ~i 2rj'~ B
forms part of the shell.
The second disadvantage is eliminated according to the invention by means of a second distribution plate arranged in the lower chamber at a level below the outlet therein of the return tu`be.
In this proposed construction, in contrast with the known apparatus, the device that impedes the granules from reachins, at standstill, the inlet for the fluid medium in the lower chamber cannot serve as a shutoff valve against the lower eàge of the return tube. Consequently under all conditions a downward flow of the fluid medium will occur inside the return tube which, in the construction proposed, can amount to approx.
25 per cent of the fluid medium mass flow supplied to the heat exchanger inlet. As the result the average logarithmic temperature difference inside the riser tubes will be less favourable which requires that, to achieve a desired efficiency, a larger heated surface must be installed.
Tne last requirement can be obviated to a certain degree according to the invention by constructing the distribution plate at a level above the return tube outlet into the lower chamber in multiple; preferably so that the apertures in the various distribution plates of the multiple construction are not vertically in line.
It appears that the downward flow of the fluid medium throush the return tube or the return tubes can thus be limited to about 15 per cent of the mass flow through the heat exchanger inlet.
.
The absence of any moving parts in the ~ower chamber, i.e. of the provision as a valve of the device that prevents granules from -eaching, at standstill, the fluid medium inlet into the lower chamber, and ,he reduced wear of lower chamber parts of~set the disadvantage of fluid medium circulation through the return tube.
To stabilise the fluidised bed in a riser tube it has been suggested to provide the inflow pipe element with a lateral bore at a level where, during operation, no granules are present in the lower chamber, i.e. where only the fluid medium is present. If stroncly contaminating fluid media are used, e.g. fluid media that carry solids, the lateral bore may get clogged causing the fluidised bed in the riser tube to sag and finally causing the unintended functioning as a return tube of the riser tube, which must be defined as objectionable.
In a method of operation of apparatus of the type described at the outset, this last disadvantage is avoided by temporarily reducing the pressure of the fluid medium at the top of the lower chamber.
According to the invention, the apparatus of the type àescribed at the outset is thereby characterised by lateral bores provided in the inflow pipe elements. The top of the lower chamber above the level of the lateral bores is fitted with an outlet with shutoff valve.
In particular the apparatus according to the invention is characterised in that the outlet at the top of the lower chamber is directly connected with a fluid medium outlet of the upper chamber.
The presence of a return tube or of return tubes has the associated disadvantage of causing displacement of the fluid medium from the upper chamber to the lower chamber.
Although the granular mass flow inside the return tube will under some conditions stagnate and as it were clog up the return tube, in that case the intended average logarithmic temperature difference between the outer and inner surfaces of the riser tubes reguired for proper functioning of the heat exchanger will be adversely affecte2, unless by chance an operating point is found where this is not the case. However, such an operating point will entail undesirable restrictions and limitations of other operating parameters.
To be able at least to reduce this adverse effect the apparatus of the type described at the outset is character-ised by 2 bypass between the inlet for the fluid medium used in the process in the lower chamber and a point in the upper chamber where the bypass opens into the upper chamber at the level of the inlet opening of the return tube or 'ubes.
Thus the bypass, which is preferably fitted with an adjustable valve to control the flow through it, will at least partly eliminate the temperature difference be~ween the upper and the lower chambers.
7~
According to the invention another solution of the same problem is provided in that a throttle device is located before the inlet opening of the return tube, which gives precedence to passage through the return tube to the fluid medium over that of the granu]ar mass.
If the quantity of granular mass inside the return tube is thus limited less driving power will be available for circulation, which will cause reduced circulation through the return tube of granular mass and fluid medium.
Fouling can also occur on the outer wall of the riser tubes due to the nature of the second fluid medium used in the heat exchanging process. This particular problem relates to a more general class of heat exchangers, i.e. of the type where the second fluid medium that is used in the heat exchanging process is a fluid that, like a film, flows down the vertical riser tubes of apparatus for carrying out physical and/or chemical processes, more in particular a heat exchanger of the continuous type, consisting of a bundle of parallel vertical riser tubes, an upper chamber, a lower chamber, an upper pipe pla~e and a lower pipe plate for open connection of the pipe bundle with the upper and lower chambers, respectively, all for throughf]ow of the first fluid mediu~ and an upper distribution chamber and a lower collecting chamber for throughflow of the second fluid medium, the upper distribution chamber closing around each riser tube leaving a gap in the bottorn of the upper distribution chamber around each riser tube and the top of the lower collecting chamber being provided with collecting apertures around each riser tube.
S~ch apparatus is known from the article by D. G. Klaren in "Fouling Prevention Research Digest", Vol.
5, No. 1, pp. III-XVII (~arch 1983).
If the temperature and pressure occurring do not require that the fluid that is the second fluid medium is enclosed by a fixed jacket wall, the tubes can be easily cleaned from the outside, e.g. by washing down the pipe bunldes which may be done during operation. However, if a very strongly fouling fluid is used as the second fluid medium in the heat exchanging process the bund~es must be washed down so frequently that this is not practicable. Even if the process temperature and pressure do require that the second fluid medium is enclosed by a fixed jacket wall, this method for pipe bundle washing is out of the question. According to the invention optimal methods for cleaning the outer surfaces of the riser tubes are provided, in that all tubes have been fitted on the outside with a scraping device in a supporting construction that can be driven mechanically.
The scraping device of this type cannot reach the gaps in the bottom of the upper distribution chamber that may get clogged due to fouling.
To prevent the gaps from thus clogging up, or to at least delay the clogging process, the upper distribution chamber is provided, above its bottom, with a distribution shell that has apertures for distribution of the fluid over the saps in the bottom.
Thus the gaps in the bottom can be wider without substan,ially increasing the height of the upper distribution chamber.
_9_ ~5~9~
The invention in all its aspects wil] b~ illustra~ed below with a description referring to a plan. In the plan Fig. 1 shows an embodiment of a first aspect of the invention;
Figs. 2 and 3 show embodiments of the invention according to a second aspect;
Figs. 4 and 5 show embodiments of the i~vention according to a third aspect;
Fig. 6 shows an embodiment of the invention according to a fourth aspect;
Figs. 7 and 8 show an embodiment of the invention according to a fifth aspect;
Figs. 9 and 10 show an embodiment of the invention according to a sixth aspect; and Figs. 11 and 12 show an embodiment of the invention according to a seventh aspect.
