Patent Publication Number: US-2020284514-A1

Title: Heat Exchanger

Description:
The invention relates to a heat exchanger and in particular to a thermosyphon heat pipe type heat exchanger. 
     Heat recovery from slurries and scaling fluids is often conducted by flashing the slurry or fluid to a lower pressure and condensing the flashed vapour in a heat exchanger, heating a cooler process stream. 
     For example, in alumina refineries with low temperature digestion (at ˜145° C.) there are normally 3 digestion flash tanks online, and in high temperature digestion (normally ≥240° C.) there are normally 10 flash tanks online in the digestion section of the alumina refinery. A reasonable temperature drop in a flash tank is 12° C., although it can be higher, especially in high temperature digestion refineries. The refinery liquor typically has a boiling point elevation of 8° C. and the heat exchanger may have an approach temperature as low as 2° C. This means that the net heating in digestion must be at least around 12+8+2° C., or normally more than 22° C., typically ˜25° C. in low temperature digestion, and more in high temperature digestion. 
     Steam from digestion flash tanks invariably contains trace amounts of refinery liquor that contributes to scaling of the outside of the heat exchange tubes, whether they are tubes in a shell and tube heat exchanger, or “tubes” in a jacketed tube digestor. This scale is difficult to remove as it is on the “shell-side” of the heat exchanger or tube digestor. 
     Flash tanks, due to their geometry and size, are descaled manually by mechanical means; whereas the insides of tubes are easier to clean, either chemically through turbulent flow, or by semi-automatic mechanical means. 
     In addition to the refinery&#39;s high-energy requirement, another disadvantage of flash tanks in digestion is the increasing caustic concentration of the liquor passing through digestion flash tanks which reduces refinery productivity. 
     Heat recovery from the precipitation slurry of a traditional alumina refinery is not practical as the additional heat cannot be utilised in digestion with the current technology of flash cooling of the digestion slurry and heat exchange to the digestion feed stream. Often refineries even enhance heat loss in the precipitation section of the refinery. 
     A heat-pipe based heat exchanger, as described in U.S. Pat. No. 5,027,891, can be applied to achieve approach temperatures that are significantly less than 22° C. The heat exchanger is typically a shell and tube heat exchanger with a plurality of conduits and water (H 2 O, R-718) as the heat transfer fluid. There is no requirement for a wick as the “cold” pipes are located above the “hot” pipes so gravity returns the condensate to the fluid surrounding the “hot” pipes. Unfortunately, the use of a plurality of closely packed tubes, as desired to maximise heat transfer area in a traditional shell and tube heat exchanger, may lead to operability problems as the possibility of flooding of the heat exchanger, as heat transfer fluid accumulates about the “cold” pipes reduces its heat transfer efficiency. To the Applicant&#39;s knowledge, the heat exchanger of U.S. Pat. No. 5,027,891 has not been used commercially. 
     It is an object of the present invention to avoid operability problems such as those due to flooding in a heat exchanger, especially of heat pipe type. Such a heat exchanger could usefully be deployed in industry, for example the alumina industry, but the present invention is not limited to use in alumina refining, or any process that conducts heat recovery via flash tank and heat exchanger. 
     With this object in view, the present invention provides a heat exchanger of thermosyphon heat pipe configuration for transferring heat between a first process stream and a second process stream through the medium of a heat transfer fluid comprising: 
     at least one first process stream passage; 
     at least one second process stream passage; and 
