EP1015100A4 - Absorbeur a barbotage avec remise en circulation - Google Patents

Absorbeur a barbotage avec remise en circulation

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Publication number
EP1015100A4
EP1015100A4 EP97940589A EP97940589A EP1015100A4 EP 1015100 A4 EP1015100 A4 EP 1015100A4 EP 97940589 A EP97940589 A EP 97940589A EP 97940589 A EP97940589 A EP 97940589A EP 1015100 A4 EP1015100 A4 EP 1015100A4
Authority
EP
European Patent Office
Prior art keywords
vapor
liquid
channels
upflow
compartment
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.)
Withdrawn
Application number
EP97940589A
Other languages
German (de)
English (en)
Other versions
EP1015100A1 (fr
Inventor
Donald Charles Erickson
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
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Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of EP1015100A1 publication Critical patent/EP1015100A1/fr
Publication of EP1015100A4 publication Critical patent/EP1015100A4/fr
Withdrawn legal-status Critical Current

Links

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
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/10—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically
    • F28D7/106—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically consisting of two coaxial conduits or modules of two coaxial conduits
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
    • B01J10/002—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor carried out in foam, aerosol or bubbles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B37/00—Absorbers; Adsorbers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00121—Controlling the temperature by direct heating or cooling
    • B01J2219/00128—Controlling the temperature by direct heating or cooling by evaporation of reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00162—Controlling or regulating processes controlling the pressure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/18—Details relating to the spatial orientation of the reactor
    • B01J2219/185—Details relating to the spatial orientation of the reactor vertical
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/19—Details relating to the geometry of the reactor
    • B01J2219/194—Details relating to the geometry of the reactor round
    • B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
    • B01J2219/1943—Details relating to the geometry of the reactor round circular or disk-shaped cylindrical

Definitions

  • Multi-component fluid mass exchanging apparatus and processes such as absorption, desorption, and fractional distillation are encountered in many industrially important processes such as petroleum refining, chemicals production, CO 2 scrubbing and subsequent regeneration, and absorption heat pumping.
  • Multi-component fluid mass exchanging apparatus and processes such as absorption, desorption, and fractional distillation are encountered in many industrially important processes such as petroleum refining, chemicals production, CO 2 scrubbing and subsequent regeneration, and absorption heat pumping.
  • each operating regime can be at one end only (hot end for supplied heat, cold end for extracted), in which case the remainder of the mass exchange is termed adiabatic, or the heat exchange can be all along the component, in which case it is termed diabatic.
  • each operating regime can be further distinguished according to whether the vapor is single component (non-volatile liquid absorbent) or multi- component (at least two volatile species in the liquid, i.e. volatile liquid absorbent).
  • Multi-component fluid mass exchange as presently practiced entails numerous problems and difficulties, as indicated below.
  • the exchange of mass between liquid and vapor can be conducted cocurrently, countercurrently, or crosscurrently, analogous to heat exchange processes.
  • Countercurrent mass exchange can achieve complete separations and correspondingly maximum temperature glide (the change in equilibrium temperature associated with a change in concentration).
  • Cocurrent mass exchange is severely limited both as to the degree of separation achievable and the temperature glide resulting from absorption.
  • crosscurrent mass exchange can be made to approach countercurrent performance.
  • the exothermic multi-component fluid mass exchanging processes i.e. those in which there is a net transfer of mass from vapor to liquid phase, exhibit high resistance to mass transfer owing to a concentration gradient in the liquid film.
  • a concentration gradient exists in the vapor phase, which in many cases is an even greater resistance to mass transfer.
  • These effects are also present in the endothermic processes, e.g. desorption or stripping.
  • the endothermicity i.e. the supplied heat
  • the difference in concentration between the vapor and liquid phase causes large concentration gradients locally.
  • this effect is offset by the mixing effect that the moving bubbles have on the liquid film.