Fig. 1 shows an embodiment of the apparatus according to the first aspect of the invention. The heat exchanber 10 has, for a first fluid medium, an inlet 11 and an outlet 12 and, for a second fluid medium, an inlet 13 and an outlet 19.
Inside the jacket 15 a lower chamber 17 connects to the inlet 11 and an upper chamber 16 connects to the outlet 12. A riser tube bundle 18 is arranged between an upper pipe plate 19 and a lower pipe plate 20, the riser tube bun~le including a return tube 21. The riser tubes are provided with inflow pipe elements 22 that extend from the lower pipe plate 20 downwardly into the lower chamber 17. The inflow pipe elements - - 1 0~
are provided with lateral bores 23. In the lower chamber 17-a distribution plate 24 is located below the inlets of the riser tubes and above the outlet of the return tube. The lower chamber 17 is further provided with a device 25 that prevents the granules in the lower chamber, the riser tubes, the upper chamber and the return tube from reaching the inlet 11. The device 25 is mounted on a spring assembly 26 which, at standstill, presses the device 25 against the outlet aper'ure of the return tube. In any case the granules can be brought into the fluidised bed condition in the riser tubes 18. The lower end of the return tube 21 will contain a stagnating granular mass 27.
According to the invention the upper pipe plate 19 of the heat exchanger 10 is provided with throttling apertures 32 via which the riser tubes 18 open into the upper chamber 16. For instance the apertures 32 are provided in a throttle plate 31 constituting, within the assembly, an integral part of the upper pipe plate 19 and not forming an obstacle for the return tube 21.
It will be obvious that the throttling apertures 32 in the outlets of the riser tubes 18 are effective to prevent granules from dropping into the riser tubes from the upper pipe plate independently of the valve action of the device 25.
Figs. 2 and 3 show embodiments of the invention according to a second aspect. The desig~ of the apparatus in these embodiments corresponds in most respects with that sho~n in Fig. 1. To prevent the material of the jac~et, 5~g8 particularly at the junction of the bottom cover 43 to the cylindrical wall 44, from being excessively worn due to the eddying motion of the granules constituting the material of the fluidised beds in the riser tubes, a second distribution plat. 92 is proviaed in the lower chamber 17 at a level below the outlet in the lower chamber 17 of the return tube 21.
The device that prevents granules from reaching, at standstill, the inlet 11 in the lower chamber 17 is provided as a simple bell ~1 which is mounted fixedly and distributes the fluid medium from the projecting inlet 11 laterally through the lower chamber 17.
At standstill of the heat exchanger the majority of the granular mass will be present in the lower chamber, below the first distribution plate 24. At start-up the fluid medium flow from the inlet 11 will try to follow the least obstructed route. Initially the fluid medium will flow mainly through the return tube 21, but as the granular mass is carried in fluidised state by the fluid medium flow the medium passing through the return tube will gradually meet with greater resistance, causing the fluid medium to start rising also in the riser tubes 18 with simultaneous fluidisation of the granular mass inside the riser tubes. A further increase of the fluid medium mass flow will cause the fluidised beds inside the riser tubes 18 to rise faster than the fluidised bed inside the return tube 21. This is due to the lateral bores 23 in the inflow pipe lengths 22 that cause the fluidised bed inside the riser tubes tO have a higher porosity than the bed inside the return tube. The fluidised granular mass in the riser tubes will first reach the upper chamber 16 and overflow into the return '~5~
t~be 21 throush which the granular mass and the fluid medium will start to flow down. In the lower chamber 17 between distribution plates 24 and q2 the downward flow through the return tube 21 and the upward fluid medium flow from the inlet 11 will be mixed, and finally a balanced state occurs where the volum~ of fluid medium leaving the heat exchanger via outlet 12 equals the volume that enters the heat exchanger through inlet 11 and the granular mass is circulating through the riser tubes 18 and the return tube 21. During the circulation process the riser tubes 18 are less hea~ily charged with granular mass than the return tube 21. To suppress the adverse e fect on the average logarithmic temperature difference due to the fluid medium flow through the return tube, circulation of the fluid medium through the return tube should be minimal.
An increase of the pressure difference between the upper and lower chzmbers contributes to reducing the fluid medium flow through the return tube. The increase of the pressure difference is achieved by fitting several distribution plates at a level above the return tube outlet into the lower chamber, preferably so that the apertures in the various distribution plates of the multiple desian are not vertically in line.
Fig. 3 shows the multiple distribution plate design 45,46,47 in the lower chamber 17 above the return tube 21 outlet.
~ igs. q and 5 illustrate the operation and design of the device for cleaning the lateral bores in the inflow pipe elements of the riser tubes. Fig. 4 shows the heat exchanger 1~ as it is shown in ~ig. 1 under normal operating conditions, the rise- tubes 18 functioning normallyA From rig. 4 is appears that the up?er section of the lower chamber 17 i5 connected, ~ 2~
by a pipe 51 provided with a shutoff valve 52, to a discharge line 53 that carries off the flowing fluid medium from the outlet 12. During normal operation the shutoff valve 52 is closed. The lower chamber 17 contains a granular mass volume in fluidised condition up to a level just below the lateral bores 23 in the inflow pipe lengths 22. Fluidised granular mass is further present in the riser tubes 18 and in the upper chamber 16. In the riser tubes 18 the granular mass and the fluid medium move upward and downward in the return tube 21.
If a lateral bore in an inflow pipe length of a riser tube clogs up the upward flow inside that riser tube may suddenly change into a downward flow. To avoid this undesirable situation it should be possible to remove any dirt deposits on the outer surface of the inflow pipe element. This is achieved by partly opening the shutoff valve 52. This will cause part o~ the fluid medium to flow to the discharge line 53 via the lower chamber 17 and the partly opened shutoff valve 52. The fluidised granular mass in the riser tubes 18 will sag to a level e.g. half the height of the riser tubes, and the upper chamber 16 will not contain any more granular mass at all.