     a shell enclosing said plurality of first and second process stream passages within a volume, said volume being, as a result of a heat transfer process, fully filled with both vapour and liquid phases of said heat transfer fluid wherein said at least one first process stream passage and said at least one second process stream passage are spaced by a disengagement zone enabling separation of said vapour and liquid phases and limiting accumulation of liquid phase heat transfer fluid about said first process stream passages. Advantageously, the heat exchanger includes a plurality of first and second process stream passages to enhance heat transfer efficiency. A convenient form of passage is contained within a pipe or tube and the terms “passage”, “pipe” and “tube” may be used interchangeably in the following description. 
     The first process stream passages or pipes may contain a stream, preferably a liquor stream, which is to be heated by the condensation of the vapour phase of the heat transfer fluid. The liquor stream may be a slurry. The first process stream passages may be referred to as “cold” pipes. The second process stream passages or pipes then conveniently contain a stream, preferably a liquor stream which is to be cooled by the evaporation of the liquid phase of the heat transfer fluid. The liquor stream may be a slurry. The first process stream pipes are typically located above the second process stream passages with the heat exchanger being a thermosyphon heat pipe heat exchanger. The second process stream pipes may be referred to as “hot” pipes. The diameters of the pipes are selected as small as possible to provide maximum surface area for heat exchange, but without the risk of blockage with a reasonable period of chemical and, or mechanical cleaning, nor too much pressure drop for a conventional hydraulic or pumping system. 
     The first and second process stream pipes may be arranged in a number of ways. The first and second process stream pipes may have the same arrangement, for example each being arranged in parallel or in a bundle. First and second process stream pipes may also be arranged in discrete groups or bundles having the same or different numbers of pipes in each group. Diameters of the first and second process stream pipes may be the same or different. For instance, the “cold” pipes may have lesser diameter, collectively providing greater surface area, than “hot” pipes. One method is to arrange the first process stream pipes in a conventional shell and tube condenser arrangement, and the second process stream and entrainment disengagement zone in a conventional shell and tube reboiler arrangement. For instance, the tube pitch of the first process stream pipes can be 1.25 of the first process stream pipe diameter, typical of the tube pitch found in conventional shell and tube condensers, whereas the tube pitch of the second process stream can be 1.5 to 2.0 of the second process stream pipe diameter, typical of the tube pitch found in conventional shell and tube reboilers. 
     The first and second process stream pipes may be separated by one or more baffles arranged in the disengaging zone. Including baffle(s), conveniently in the form of metal plates, would increase the heat load at which a flooding point is reached and may be advantageous dependent on the selected heat transfer fluid. Baffle(s) may be disposed in the heat exchanger to direct vapour and/or condensate along desired paths selected to further minimise flooding risk. To this end, baffle(s) are desirably spaced from the shell by a gap to direct vapour along a path so as to “push” condensate towards the shell away from the rising vapour thus minimising the impact of vapour velocity on flooding the heat exchanger. 
     Pressure within the first and second process stream pipes is desirably maintained above the vapour pressure of the liquid phase to avoid two phase flow. 
     The heat exchanger enables disengagement of liquid and vapour phases of said heat transfer fluid by gravity. A wick could be used but should not be necessary. Entrainment separators could be installed in the disengagement zone. The disengaging zone has height and horizontal cross-sectional area sufficient to enable a desired degree of liquid disengagement of condensate from the vapour phase by gravity for a given heat transfer fluid. The disengagement zone can be designed in the same way as the disengagement zone in a conventional shell and tube reboiler, for instance the maximum vapour velocity can be defined by the Souders Brown equation: 
     