  • liquid recirculation causes higher liquid to vapor ratios in the boiling channels, enabling cocurrent upflow boiling while keeping the walls wetted at higher velocities, thereby causing thinner liquid films, more mixing, and more uniform temperatures.
  • Liquid recirculation has also been applied to boiling a two component mixture ( T. Fukuchi, "Development of Small-Sized Double Effect Gas Absorption Chiller/Heater," Proceedings 19th International Congress of Refrigeration Volume III b, p. 782-789, August 1995, and US Patent 4,127,993).
  • one downcomer serves one group of upflow channels, and a second one serves a second group.
  • the two groups are not pressure equalized via a common vapor space.
  • Additional examples of cocurrent upflow in the channels of an absorption cycle generator can be found in US Patents 3,254,507, 5,435,154 and elsewhere. Cocurrent upflow is also known in absorption cycle absorbers, e.g. US Patent 5,339,654.
  • Countercurrent operation in the absorber is desirable because that yields the greatest temperature glide, thus resulting in greatest temperature overlap. Larger temperature overlap makes possible more internal transfer of heat, thus increasing cycle Coefficient of Performance (COP). Countercurrent operation in the desorber is desirable as it reduces or eliminates subsequent rectification needs.
  • COP cycle Coefficient of Performance
  • tray pressure drops are cumulative, i.e. the trays are not pressure equalized via a common vapor space, and also most of the vapor must traverse most of the trays.
  • process and apparatus comprised of a series of at least three cocurrent upflow vapor liquid contacts (sorptions) which are 1 ) pressure equalized, 2) individually liquid recirculated by gravity, and/or 3) globally crosscurrent (at least two and preferably all three features are incorporated).
  • sorptions are diabatic, i.e. each contact zone is in heat exchange relationship with a heat transfer medium.
  • vapor is preferably withdrawn from the several desorptions countercurrently to the sequence in which sorbent is supplied to them.
  • heat is removed vapor is preferably fed crosscurrently to the several absorptions, preferably to the bottom of each cocurrent upflow region.
  • cocurrent upflow regions there are preferably at least ten cocurrent upflow regions, and they may number in the thousands. They are preferably horizontally arrayed and the sorbent is routed sequentially through the array in one or more parallel paths whereby the sorbent concentration changes in each member of the sequence.
  • a diabatic absorber comprised of a plurality of vapor-liquid contact compartments; a vapor injection port in the bottom portion of each compartment; a common vapor space connecting the compartments; flow openings for restricted flow of liquid into and out of each compartment; and a means for rejecting heat from each compartment.
  • an apparatus for absorbing a vapor into a liquid comprised of a plurality of channels adapted for cocurrent absorptive upflow of vapor and liquid, each channel having a vapor injection port in the bottom portion; a plurality of channels adapted for liquid downflow, wherein each of said downflow channels is in liquid communication with at least one of said absorptive upflow channels; a vapor space which interconnects the upper portions of said channels; and a vapor manifold for supplying said vapor injection ports.
  • a process for absorbing a vapor into a liquid comprising cooling a plurality of compartments; injecting vapor into a vapor-liquid upflow channel in each compartment, said upflow caused by the rising of said vapor; and recirculating the liquid within each compartment by providing a liquid downflow channel.
  • the locally cocurrent sorptions may be arranged in groups or tiers, where the vapor exiting one tier is then crosscurrently supplied to the next tier. Note that when the sorption is a desorption, the use of tiering requires that the locally cocurrent compartments of the downstream desorption tier have vapor injection ports.
  • the advantage of tiering is that the sorption process thereby more closely approaches countercurrent conditions - the disadvantage is that the vapor pressure drop accumulates from tier to tier.
  • the same effect of causing the sorption to more closely approach countercurrency can be obtained by preconditioning part of the vapor by contacting it with a small amount of sorbent before it is injected - preferably the hot, higher volatility sorbent.