~nder such conditions the return tube 21 will function as a partly filled riser tube. In the lower chamber 17 the volume of fluidised granular mass will be growing substantially, which will cause the granular mass to e~tend beyond the lateral bores 23 while yet keeping an adequate distance between the mass and the connection of pipe 51 to the lower chamber in order 9~
to prevent any granular mass from being carried off with the fluid medium. The abrasive action of the fluidised granular mass on the lateral bores in the inflow pipe lenaths will remove the ouling deposits and carry them off via the pipe 51.
Fig. 5 shows the position of the fluidised granular mass inside the system, with the shutoff valve 52 in the partly open position. It appears that the operating condition, which varies in that the shutoff valve 52 is partly open so that the lateral bores are being cleaned, has to be maintained for only a few do~en seconds, which is not generally considered objectionable. For inspection of the level of the fluidised granular mass in the lower chamber 17 during cleaning of the lateral bores in the inflow pipe elements, simple pressure difference measurement will be sufficient. When the shutoff valve 52 closes again the system will return to the original operating condition.
As already said, a disadvantage of an apparatus of the type described at the outset is that sometimes the circulation within the system of the fluid medium and of the granular mass produces an excessively adverse effect on the average logarithmic temperature difference across the heat exchanger. The main source of the problem is fluid medium circulation.
Fig. 6 shows an embodiment of a suitable solution for this problem that consists of providing a bypass 61 between the inlet 11 which opens into the lower chamber 1~ for the fluid medium taking part in the process and a position 62 in -15- ~2~ 9~3 the upper chamber 16 at which the bypass 61 opens at the ]evel of the inlet 63 of the return tube 21.
The bypass is provided with an adjustable valve 64.
At start-up of the heat exchanger it is recommended to keep the shutoff valve 64 in- the bypass 61 closed. When the s~stem is in a stable operating condition the shutoff valve 6~ can be sradually opened to partl~ or fully open depending on the process requirements. A fluid medium flow with a temperature equal to the entry temperature of th~ fluid medium in the lower chamber 17 is now present in the immediate area of the inlet opening 63 of the return tube. As the result the average temperature inside the return tube will be nearer to the entry temperature of the fluid medium in the lower chamber than it would be in the absence of the bypass which produces the beneficial effect referred to earlier. The bypass can also be located inside the heat exchanger.
Another solution for the problem that is solved by the embodiment of Fig. 6 is according to the invention achieved by locating a throttle device in front of the return tube inlet that gives precedence to passage of the fluid medium through the return tube over passage of the granular mass. Figs. 7 and 8 show an embodiment of this other solution. In Fig. 7 the throttle device 71 is a pipe that is provided as a continuation of the return tube 21 at 2 distance h from the inlet 63 of the return tube in the upper chamber 16. In principle the throttle device 71 can consist of a straight pipe length the top end of which extends far enough into the upper chamber 16 to prevent granules from dropping through the straight pipe into the return tube 21 during all normal operating conditions. Experimental results have shown that the distance h affects the rate of circulation of the granular mass and the fluid medium flow through the return tube. For correct adjust~ent of the circulation rate the distance h must satisfy the condition:
0.1 x Dv < h < 2.0 x Dv where Dv is the inner diamter of the return tube above which the throttle device is positioned.
By slightly changing the shape of the throttle device, the device will be capable of performing yet another function.
If insufficient care is exercised at start-up of the heat exchanger, the return tube may, 25 mentioned earlier, start to operate as a reiser tube carrying very large volumes of fluid medium and granular mass from the lower chamber 17 to the upper chamber 16. As the result the throttle device of the straight pipe type can blow the granules very high into the upper chamber and granules may be lost via outlet 12 for the fluid medium. This is an undesirable situation. By selecting a suitable inner diameter of the throttle device of the straight pipe type, and by bending the pipe at the top from the vertical plane into the horizontal plane and then bending it slightly down and again over an angle of about 90 degrees the granules and the fluid medium that are brought at high velocity out of the return tube 21 are trapped in the bent pipe and are further guided so that the granules remain in the upper chamber. Fig. 8 sho~s a top view of the design as a cross-section of the upper chamber illustratins how the pipe to be used as a throttle device must be bent. The inner diameter of the throttle devioe of the bent pipe type must exceed the inner diameter of the return tube to prevent granules from being lost.
A next aspect of the invention relates to apparatus for carrying out physical and/or chemical processes, in particular a heat exchanger of the continuous type, consisting of a bundle of parallel vertical riser tubès, an upper chamber, a lower chamber, an upper pipe plate and a lower pipe plate for open connection of the pipe bundle to the upper and lower chambers respectively, all of which are provided for through-flow of a first fluid medium, and an upper distribution chamber and a lower collecting chamber for throughflow of a second fluid medium, the bottom of the upper distribution chamber closing around each riser tube leaving a gap between the bottom of the upper distribution chamber and the riser tube wall, the top of the lower collecting chamber being open.
In this apparatus, the second fluid medium is a fluid that flows down as a film along the vertical riser tubes in cour,terflow with the first fluid medium that rises inside the riser tubes. For optimal cleaning of the outer surface of the riser tubes ox the outer surface of other pipes of the same bundle all tubes and pipes are fitted on the outside with a scraping device mounted in a supporiing assembly that can be driven mechanically. ~ig. 9 shows an embodiment of the scraping device, i.e. a top view perpendicular to the pipes.
In a ~rame consisting mainly of two yokes 201,202 and two crossbars 203,204, spacers 20~ are used to mount strips 206,207 tha. fit closely around the riser tubes 118. The frame is ~ 2~ 9~
displaced in the longitudinal direction along the riser tubes by means of a spindle 208 that engages in a threaded hole 209 in the yoke 201. The yoke 202 is guided by a ro~ 210 that passes through a hole 211 in the yoke. ~his is illustrated in Fig. 10 which shows a cross section of the scraping device in Fig. 9 along the line X-X shown in that figure. To allow mountiny of the scraping device in the heat exchanger the strip width must not exceed the free gap between the pipe rows in the bundle.