       
         
           
             V 
             = 
             
               k 
                
               
                 
                   
                     
                       ρ 
                       L 
                     
                     - 
                     
                       ρ 
                       V 
                     
                   
                   
                     ρ 
                     V 
                   
                 
               
             
           
         
       
     
     where: V=maximum heat transfer fluid vapour velocity (m/s) 
     k=constant (m/s) 
     ρ L =density of heat transfer fluid liquid (kg/m 3 ) 
     ρ L =density of heat transfer fluid vapour (kg/m 3 ) 
     The Souders-Brown equation constant, k can be set to 0.2 m/s similar to that used in a conventional reboiler disengagement zone. 
     The heat transfer fluid and heat exchanger cross-sectional area are selected so that a heat transfer fluid vapour velocity is sufficient to avoid flooding. The selected heat transfer fluid desirably reduces the vapour upward velocity by selecting one that has a high heat flux (energy flow per horizontal cross-sectional area, e.g. KW/m 2 ) at the normal heat exchanger operating temperature. Preferred parameters include one or more of high heat of evaporation, high vapour pressure, high difference in liquid and vapour density; and high boiling and condensing heat transfer coefficients. The heat transfer fluid can be selected from known refrigerants and heat pipe heat transfer fluids. 
     First and second process stream pipes may be respectively arranged in discrete vessels, i.e. hot and cold vessels, which communicate through separate passages. One such set of passages may enable vapour to travel from the hot vessel to the cold vessel. Another set of passages could enable condensed heat transfer fluid to return from the cold vessel to the hot vessel. 
     In such case, a portion of, or all of, the vapour phase may be compressed to increase condensation temperature if desired to increase heat transfer efficiency. Compression increases the vapour pressure, and thus the condensation temperature and so the driving force for heat transfer in the heat exchanger. A combination of compressor and restriction—such as an orifice—respectively on the vapour and condensate of the heat transfer fluid can be used to reduce heat transfer area and, or reduce approach temperature of the heat exchanger system to a smaller value or even to a negative value. 
     The present invention also provides a process for transferring heat between a first process stream and a second process stream through the medium of a heat transfer fluid in a heat exchanger of heat pipe configuration comprising: 
     directing a first process stream through at least one first process stream passage; 
     directing a second process stream through at least one second process stream passage; and 
     placing a heat transfer fluid in a shell enclosing said first and second process stream passages within a volume, said volume being, as a result of the heat transfer process, fully filled with both vapour and liquid phases of said heat transfer fluid wherein said at least one first process stream passage and said at least one second process stream passage are spaced by a disengagement zone enabling separation of said vapour and liquid phases and limiting accumulation of liquid phase heat transfer fluid about said at least one first process stream passage. Advantageously, the heat exchanger includes a plurality of first and second process stream passages to enhance heat transfer efficiency. 
     The selection of optimum heat transfer fluids depends, in addition to considerations described above, on the operating temperature range of a process in which the heat exchanger is deployed. Some preferred heat transfer fluids for 100° C., without limitation because a range of refrigerants and heat pipe heat transfer fluids can be used, are water (H 2 O, R-718), ammonia (NH 3 , R-717), chloromethane (CH 3 Cl, R-40), butane (C 4 H 10 , R-600), chloroethane (C 2 H 5 Cl, R-160), and dodecafluoropentane (C 5 F 12 , R-4-1-12). The heat transfer fluid is selected to have a critical point above the desired temperature operating range for a chemical process. The heat transfer medium is conveniently selected to have thermal stability and no formation of scale throughout the heat exchanger operating temperature range. For example, while water (H 2 O, R-718) could be used as a heat transfer medium operating at 100° C., its selection is not preferable as other fluids, such as ammonia (NH 3 , R-717) and chloromethane (C 2 H 5 Cl, R-160), have a higher heat flux at their flooding point and so are less susceptible to flooding at this temperature. 
     The heat exchanger and process may be used in a range of industries, for example in hydrometallurgical processes including in the alumina industry where heat exchangers, as described above, may be applied to replace a conventional flash cooling system in a Bayer process plant in which case the first and second process streams may be termed Bayer process streams. The heat exchanger may be included within a tubular reactor, such as a tubular digester used in the alumina industry. The heat exchanger could also be used in other tubular reactors. 
    
    
     
       The heat exchanger and heat transfer process may be more fully understood from the following description of preferred embodiments thereof. Such description is made with reference to the accompanying drawings in which: 
         FIG. 1  is a flowsheet for a prior art Bayer process. 
         FIG. 2  is a flowsheet for a Bayer process including the heat exchanger of embodiments of the present invention. 
         FIG. 3 a    is a cross-section of a heat exchanger according to a first embodiment of the present invention. 
         FIG. 3 b    is a cross-section of a heat exchanger according to a second embodiment of the present invention. 
         FIG. 4  is a cross-section of a heat exchanger according to a third embodiment of the present invention and including a baffle. 
         FIG. 5  is a cross-section of a heat exchanger according to a fourth embodiment of the present invention and including a baffle arrangement. 
         FIG. 6  is a cross-section of a heat exchanger according to a fifth embodiment of the present invention and including a baffle arrangement. 
         FIG. 7  is a cross-section of a heat exchanger according to a sixth embodiment of the present invention and including a baffle arrangement. 
         FIG. 8  is a cross-section of a heat exchanger according to a seventh embodiment of the present invention and including a baffle arrangement 
         FIG. 9  is a cross-section of a heat exchanger in which first and second process stream passages are arranged in two separate vessels. 
         FIG. 10  is a cross-section of a heat exchanger in which there is a compressor in the vapour stream and a restriction in the liquid line between the first and second process stream passages are arranged in two separate vessels. 
     