  • the locally cocurrent horizontally arrayed compartments may take a variety of forms: 1 ) brazed (or welded) plate fin exchangers, wherein the flat plate members constitute the pressure boundaries between the sorption and the heating medium, and the fin members form the compartment boundaries (taller segments) and channel boundaries (shorter segments); 2) horizontal cylindrical annulus, wherein the compartment boundaries are thermally coupled flat disc fins, and curved shrouds form the channel boundaries; 3) vertical cylindrical annulus such as roll-former shapes, sheet, fin, inserts, etc., with thermally coupled vertical wall members in the annulus forming the compartment boundaries and the channel boundaries; 4) vertical fin tube members with gaseous heat exchange outside and an internal partition or concentric tube forming the channel boundaries; and 5) other comparable geometries.
  • the locally cocurrent upflow provides intensified heat and mass transfer and eliminates the need for a liquid distributor.
  • the intensification is particularly high in the slug flow and churn flow regimes, and not so high in bubbly flow, unless the bubbles are very small.
  • the bubbly flow region top portion of absorption channels
  • flow splitters e.g. lanced offset fin, which acts to break up and reduce the size of the bubbles.
  • L/V liquid-to-vapor ratios
  • the liquid recirculation via downcomers allows that ratio to increase to the desired value.
  • dividing the vapor into multiple parallel paths also increases the L/V in each channel. The more compartments there are, the less liquid recirculation within the same compartment is required, and proportionately more of the liquid is recirculated or re-elevated to the next compartment. In the limiting case, all the downcomer liquid is recirculated (re- elevated) to the next compartment.
  • the pressure equalization ensures that the total pressure drop is approximately equal to the pressure drop of a single compartment vice the accumulated pressure drops of all compartments.
  • Typical vertical dimensions of the vapor-liquid contact upflow channels range from 10 cm to 200 cm. Consider an array of 50 compartments, each 30 cm high. With pressure equalization, the pressure drop is approximately 20 cm of hydrostatic head, whereas without it the ⁇ p would be 1500 cm hydrostatic head- a clearly undesirable amount.
  • the flow of liquid sorbent through the compartments is by gravity.
  • the liquid height change necessary for gravity flow from compartment to compartment is on the order of 2 mm or less.
  • the tradeoffs between the horizontal annular configuration and the vertical annular configuration include the following. With the horizontal configuration, the cylinder diameter approximately fixes the vertical height of the riser channel, and the cylinder length fixes the number of compartments. Conversely with the vertical configuration the cylinder diameter constrains the number of compartments, and the cylinder length (height) limits the height of the riser channels. Thus when the cylinder diameter is constrained by a consideration such as pressure vessel code, and doesn't result in channels of the desired length, then the vertical configuration would be preferred.
  • the disc fins would typically be stamped from flat stock and then pressed or heat shrunk in place. The vertical fin material is readily available, easily assembled, and can be brazed or pressed in place.
  • the vertical configuration suffers more heat leakage due to the insulated idle compartment which separates the coldest compartment from the hottest.
  • that loss can be avoided by having two parallel paths for the liquid, proceeding in opposite directions around the circumference, whereby the hottest compartments are located 180° apart from the coldest ones. This is particularly valuable for a fired generator externally heated from a linear burner, whereby the hot combustion gas can impinge against the hottest side of the generator, and exit to the coldest, thus extracting more heat.
  • Figures 1 through 20 present details of the vertical annular cylindrical configuration of the invention, both as an absorber and as a desorber, plus also as a combined (GAX) apparatus ( Figures 15 and 20).
  • Figures 21 through 28 present embodiments of the disclosed invention which are realized in plate fin exchanger apparatus.
  • FIGS 29 through 37 illustrate modes of realization of the disclosed invention in horizontal annular cylindrical geometry.
  • Figures 38 through 40 illustrate the recirculating bubble absorber in a shell and tube configuration.
  • Figures 41 through 44 illustrate the recirculating bubble absorber in a modular plate fin configuration.