In a system of the last-described t~pe, particularly the gaps in the bottom of the upper dis.ribution chamber that allow the fluid to flow from the upper distribution chamber to the film around the riser tubes can get clogged. To reduce the risk of these gaps clogging up, in accordance with the invention at least one distribution shell is arranged in the uDper distribution chamber above the base; the shell is pTovided with apertures for distribution of the fluid over th~ gaps int he base. Fig. 11 shows apparatus 100 of the type described, having an upper chamber 116, a lower chamber 117 and a pipe bundle 118 for throughflow of the first fluid medium, and an upper distribution chamber 101 and a lower collect-iiJ~ chamber 102 for throughflow of a second fluid medium, wherein the upper distribution chamber 101 closes around each riser tube 118 so as to leave a gap 103 in the bottom 105 of the upper distribution chamber of the riser tube and wherein the top 106 of the lower collecting chamber 102 is open.
The upper distribution chamber is provi~ed with a distribu.ion plate 131 with apertures 130 centred between the -19 ~5~
riser tubes 1'8 which extend throush the upper dis~ribution chamber. The presence o~ the distribution plate 131 allows gaps 103 of g~eater width than is otherwise possible. Fig.
12 which shows a top view of a section of the distribu.ion plate 131, illustrates the centred positions of the apertures 130 between the riser tubes 118. For the sake of clarity, the scale ratios do not correspond with an actual embodiment.
As to the operation of the system, the fluid flowing down through ,he apertures 130 splashes outwardly on the bottom 105 and so reaches the outer walls of the riser tubes and runs down them as a film. Thus the gap 103 does not need to contribute essentially to the formation of the film. To ensure that the fluid jet will splash outwardly through an aperture 130 a suitable dis,ance must be maintained between the distribution plate 131 and the bottom 105.
It is remarked that, whereas the distribution plate re erred to above has been provided with apertures, these apert-ures rnay also be fitted with tuyeres, or spray nozzles, that cause lateral outflow from an a?erture.
To ensure stable operation of the various systems described above, the pressure drop in the fluid ~edium flow over the distribution plate into the lower chamber directly below the riser tubes must be in e~cess of one-ten.h of the pressure drop due to the total weight of the granular mass, as defined in the article quoted earlier and is illustrated in Canadian patent No. 1095507.
This is a division of Canadian Application No. 458,992 filed July 16, 1984.
The invention relates to apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type, comprising a bundle of parallel vertical riser tubes, an upper chamber, a lower chamber, upper and lower tube plates for open connection of the tube bundle with the upper and lower chambers respectively, a granular mass that can be kept in a fluidised condition, at least in the riser tubes, by a fluid medium flowing during operation upwardly through the lower chamber, the riser tubes and the upper chamber, a distribution pla-te for the granular mass in the lower chamber, and at least one return tube opening below the distribution plate for return of an overflow of granulax mass above the upper tube plate from the upper chamber to the lower chamber, wherein each riser tube is provided with an inflow element extending in the lower chamber, from the lower tube plate to a level above the distri-bution plate through which the return tube or return tubes projects or project, and wherein the lower chamber is provided with a device which prevents granules from reaching the lower chamber inlet for the fluid medium during standstill.
'~2~
An apparatus of this type is known from an article by D. G. Klaren in "Fouling Prevention Research Digest", Vol.
5, No. 1 pp. III-XVII (March 1983). The known heat exchanger that because of the presence of the fluidised bed has a high efficiency as a result of breakage of the fluid film along the inner surface of the riser tubes is primarily of interest, if, from the fluid medium on the inner surface of the riser tubes, a layer of material can be deposited that impedes heat transfer through the riser tube walls. This impeding layer is not deposited in the known apparatus due to the abrasive action of the granules. Therefore the known apparatus is ideal for application iJl e.g. the food industry.
On the other hand the presence of the granular mass brings its disadvantages. One disadvantage of the ~nown apparatus is that it is never completely certain that the downward flow of the granular mass will occur only in the return tube or the return tubes that are intended for the purpose. To achieve a correct desiqn and to ensure an even distribution of both the fluid medium and the granular mass across all riser tubes it is of utmost importance that only tubes that are intended for the purpose serve as return tubes. The situation where one or more riser tubes will still start to function as return tubes can occur in particular if insufficient care is exercised at start-up of the heat exchangerO It is then possible that the fluidised granules inside several riser tubes reach the top enas thereof earlier th2n the granules in other riser tubes, 5~
which causes the granules issuing from the former riser tubes to flow through the upper chamber into the adjoining riser tubes that are not yet completely filled with fluidised granules.
The result is disturbance of the pressure balance between the various tubes causing a downward flow of fluid medium and granules into one or several tubes that were not originally intended for such a downward flow.
The invention eliminates this first objection by means of a constriction at the ends of the riser tubes that open into the u?per chamber.
In this constriction the velocity of the fluid medium is increased to such an extent that the granules cannot drop from the upper chamber back into a riser tube. With the constriction correctly dimensioned, even a high irregular distribution of the granular mass across the riser tubes w th startup of the heat exchanger cannot cause one or several riser tubes to start acting as return tubes.
An advantageous construction of the apparatus is characterised by an upper pipe plate ?rovided with apertures for the riser tibes having smaller cross-sections than the riser tubes themselves.
The sranular mass circulates in the upward direction through the riser tubes and in the downward direction through the return tube. During this circulation, particularly in operation, sranules are in eddying motion also in the lower chamber tha. apparently are the source of very severe wear of the heat exchanger jacket, especially of the material at the junction of the bottom cover and the cylindrical wall which ~i 2rj'~ B
forms part of the shell.
The second disadvantage is eliminated according to the invention by means of a second distribution plate arranged in the lower chamber at a level below the outlet therein of the return tu`be.
In this proposed construction, in contrast with the known apparatus, the device that impedes the granules from reachins, at standstill, the inlet for the fluid medium in the lower chamber cannot serve as a shutoff valve against the lower eàge of the return tube. Consequently under all conditions a downward flow of the fluid medium will occur inside the return tube which, in the construction proposed, can amount to approx.
25 per cent of the fluid medium mass flow supplied to the heat exchanger inlet. As the result the average logarithmic temperature difference inside the riser tubes will be less favourable which requires that, to achieve a desired efficiency, a larger heated surface must be installed.
Tne last requirement can be obviated to a certain degree according to the invention by constructing the distribution plate at a level above the return tube outlet into the lower chamber in multiple; preferably so that the apertures in the various distribution plates of the multiple construction are not vertically in line.