    
    
     Referring now to  FIG. 1 , a prior art Bayer process plant  1  employs flash cooling between the digestion stage and red mud separation stages. Bauxite ore is ground and leached with a caustic solution in a heated digester. Low temperature or high temperature digestion processes can be used in accordance with known practice in the art. A slurry comprising a liquor portion containing dissolved sodium aluminate values, and a solid portion made up of undissolved bauxite ore and gangue is then cooled in a flash cooling system which typically requires substantial space. Flash cooling occurs due to successive pressure reduction steps, typically around ten steps in high temperature digestion and three in low temperature digestion, which causes some of the liquor portion to evaporate to steam. This steam is used to heat spent or regenerated liquor, or a slurry of these liquors and bauxite for return to the digester. The heat transfer efficiency in flash cooling is limited by considerations such as those described above, particularly the boiling point elevation and the temperature drop in the flashing stage. Scaling and concentration of the liquor stream can also cause operational efficiency concerns. 
     The flash cooling stage of  FIG. 1  is replaced with a plurality of heat exchangers  10  in the Bayer process plant  100  of  FIG. 2  and notably in the digestion and precipitation sections. Heat exchanger  10  has a heat pipe configuration of thermosyphon type for transferring heat between the hot pregnant liquor stream or slurry containing dissolved sodium aluminate and undissolved bauxite and gangue; and a cooler spent liquor stream or a slurry of spent liquor and bauxite through the medium of a heat transfer fluid. Heat exchanger  10  comprises, as shown in  FIGS. 3 a    to  9 , a plurality of first process stream pipes and a plurality of second process stream pipes, all of cylindrical geometry and fabricated from thermally conductive material such as carbon steel, stainless steel, nickel plated or nickel. A cylindrical shell  11  encloses the first and second process stream pipes which extend horizontally within a volume  55  which, as a result of a heat transfer process, is fully filled with both vapour and liquid phases of the heat transfer fluid. The liquid phase of the heat transfer fluid forms a liquid volume  35  in which the first process stream pipes are fully immersed. The heat transfer fluid is selected taking the following considerations into account. Depending on the operating temperature, water (H 2 O, R-718) may not be the preferred heat transfer fluid for the application due to its propensity to cause flooding of heat exchanger  10  at lower heat transfer flux than other possible heat transfer fluids. Such heat transfer fluids may, for example and without limitation, be selected from refrigerants and heat pipe heat transfer fluids the group consisting of ammonia (NH 3 , R-717), chloromethane (CH 3 Cl, R-40), propane (C 3 H 8 , R-290)), butane (C 4 H 10 , R-600), chloroethane (C 2 H 5 Cl, R-160), octafluoropropane (C 3 F 8 , R-218) and dodecafluoropentane (C 5 F 12 , R-4-1-12) may be preferred to address such issues. 
     The heat transfer fluid partially vapourises as heat is transferred from the hot pipes to the heat transfer fluid. Saturated vapour with heat transfer fluid rises to the disengagement zone, where mainly heat transfer vapour then rises towards the cold pipes and condenses so latent heat of vaporisation is transferred from the heat transfer fluid to the cold pipes. Spent liquor or spent liquor and bauxite slurry are heated in this process. 
     The plurality of first process stream pipes and the plurality of second process stream pipes are spaced by a disengagement zone  50  of height and horizontal cross-section sufficient to enable separation of said vapour and liquid phases by gravity and limiting accumulation of liquid phase heat transfer fluid about said first process stream pipes. 
     In  FIG. 2 , the cooling in precipitation is replaced by the heat exchanger  10  where precipitation slurry is the “hot” process stream and spent liquor is the “cold” process stream. If the heat balance of the process requires it, a heat exchanger  10  can be used where precipitation slurry is the hot stream and a cooling fluid such as cooling water can be the “cold” stream. 