  • a locally cocurrent upflow diabatic absorber is depicted in an elevation cross-sectional view, with Figure 2 the corresponding cross-section viewed from above.
  • Outer vertical cylinder 1 and inner cylinder 2 jointly form an annular space which is divided into compartments by partitions.
  • the partitions may have a tee-shaped cross-section as depicted in Figure 3, with cross-member 7, perpendicular member 5, and passages 4 for liquid transport.
  • the tee-shapes may have vapor holes 6 for pressure equalization or alternatively may just be reduced in height to permit maximum vapor flow space.
  • Vapor manifold 8 is supplied from vapor supply port 9.
  • a vapor injection port 10 supplies vapor from manifold 8 into the bottom portion of each compartment.
  • the quantity of vapor in the channel decreases with height as absorption proceeds.
  • any remaining vapor separates from the liquid and joins the vapor exiting all other compartment risers via ports 6.
  • the liquid returns by gravity to the bottom portion of the compartment through a downcomer channel, i.e. the portion of the compartment which is closer to the center than is member 5.
  • Member 5 is shorter than cross member 7 both at the top and bottom, thus allowing liquid flow respectively into and out of the downcomer channel.
  • FIG. 1 and 2 can readily be adapted to sequential flow of liquid through all the compartments by incorporating insulating segment 11 in the sorption annulus, and then supplying sorbent liquid to the compartment on one side of block 11, and removing absorbed liquid from the compartment on the other side of block 11.
  • Segment 11 blocks the flow of sorbent through that section of annulus, and also provides insulation between the two different temperatures present on each side of it.
  • Vapor injection through port 10 is globally crosscurrent to this flow of liquid, while being locally cocurrent within each compartment.
  • Cooling is supplied to the diabatic absorber via concentric cooling compartment 12.
  • the cooling may be supplied equally to all compartments.
  • a blocking segment 13 may be incorporated and the cooling water supplied initially to the coldest compartment wall via supply port 14, and withdrawn from the warmest compartment wall via withdrawal port 15.
  • the tee members which form the compartment and channel partitions may be affixed in place via any desired means, e.g. welding, brazing, heat shrink, press fit, etc. Preferably they will have good thermal contact with the cooled wall and hence will enhance the overall heat transfer.
  • the vapor injection rate into each channel will preferably be large enough to cause slug flow in at least part of the channel, whereby very high transfer coefficients are obtained.
  • Figure 4 is a perspective view of a sorber similar to that depicted in Figures 1 and 2. Absorbing occurs in the annular space between outer cylinder 20 and inner cylinder 21. The annular space is divided into compartments by partitions 22, and each compartment is divided into an inner and outer channel by baffles 23. Vapor supply manifold 24 supplies vapor crosscurrently into each channel via vapor injection ports 25. All compartments are pressure equalized via connecting their vapor spaces via vapor openings 26. Sorbent liquid is supplied at port 27, traverses all compartments via liquid openings 28, and exits from port 29. Port 29 can be located at a height appropriate to maintain the desired liquid level in all compartments. Figure 4 is depicted as an adiabatic sorber, i.e.
  • heat exchange fluid could be added in contact with the inner wall, as shown in Figures 1 and 2, and/or in contact with the outer wall as will be subsequently shown. If the heat exchange fluid is a heating fluid, the Figure 4 apparatus is thereby a desorber, and vapor exit port 30 is used to withdraw described vapor countercurrently to the flow direction of the sorbent. Conversely, when the heat exchange fluid is a cooling fluid, the apparatus is an absorber (provided less volatile liquid is supplied at port 27).
  • Figures 5 and 6 are respectively elevation and plan view cross- sections of another embodiment of a diabatic absorber.
  • Outer and inner cylinders 35 and 36 define the annular space wherein sorption occurs;
  • vapor supply port 37 supplies vapor manifold 38 which is located in the same annulus;
  • partitions 39 divide the annulus into individual compartments which are all interconnected at the top by a common vapor space, and which include passages 40 for restricted flow of sorbent liquid sequentially through the compartments.