It appears that the downward flow of the fluid medium throush the return tube or the return tubes can thus be limited to about 15 per cent of the mass flow through the heat exchanger inlet.
.
The absence of any moving parts in the ~ower chamber, i.e. of the provision as a valve of the device that prevents granules from -eaching, at standstill, the fluid medium inlet into the lower chamber, and ,he reduced wear of lower chamber parts of~set the disadvantage of fluid medium circulation through the return tube.
To stabilise the fluidised bed in a riser tube it has been suggested to provide the inflow pipe element with a lateral bore at a level where, during operation, no granules are present in the lower chamber, i.e. where only the fluid medium is present. If stroncly contaminating fluid media are used, e.g. fluid media that carry solids, the lateral bore may get clogged causing the fluidised bed in the riser tube to sag and finally causing the unintended functioning as a return tube of the riser tube, which must be defined as objectionable.
In a method of operation of apparatus of the type described at the outset, this last disadvantage is avoided by temporarily reducing the pressure of the fluid medium at the top of the lower chamber.
According to the invention, the apparatus of the type àescribed at the outset is thereby characterised by lateral bores provided in the inflow pipe elements. The top of the lower chamber above the level of the lateral bores is fitted with an outlet with shutoff valve.
In particular the apparatus according to the invention is characterised in that the outlet at the top of the lower chamber is directly connected with a fluid medium outlet of the upper chamber.
The presence of a return tube or of return tubes has the associated disadvantage of causing displacement of the fluid medium from the upper chamber to the lower chamber.
Although the granular mass flow inside the return tube will under some conditions stagnate and as it were clog up the return tube, in that case the intended average logarithmic temperature difference between the outer and inner surfaces of the riser tubes reguired for proper functioning of the heat exchanger will be adversely affecte2, unless by chance an operating point is found where this is not the case. However, such an operating point will entail undesirable restrictions and limitations of other operating parameters.
To be able at least to reduce this adverse effect the apparatus of the type described at the outset is character-ised by 2 bypass between the inlet for the fluid medium used in the process in the lower chamber and a point in the upper chamber where the bypass opens into the upper chamber at the level of the inlet opening of the return tube or 'ubes.
Thus the bypass, which is preferably fitted with an adjustable valve to control the flow through it, will at least partly eliminate the temperature difference be~ween the upper and the lower chambers.
7~
According to the invention another solution of the same problem is provided in that a throttle device is located before the inlet opening of the return tube, which gives precedence to passage through the return tube to the fluid medium over that of the granu]ar mass.
If the quantity of granular mass inside the return tube is thus limited less driving power will be available for circulation, which will cause reduced circulation through the return tube of granular mass and fluid medium.
Fouling can also occur on the outer wall of the riser tubes due to the nature of the second fluid medium used in the heat exchanging process. This particular problem relates to a more general class of heat exchangers, i.e. of the type where the second fluid medium that is used in the heat exchanging process is a fluid that, like a film, flows down the vertical riser tubes of apparatus for carrying out physical and/or chemical processes, more in particular a heat exchanger of the continuous type, consisting of a bundle of parallel vertical riser tubes, an upper chamber, a lower chamber, an upper pipe pla~e and a lower pipe plate for open connection of the pipe bundle with the upper and lower chambers, respectively, all for throughf]ow of the first fluid mediu~ and an upper distribution chamber and a lower collecting chamber for throughflow of the second fluid medium, the upper distribution chamber closing around each riser tube leaving a gap in the bottorn of the upper distribution chamber around each riser tube and the top of the lower collecting chamber being provided with collecting apertures around each riser tube.
S~ch apparatus is known from the article by D. G. Klaren in "Fouling Prevention Research Digest", Vol.
5, No. 1, pp. III-XVII (~arch 1983).
If the temperature and pressure occurring do not require that the fluid that is the second fluid medium is enclosed by a fixed jacket wall, the tubes can be easily cleaned from the outside, e.g. by washing down the pipe bunldes which may be done during operation. However, if a very strongly fouling fluid is used as the second fluid medium in the heat exchanging process the bund~es must be washed down so frequently that this is not practicable. Even if the process temperature and pressure do require that the second fluid medium is enclosed by a fixed jacket wall, this method for pipe bundle washing is out of the question. According to the invention optimal methods for cleaning the outer surfaces of the riser tubes are provided, in that all tubes have been fitted on the outside with a scraping device in a supporting construction that can be driven mechanically.
The scraping device of this type cannot reach the gaps in the bottom of the upper distribution chamber that may get clogged due to fouling.
To prevent the gaps from thus clogging up, or to at least delay the clogging process, the upper distribution chamber is provided, above its bottom, with a distribution shell that has apertures for distribution of the fluid over the saps in the bottom.
Thus the gaps in the bottom can be wider without substan,ially increasing the height of the upper distribution chamber.
_9_ ~5~9~
The invention in all its aspects wil] b~ illustra~ed below with a description referring to a plan. In the plan Fig. 1 shows an embodiment of a first aspect of the invention;
Figs. 2 and 3 show embodiments of the invention according to a second aspect;
Figs. 4 and 5 show embodiments of the i~vention according to a third aspect;
Fig. 6 shows an embodiment of the invention according to a fourth aspect;
Figs. 7 and 8 show an embodiment of the invention according to a fifth aspect;
Figs. 9 and 10 show an embodiment of the invention according to a sixth aspect; and Figs. 11 and 12 show an embodiment of the invention according to a seventh aspect.
Fig. 1 shows an embodiment of the apparatus according to the first aspect of the invention. The heat exchanber 10 has, for a first fluid medium, an inlet 11 and an outlet 12 and, for a second fluid medium, an inlet 13 and an outlet 19.
Inside the jacket 15 a lower chamber 17 connects to the inlet 11 and an upper chamber 16 connects to the outlet 12. A riser tube bundle 18 is arranged between an upper pipe plate 19 and a lower pipe plate 20, the riser tube bun~le including a return tube 21. The riser tubes are provided with inflow pipe elements 22 that extend from the lower pipe plate 20 downwardly into the lower chamber 17. The inflow pipe elements - - 1 0~
are provided with lateral bores 23. In the lower chamber 17-a distribution plate 24 is located below the inlets of the riser tubes and above the outlet of the return tube. The lower chamber 17 is further provided with a device 25 that prevents the granules in the lower chamber, the riser tubes, the upper chamber and the return tube from reaching the inlet 11. The device 25 is mounted on a spring assembly 26 which, at standstill, presses the device 25 against the outlet aper'ure of the return tube. In any case the granules can be brought into the fluidised bed condition in the riser tubes 18. The lower end of the return tube 21 will contain a stagnating granular mass 27.