       FIG. 3 a    shows a heat exchanger  10  with a single hot pipe  29  and single cold pipe  19 . Heat transfer efficiency would be improved, in most cases, by providing a plurality of hot pipes and a plurality of cold pipes. 
       FIG. 3 b    shows heat exchanger  10  with three hot pipes  30  and three cold pipes  20 , all of the same diameter, sufficient to avoid blocking due to scale formation. Hot pipes  30  and cold pipes  20  are arranged in the same manner. 
       FIG. 4  shows a heat exchanger  10  containing a hot pipe  31  separated from cold pipe  21  by a baffle  59  in the form of a metal plate. Hot pipe  31  and cold pipe  21  have the same diameter. Baffle  59  increases the heat load at which a flooding point is reached by directing the vapour in such a way as to “push” the condensate towards the outer perimeter of the outer shell  11  and through small gap  59   a;  thus, minimising the impact of vapour velocity on flooding the heat exchanger  10 . The condensate will tend to return by gravity to the base of the outer shell  11  via the small gap  59   a  purposefully disposed between the baffle  59  and the outer shell  11 . It will be understood that the dimensions of gap  59   a  may be selected to obtain the desired condensate flow behaviour. 
       FIG. 5  shows a heat exchanger  10  having three hot pipes  32  and three cold pipes  22 , all having the same diameter. Baffles  60 ,  61  and  62  separate the hot pipes  32  from the cold pipes  22 . Baffles  61  and  62  co-operate in an arrangement aimed to increase the heat load at which a flooding point is reached by directing the vapour along a path as to “push” the condensate towards the outer perimeter of the outer shell  11 ; thus, minimising the impact of vapour velocity on flooding the heat exchanger  10 . The condensate will tend to return by gravity to the base of the outer shell  11  via small gaps  60   a  purposefully disposed between the baffles  60  and  61 ; and baffle  62  of the outer shell  11 . It will again be understood that the dimensions of gaps  60   a  may be selected to obtain the desired condensate flow behaviour. 
       FIG. 6  shows a heat exchanger  10  in which cold pipes are arranged in two discrete groups or bundles  180  and  190 , with cold pipes  182  and  192 , in this case, all having the same diameter. Bundles  180  and  190  are separated from a bundle of hot pipes  190  by baffles  165  and  166  for increasing the heat load at which a flooding point is reached. Hot pipes  172  have greater diameter than the cold pipes  182  and  192 , for example having 2″ diameter compared with 1″ diameter. Hot pipes  182  carry the scaling pregnant liquor including erosive solids. 
       FIG. 7  shows a heat exchanger  10  in which cold pipes are arranged in two groups or bundles  220  and  240 , with cold pipes  222  and  242  all having the same diameter. Bundles  220  and  240  are separated from a bundle of three hot pipes  230  by baffles  160  and  161  for increasing the heat load at which a flooding point is reached. Hot pipes  172 , which are disposed horizontally and in parallel, have greater diameter than the cold pipes  222  and  242 , for example having 2″ diameter compared with 1″ diameter. Hot pipes  230  carry the scaling pregnant liquor including erosive solids. As the heat exchangers  10  of  FIGS. 6 and 7  have similar operating conditions and the heat exchanger  10  in  FIG. 7  has more “cold” pipes  222  and  242 , the width of the outer shell  11  has to be wider to allow for the higher heat load, and thus higher volume of vapour rising with same heat transfer fluid and thus the same flooding point upward velocity. 
       FIG. 8  is an embodiment where the number of cold pipes  207  and  216  is higher than in  FIG. 7  because of more than one pass through the heat exchanger  10 .  FIG. 8  shows a heat exchanger  10  in which cold pipes are arranged in two groups or bundles  205  and  215 , with cold pipes  207  and  216  all having the same diameter. Bundles  205  and  215  are separated from hot pipes  230  by two relatively small (in comparison to volume  55 ) baffles  155  and  156  for increasing the heat load at which a flooding point is reached. Hot pipes  272 , which are disposed horizontally and in parallel, have greater diameter than the cold pipes  207  and  216 , for example having 2″ diameter compared with 1″ diameter. Hot pipes  272  carry the pregnant liquor including erosive and scaling solids. This arrangement enables the logarithmic average temperature difference (LMTD) on the cold pipes  207  and  216  to be reduced while the LMTD on the hot pipes  272  is increased compared to the heat exchanger in  FIG. 7 . 