  • Sorbent liquid is supplied through port 42 and removed via port 43, where the two ports are separated by blocking segment 41.
  • Vapor injection ports 44 supply the vapor into the bottom of a riser channel in each compartment, where the riser channel is separated from an accompanying downcomer channel by baffles 45.
  • the baffle is shortened at top to allow vapor liquid separation within the compartment and at bottom so as to recirculate liquid to the riser channel.
  • the cooling is provided via jacket 46, with supply and return ports 47 and 48. Blocking segment 49 allows the coolant to flow countercurrently, thus achieving maximum temperature increase.
  • Figure 7 is a perspective view of a similarly configured absorber, except for ease of illustration the cooling jacket 50 has been moved to the inside vice outside as in Figure 6. Similar to Figure 6, Figure 7 shows the baffles 51 which separate the riser and downcomer channels as being radially oriented rather than circumferentially oriented. Thus the riser and downcomer channels are circumferentially displaced vice radially displaced as in Figures 1 and 2. This is possible for absorbers, since cooling the downcomer walls is helpful as well as cooling the riser walls. However it is not a preferred configuration for desorbers, since the heated walls are what give rise to the vapor which activates the riser channel. Figure 7 also illustrates that the vapor injecting ports 52 may be actual standpipes or tubes, i.e. more elaborate than the simple holes illustrated previously.
  • FIG 8 is a segment of a cross-sectional plan view of an adiabatic sorber which shows another approach to achieving locally cocurrent vapor- liquid upflow contact in compartments in a vertical annular configuration.
  • Rectangular plate fin material 50 as illustrated in Figure 9 is inserted in the annular space between outer cylinder 51 and inner cylinder 52.
  • the facing bi. faces of the rectangular fin have cutouts 53 at the top and 54 at the bottom, thereby defining the channel baffle.
  • Partition 55 affixed to the rectangular fin by a fastener through hole 56, e.g. a rivet, defines the channel baffle for an adjacent compartment. Holes 57 in the rectangular fin 50 allow sorbent passage.
  • FIGs 10 and 11 illustrate how a single piece of fin 60 (in this case with rounded crown vice rectangular) can also be used to create locally cocurrent upflow compartments.
  • Every other leg of the fin material has top cutouts 61 and bottom cutouts 62, thereby forming the channel baffle.
  • the opposing legs have holes 63 for restricted passage of sorbent liquid.
  • Cooling jacket 64 supplies cooling to the absorption.
  • the risers and downcomers are spaced circumferentially around the annulus between cylinders 65 and 66.
  • Figures 12 and 13 are respectively front and top cutaway views of a locally cocurrent upflow globally countercurrent diabatic desorber.
  • Vertical outer cylinder 70 and inner cylinder 71 delimit the annular space within which desorption occurs.
  • Flameholder 72 supplies heating fluid (combustion gas) to the outer wall of cylinder 70.
  • Rectangular fin 73 (also shown in Figure 14) is fitted into the annular space to form a plurality of compartments.
  • Liquid sorbent transport holes 74 are in the bottom portion of each parallel fin member. From sorbent supply port 75 the sorbent liquid traverses both directions around the annulus to annulus exit port 76, becoming hotter and more concentrated as it does so.
  • That figure is a segment of a cross-sectional plan view of a GAX component, comprised of outer cylinder 90 plus intermediate cylinder 91 , which jointly delimit an absorption annulus which contains crested fin 92 (also illustrated in Figure 16) which divides the annulus into a plurality of compartments. Cutouts 93 and 94 cause every other fin to function as a baffle separating a riser and downcomer .
  • a section of flow splitter 95 is mounted in the top section of each riser channel. This is an optional enhancement, which functions to maintain high transfer coefficients in that portion of the channel where flow has changed to bubbly flow vice slug or churn flow.