According to the invention the upper pipe plate 19 of the heat exchanger 10 is provided with throttling apertures 32 via which the riser tubes 18 open into the upper chamber 16. For instance the apertures 32 are provided in a throttle plate 31 constituting, within the assembly, an integral part of the upper pipe plate 19 and not forming an obstacle for the return tube 21.
It will be obvious that the throttling apertures 32 in the outlets of the riser tubes 18 are effective to prevent granules from dropping into the riser tubes from the upper pipe plate independently of the valve action of the device 25.
Figs. 2 and 3 show embodiments of the invention according to a second aspect. The desig~ of the apparatus in these embodiments corresponds in most respects with that sho~n in Fig. 1. To prevent the material of the jac~et, 5~g8 particularly at the junction of the bottom cover 43 to the cylindrical wall 44, from being excessively worn due to the eddying motion of the granules constituting the material of the fluidised beds in the riser tubes, a second distribution plat. 92 is proviaed in the lower chamber 17 at a level below the outlet in the lower chamber 17 of the return tube 21.
The device that prevents granules from reaching, at standstill, the inlet 11 in the lower chamber 17 is provided as a simple bell ~1 which is mounted fixedly and distributes the fluid medium from the projecting inlet 11 laterally through the lower chamber 17.
At standstill of the heat exchanger the majority of the granular mass will be present in the lower chamber, below the first distribution plate 24. At start-up the fluid medium flow from the inlet 11 will try to follow the least obstructed route. Initially the fluid medium will flow mainly through the return tube 21, but as the granular mass is carried in fluidised state by the fluid medium flow the medium passing through the return tube will gradually meet with greater resistance, causing the fluid medium to start rising also in the riser tubes 18 with simultaneous fluidisation of the granular mass inside the riser tubes. A further increase of the fluid medium mass flow will cause the fluidised beds inside the riser tubes 18 to rise faster than the fluidised bed inside the return tube 21. This is due to the lateral bores 23 in the inflow pipe lengths 22 that cause the fluidised bed inside the riser tubes tO have a higher porosity than the bed inside the return tube. The fluidised granular mass in the riser tubes will first reach the upper chamber 16 and overflow into the return '~5~
t~be 21 throush which the granular mass and the fluid medium will start to flow down. In the lower chamber 17 between distribution plates 24 and q2 the downward flow through the return tube 21 and the upward fluid medium flow from the inlet 11 will be mixed, and finally a balanced state occurs where the volum~ of fluid medium leaving the heat exchanger via outlet 12 equals the volume that enters the heat exchanger through inlet 11 and the granular mass is circulating through the riser tubes 18 and the return tube 21. During the circulation process the riser tubes 18 are less hea~ily charged with granular mass than the return tube 21. To suppress the adverse e fect on the average logarithmic temperature difference due to the fluid medium flow through the return tube, circulation of the fluid medium through the return tube should be minimal.
An increase of the pressure difference between the upper and lower chzmbers contributes to reducing the fluid medium flow through the return tube. The increase of the pressure difference is achieved by fitting several distribution plates at a level above the return tube outlet into the lower chamber, preferably so that the apertures in the various distribution plates of the multiple desian are not vertically in line.
Fig. 3 shows the multiple distribution plate design 45,46,47 in the lower chamber 17 above the return tube 21 outlet.
~ igs. q and 5 illustrate the operation and design of the device for cleaning the lateral bores in the inflow pipe elements of the riser tubes. Fig. 4 shows the heat exchanger 1~ as it is shown in ~ig. 1 under normal operating conditions, the rise- tubes 18 functioning normallyA From rig. 4 is appears that the up?er section of the lower chamber 17 i5 connected, ~ 2~
by a pipe 51 provided with a shutoff valve 52, to a discharge line 53 that carries off the flowing fluid medium from the outlet 12. During normal operation the shutoff valve 52 is closed. The lower chamber 17 contains a granular mass volume in fluidised condition up to a level just below the lateral bores 23 in the inflow pipe lengths 22. Fluidised granular mass is further present in the riser tubes 18 and in the upper chamber 16. In the riser tubes 18 the granular mass and the fluid medium move upward and downward in the return tube 21.
If a lateral bore in an inflow pipe length of a riser tube clogs up the upward flow inside that riser tube may suddenly change into a downward flow. To avoid this undesirable situation it should be possible to remove any dirt deposits on the outer surface of the inflow pipe element. This is achieved by partly opening the shutoff valve 52. This will cause part o~ the fluid medium to flow to the discharge line 53 via the lower chamber 17 and the partly opened shutoff valve 52. The fluidised granular mass in the riser tubes 18 will sag to a level e.g. half the height of the riser tubes, and the upper chamber 16 will not contain any more granular mass at all.
~nder such conditions the return tube 21 will function as a partly filled riser tube. In the lower chamber 17 the volume of fluidised granular mass will be growing substantially, which will cause the granular mass to e~tend beyond the lateral bores 23 while yet keeping an adequate distance between the mass and the connection of pipe 51 to the lower chamber in order 9~
to prevent any granular mass from being carried off with the fluid medium. The abrasive action of the fluidised granular mass on the lateral bores in the inflow pipe lenaths will remove the ouling deposits and carry them off via the pipe 51.
Fig. 5 shows the position of the fluidised granular mass inside the system, with the shutoff valve 52 in the partly open position. It appears that the operating condition, which varies in that the shutoff valve 52 is partly open so that the lateral bores are being cleaned, has to be maintained for only a few do~en seconds, which is not generally considered objectionable. For inspection of the level of the fluidised granular mass in the lower chamber 17 during cleaning of the lateral bores in the inflow pipe elements, simple pressure difference measurement will be sufficient. When the shutoff valve 52 closes again the system will return to the original operating condition.
As already said, a disadvantage of an apparatus of the type described at the outset is that sometimes the circulation within the system of the fluid medium and of the granular mass produces an excessively adverse effect on the average logarithmic temperature difference across the heat exchanger. The main source of the problem is fluid medium circulation.