       FIG. 9  shows a two-vessel arrangement for the heat exchanger  10  which could also be considered a heat exchanger system. Three hot pipes  127  are arranged horizontally and in parallel within hot vessel  120 . The hot pipes  127  may, for example, be 2″ in diameter. Vapour from evaporating heat transfer fluid body  134  rises through the vapour-liquid disengagement volume  315  to be carried through vapour passage  330  into cold vessel  110  which contains a bundle  115  of cold pipes  117  having, for example, 1″ diameter. This arrangement has the advantage of the vapour “pushing” the heat transfer fluid condensate towards the bottom of vessel  110 . The condensed heat transfer fluid returns to hot vessel  120  through heat transfer fluid return passage  350 . 
     While the 1″ diameter pipes, mentioned by way of example above, may carry scaling fluids, solids are either absent or very fine, for example carrying the spent liquor in an alumina refinery. Scaling may also readily be addressed by methods known in the art of shell and tube heat exchangers. Mechanical de-scaling can be avoided. 
     Conventional entrainment separators (not drawn) can be installed in the vapour-liquid disengagement volume  315  to further increase heat load at which flooding occurs. These entrainment separators could be, but not limited to, mesh and, or chicane type. Within conduit  330  further entrainment separation can be conducted (not drawn), for instance, cyclones where the separated heat transfer liquid is returned to heat transfer body  134 . 
       FIG. 10  shows a similar heat exchanger  10  to that shown in  FIG. 9  except that it has a compressor  515  on the vapour passage  520  and a restriction  505 , such as an orifice or control valve, on the condensate return passage. Hot vessel  120 A has hot pipes  537 . Cold vessel  110 A has a significantly larger number of smaller diameter cold pipes  517 . The combined deployment of compressor  515  and orifice or control valve  505  produces a higher temperature difference so the heat transfer area can be reduced or a smaller, and even a negative, temperature difference between the “hot” and “cold” streams can be handled. 
     In each of the cases described above, the disengagement zone can be designed in the same way as the disengagement zone in a conventional shell and tube reboiler, for instance the maximum vapour velocity can be defined by the Souders Brown equation : 
     
       
         
           
             V 
             = 
             
               k 
                
               
                 
                   
                     
                       ρ 
                       L 
                     
                     - 
                     
                       ρ 
                       V 
                     
                   
                   
                     ρ 
                     V 
                   
                 
               
             
           
         
       
     
     where: V=maximum heat transfer fluid vapour velocity (m/s) 
     k=constant (m/s) 
     ρ L =density of heat transfer fluid liquid (kg/m 3)    
     ρ L =density of heat transfer fluid vapour (kg/m 3 ) 
     The Souders-Brown equation constant, k can be set to 0.2 m/s similar to that used in a conventional reboiler disengagement zone. 
     The heat transfer efficiency of heat exchanger  10  is greater than achieved through conventional flash cooling and, in the context of an alumina refinery, allows a greater productivity to be achieved with a smaller plant footprint, the latter potentially reducing process plant construction cost. It will be understood that the heat exchanger could be used for other hydrometallurgical and chemical applications. 
     Modifications and variations to the heat exchanger and heat transfer process as described in the present specification may be apparent to the skilled reader of this disclosure. Such modifications and variations are deemed within the scope of the present invention.