  • One preferred type of flow splitter is lanced offset fin. Sorbent flow between compartments is via cutouts 96.
  • the desorber portion of the vertical cylindrical GAX component is between cylinder 91 and inner cylinder 97.
  • Wall 91 is heated by absorption heat, and wall 97 is preferably heated by another heat source, e.g. exhaust gas from the primary flame.
  • Enhanced surface 98 is used to better extract heat from the exhaust gas
  • the desorption annulus is accordingly configured with risers at both walls, formed by the fins of rectangular fin 99, and downcomers between them, formed by the fins of rectangular fin 100. Note that any other suitable means of forming the interior downcomers could also be employed, e.g. the inserts of Figures 12, 13, and 14.
  • Figure 17 illustrates a multipass arrangement of a locally cocurrent upflow absorber.
  • the figure is one half of a front cutaway view of a vertical annular configuration, showing outer cylinder 101 inner cylinder 102, and cylinder axis 103.
  • Partitions 108 delimit the compartments on each tier, and baffles 107 separate the downcomer and riser channels within each compartment.
  • Incoming vapor is divided by divider 110 and supplied in parallel to manifolds 104 and 105.
  • FIG. 18 illustrates a multi-tiered desorber, further adapted for post- treatment of desorbed vapor.
  • Inner cylinder 114 with axis 115 is heated via enhanced heat transfer surface 116, causing desorption in three tiers of locally cocurrent upflow desorption compartments, contained by outer cylinder 117, and with the tiers separated by disc fins (flat washers) 118.
  • Partitions 119 delimit the compartments, and baffles 120 separate downcomer and riser channels.
  • Desorbed vapor is withdrawn into conduit 121 , which incorporates vapor liquid contact media 122 in the flowpath of vapor from the bottom tier, and vapor liquid contact media 123 in the flowpath of the combined vapor from the middle tier and from contact media 122.
  • the two contact media may be wetted with a small amount of feed sorbent.
  • Figure 20 presents an example of how the above described useful components - vertical annular configurations of horizontally arrayed, locally cocurrent upflow, pressure equalized sorbers (absorber, desorber, and GAX) can be configured into an overall useful process.
  • Figure 20 is a schematic flowsheet of a GAX absorption cycle apparatus, useful for space conditioning, refrigeration, and heat pumping.
  • Direct fired desorber 130 is heated by flameholder 131.
  • Strong sorbent, i.e. sorbent remaining after desorption, is withdrawn via conduit 132 and supplied to GHX 133, from whence it proceeds via pressure letdown 134 to the absorber section of GAX component 135.
  • the sorbent traverses that annulus, and vapor is countercurrently withdrawn via conduit 145.
  • the withdrawn vapor includes that desorbed as a result of the transfer of GAX absorption heat, plus preferably also the two pass vapor from desorber 130 via check valve 146 to injection manifold 147 (although it will be recognized that vapor stream could alternatively bypass the GAX component).
  • the desorbed vapor flows through check valve 149 to condenser 150, then condensate through refrigerant heat exchanger 151 to evaporator 152, and finally low pressure refrigerant vapor back through RHX 151 to vapor supply manifold 139.
  • the heat of absorption at absorber 138 is removed via cooling jacket 148.
  • the sorbent exiting pump 142 would preferably be routed also in heat exchange with absorber 138 before being sent to GAX desorber 144.
  • the disclosed invention is not limited to vertical annular configurations.
  • Figures 21 through 24 illustrate plate fin configurations (brazed, welded, or other fin attachment methods) which accomplish the same result.
  • Figure 21 is a perspective view of a brazed plate fin locally cocurrent upflow latent-to-latent heat exchanger, e.g. either an absorber-desorber (GAX component) or a rectifier-stripper (distillation component) or a scrubber- regenerator.