Fig. 6 shows an embodiment of a suitable solution for this problem that consists of providing a bypass 61 between the inlet 11 which opens into the lower chamber 1~ for the fluid medium taking part in the process and a position 62 in -15- ~2~ 9~3 the upper chamber 16 at which the bypass 61 opens at the ]evel of the inlet 63 of the return tube 21.
The bypass is provided with an adjustable valve 64.
At start-up of the heat exchanger it is recommended to keep the shutoff valve 64 in- the bypass 61 closed. When the s~stem is in a stable operating condition the shutoff valve 6~ can be sradually opened to partl~ or fully open depending on the process requirements. A fluid medium flow with a temperature equal to the entry temperature of th~ fluid medium in the lower chamber 17 is now present in the immediate area of the inlet opening 63 of the return tube. As the result the average temperature inside the return tube will be nearer to the entry temperature of the fluid medium in the lower chamber than it would be in the absence of the bypass which produces the beneficial effect referred to earlier. The bypass can also be located inside the heat exchanger.
Another solution for the problem that is solved by the embodiment of Fig. 6 is according to the invention achieved by locating a throttle device in front of the return tube inlet that gives precedence to passage of the fluid medium through the return tube over passage of the granular mass. Figs. 7 and 8 show an embodiment of this other solution. In Fig. 7 the throttle device 71 is a pipe that is provided as a continuation of the return tube 21 at 2 distance h from the inlet 63 of the return tube in the upper chamber 16. In principle the throttle device 71 can consist of a straight pipe length the top end of which extends far enough into the upper chamber 16 to prevent granules from dropping through the straight pipe into the return tube 21 during all normal operating conditions. Experimental results have shown that the distance h affects the rate of circulation of the granular mass and the fluid medium flow through the return tube. For correct adjust~ent of the circulation rate the distance h must satisfy the condition:
0.1 x Dv < h < 2.0 x Dv where Dv is the inner diamter of the return tube above which the throttle device is positioned.
By slightly changing the shape of the throttle device, the device will be capable of performing yet another function.
If insufficient care is exercised at start-up of the heat exchanger, the return tube may, 25 mentioned earlier, start to operate as a reiser tube carrying very large volumes of fluid medium and granular mass from the lower chamber 17 to the upper chamber 16. As the result the throttle device of the straight pipe type can blow the granules very high into the upper chamber and granules may be lost via outlet 12 for the fluid medium. This is an undesirable situation. By selecting a suitable inner diameter of the throttle device of the straight pipe type, and by bending the pipe at the top from the vertical plane into the horizontal plane and then bending it slightly down and again over an angle of about 90 degrees the granules and the fluid medium that are brought at high velocity out of the return tube 21 are trapped in the bent pipe and are further guided so that the granules remain in the upper chamber. Fig. 8 sho~s a top view of the design as a cross-section of the upper chamber illustratins how the pipe to be used as a throttle device must be bent. The inner diameter of the throttle devioe of the bent pipe type must exceed the inner diameter of the return tube to prevent granules from being lost.
A next aspect of the invention relates to apparatus for carrying out physical and/or chemical processes, in particular a heat exchanger of the continuous type, consisting of a bundle of parallel vertical riser tubès, an upper chamber, a lower chamber, an upper pipe plate and a lower pipe plate for open connection of the pipe bundle to the upper and lower chambers respectively, all of which are provided for through-flow of a first fluid medium, and an upper distribution chamber and a lower collecting chamber for throughflow of a second fluid medium, the bottom of the upper distribution chamber closing around each riser tube leaving a gap between the bottom of the upper distribution chamber and the riser tube wall, the top of the lower collecting chamber being open.
In this apparatus, the second fluid medium is a fluid that flows down as a film along the vertical riser tubes in cour,terflow with the first fluid medium that rises inside the riser tubes. For optimal cleaning of the outer surface of the riser tubes ox the outer surface of other pipes of the same bundle all tubes and pipes are fitted on the outside with a scraping device mounted in a supporiing assembly that can be driven mechanically. ~ig. 9 shows an embodiment of the scraping device, i.e. a top view perpendicular to the pipes.
In a ~rame consisting mainly of two yokes 201,202 and two crossbars 203,204, spacers 20~ are used to mount strips 206,207 tha. fit closely around the riser tubes 118. The frame is ~ 2~ 9~
displaced in the longitudinal direction along the riser tubes by means of a spindle 208 that engages in a threaded hole 209 in the yoke 201. The yoke 202 is guided by a ro~ 210 that passes through a hole 211 in the yoke. ~his is illustrated in Fig. 10 which shows a cross section of the scraping device in Fig. 9 along the line X-X shown in that figure. To allow mountiny of the scraping device in the heat exchanger the strip width must not exceed the free gap between the pipe rows in the bundle.
In a system of the last-described t~pe, particularly the gaps in the bottom of the upper dis.ribution chamber that allow the fluid to flow from the upper distribution chamber to the film around the riser tubes can get clogged. To reduce the risk of these gaps clogging up, in accordance with the invention at least one distribution shell is arranged in the uDper distribution chamber above the base; the shell is pTovided with apertures for distribution of the fluid over th~ gaps int he base. Fig. 11 shows apparatus 100 of the type described, having an upper chamber 116, a lower chamber 117 and a pipe bundle 118 for throughflow of the first fluid medium, and an upper distribution chamber 101 and a lower collect-iiJ~ chamber 102 for throughflow of a second fluid medium, wherein the upper distribution chamber 101 closes around each riser tube 118 so as to leave a gap 103 in the bottom 105 of the upper distribution chamber of the riser tube and wherein the top 106 of the lower collecting chamber 102 is open.
The upper distribution chamber is provi~ed with a distribu.ion plate 131 with apertures 130 centred between the -19 ~5~
riser tubes 1'8 which extend throush the upper dis~ribution chamber. The presence o~ the distribution plate 131 allows gaps 103 of g~eater width than is otherwise possible. Fig.
12 which shows a top view of a section of the distribu.ion plate 131, illustrates the centred positions of the apertures 130 between the riser tubes 118. For the sake of clarity, the scale ratios do not correspond with an actual embodiment.
As to the operation of the system, the fluid flowing down through ,he apertures 130 splashes outwardly on the bottom 105 and so reaches the outer walls of the riser tubes and runs down them as a film. Thus the gap 103 does not need to contribute essentially to the formation of the film. To ensure that the fluid jet will splash outwardly through an aperture 130 a suitable dis,ance must be maintained between the distribution plate 131 and the bottom 105.
It is remarked that, whereas the distribution plate re erred to above has been provided with apertures, these apert-ures rnay also be fitted with tuyeres, or spray nozzles, that cause lateral outflow from an a?erture.
To ensure stable operation of the various systems described above, the pressure drop in the fluid ~edium flow over the distribution plate into the lower chamber directly below the riser tubes must be in e~cess of one-ten.h of the pressure drop due to the total weight of the granular mass, as defined in the article quoted earlier and is illustrated in Canadian patent No. 1095507.
Claims (7)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. An apparatus for carrying out physical pro-cesses or chemical processes, or both, comprising:
a bundle of vertical riser tubes arranged parallel to each other;
an upper chamber;
a lower chamber having an inlet for a fluid medium;
an upper pipe plate and a lower pipe plate each connected to the riser tubes to provide fluid communication between the upper and lower chambers;
a granular mass which is fluidisable at least in the riser tubes by the fluid medium which flows up-wardly during operation through the lower chamber, the riser tubes and the upper chamber;
a first distribution plate for the granular mass in the lower chamber;
at least one return tube for return of the granular mass from the upper chamber to the lower chamber, the at least one return tube having an outlet below the first distribution plate;
a device in the lower chamber which is adapted to prevent the granular mass from reaching the inlet to the lower chamber when the fluid medium is stationary;
an inflow pipe element on each riser tube which extends into the lower chamber from the lower pipe plate to a position spaced above the first distribution plate; and a second distribution plate in the lower chamber and positioned below the outlet of the at least one return tube.
a bundle of vertical riser tubes arranged parallel to each other;
an upper chamber;
a lower chamber having an inlet for a fluid medium;
an upper pipe plate and a lower pipe plate each connected to the riser tubes to provide fluid communication between the upper and lower chambers;
a granular mass which is fluidisable at least in the riser tubes by the fluid medium which flows up-wardly during operation through the lower chamber, the riser tubes and the upper chamber;
a first distribution plate for the granular mass in the lower chamber;
at least one return tube for return of the granular mass from the upper chamber to the lower chamber, the at least one return tube having an outlet below the first distribution plate;
a device in the lower chamber which is adapted to prevent the granular mass from reaching the inlet to the lower chamber when the fluid medium is stationary;
an inflow pipe element on each riser tube which extends into the lower chamber from the lower pipe plate to a position spaced above the first distribution plate; and a second distribution plate in the lower chamber and positioned below the outlet of the at least one return tube.
2. An apparatus according to Claim 1 in which a plurality of first distribution plates are provided in the lower chamber above the outlet of the return tube.
3. An apparatus according to Claim 2 in which the plurality of first distribution plates are arranged so that the apertures of adjacent plates are not vertically aligned.
4. An apparatus according to any one of Claims 1 to 3 in which the apparatus is a continuous type heat exchanger.
5. An apparatus according to any one of Claims 1 to 3 in which each inflow pipe element has a lateral bore.
6. A method of operating an apparatus for carry-ing out physical processes or chemical processes, or both, comprising a bundle of vertical riser tubes arranged parallel to each other; an upper chamber; a lower chamber having an inlet for a fluid medium; an upper pipe plate and a lower pipe plate each connected to the riser tubes to provide fluid communication between the upper and lower chambers; a granular mass which is fluidisable at least in the riser tubes by the fluid medium which flows upwardly during operation through the lower chamber, the riser tubes and the upper chamber; a first distribution plate for the granular mass in the lower chamber; at least one return tube for return of the granular mass from the upper chamber to the lower chamber, the at least one return tube having an outlet below the first distribution plate; a device in the lower chamber which is adapted to prevent the granular mass from reaching the inlet to the lower chamber when the fluid medium is stationary; and an inflow pipe element on each riser tube which extends into the lower chamber from the lower pipe plate to a position spaced above the first distribution plate, each inflow pipe element having a lateral bore; wherein the pressure of the fluid medium at the top of the lower chamber is temporarily reduced.
7. A method according to Claim 6 in which the apparatus is a continuous type heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000548066A CA1251198A (en) | 1983-07-22 | 1987-09-28 | Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type |
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL8302622 | 1983-07-22 | ||
| NL8302622A NL192055C (en) | 1983-07-22 | 1983-07-22 | Device for operating physical and / or chemical processes, in particular a heat exchanger with circulation of granular mass. |
| CA000458992A CA1232602A (en) | 1983-07-22 | 1984-07-16 | Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type |
| CA000548066A CA1251198A (en) | 1983-07-22 | 1987-09-28 | Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000548066A Division CA1251198A (en) | 1983-07-22 | 1987-09-28 | Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000548066A Division CA1251198A (en) | 1983-07-22 | 1987-09-28 | Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1251198A true CA1251198A (en) | 1989-03-14 |
Family
ID=25670446
Family Applications (3)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000548065A Expired CA1256097A (en) | 1983-07-22 | 1987-09-28 | Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type |
| CA000548066A Expired CA1251198A (en) | 1983-07-22 | 1987-09-28 | Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type |
| CA000548064A Expired CA1246542A (en) | 1983-07-22 | 1987-09-28 | Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000548065A Expired CA1256097A (en) | 1983-07-22 | 1987-09-28 | Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type |
Family Applications After (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000548064A Expired CA1246542A (en) | 1983-07-22 | 1987-09-28 | Apparatus for carrying out physical and/or chemical processes, more specifically a heat exchanger of the continuous type |
Country Status (1)
| Country | Link |
|---|---|
| CA (3) | CA1256097A (en) |
-
1987
- 1987-09-28 CA CA000548065A patent/CA1256097A/en not_active Expired
- 1987-09-28 CA CA000548066A patent/CA1251198A/en not_active Expired
- 1987-09-28 CA CA000548064A patent/CA1246542A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| CA1256097A (en) | 1989-06-20 |
| CA1246542A (en) | 1988-12-13 |
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