  • a brazed plate fin locally cocurrent upflow latent-to-latent heat exchanger, e.g. either an absorber-desorber (GAX component) or a rectifier-stripper (distillation component) or a scrubber- regenerator.
  • the vapor liquid contact occurring in sections 150 and 152 is endothermic, and that in sections 151 and 153 is exothermic, and there is heat transfer between the respective sections.
  • sorbent from an absorber and pump is supplied to compartments 150 and 152 via conduits 154 and 155, and after partial desorption in a plurality of sequential desorption compartments is withdrawn at ports 156 and 157.
  • Desorbed sorbent from the externally heated desorber is supplied to compartments 151 and 153 via supply ports 158 and 159 respectively, and is withdrawn via ports 160 (not shown) and 161 after traversing a sequential plurality of absorption compartments.
  • the vapor being absorbed is supplied via port 162 and manifold 163. Heat of absorption is transferred to the desorbing compartments, and desorbed vapor is withdrawn from those compartments countercurrently to the direction in which sorbent is routed through them, the vapor exiting at ports 164 and 165.
  • Figures 22 and 23 show internal details of the Figure 21 apparatus and are respectively a cutaway top view and cutaway front view.
  • Flat plates 166 form pressure boundaries between absorbing sections 151 ,153 and desorbing sections 150,152.
  • Rectangular fin 167 forms the individual desorbing compartment boundaries or partitions, in addition to lending strength to the overall apparatus as a result of being bonded to plates 166. The bonding also promotes heat and mass transfer.
  • Rectangular fin 168 correspondingly delineates the absorbing compartment boundaries.
  • Figure 24 provides additional detail of inserts 169. They have holes 170 at the bottom to allow liquid communication from the downcomer channel to the two riser channels. Inserts 171 have a rounded shape which promotes good slug flow transfer characteristics in the riser channels, and which also provides some spring action to hold it firmly in the compartment (e.g. until brazing). The top of the inserts are lower than the tops of rectangular fins 167 and 168, thereby delineating the vapor-liquid separation zone. Vapor injection ports 171 supply vapor from manifold 163 into each absorption riser channel. It will be recognized that either the absorber sections of Figures 21-23 or the desorber sections can be applied in other configurations - stand-alone
  • Figures 25 (cutaway elevation cross- section) and 26 (cutaway plan view) illustrate a plate fin absorber-desorber heat exchange (GAX) configuration wherein the desorber uses the same configuration of three adjacent rows of rectangular fin as in Figurel 5 to form the compartments and channels, and the absorber uses a similar arrangement.
  • Plate members 100 form the pressure boundaries between absorption zones and desorption zones, and intermediary partial plates 101, in conjunction with folded rectangular fin, form the channel boundaries.
  • Folded fin segments 102 form the absorber risers; segment 103 form the absorber downcomers; segments 104 the desorber risers; and segments 105 the desorber downcomers.
  • Each absorber riser channel has an associated vapor injection port 106.
  • the pressure boundary plates 100 usually rely on the additional strength imparted by the brazed fin members, hence it is preferred to extend the vertical fin into the vapor space and use holes 107 to accomplish pressure equalization, as shown in the absorber sections; or to incorporate a separate horizontally oriented perforated fin 108, as shown in the desorber sections. The latter permits higher vapor flow rates above the desorption zones. Similar fin material may also be incorporated in vapor manifold 109 for strengthening it.
  • the plate fin absorbers can alternatively or additionally be cooled by a sensible heat cooling medium, and similarly that the plate fin desorbers can alternatively or additionally be heated by a sensible heat heating medium, for example combustion gas.
  • the plate fin configuration can also incorporate tiering and multipassing, as illustrated by Figures 27 (front cutaway) and 28 (side cutaway).
  • Pressure boundaries 110 and 111 enclose a vertical stack of absorption tiers, each respectively fed vapor crosscurrently by vapor injection manifold 112, 113, and 114.
  • Each tier is comprised of channel baffles 115, and vapor injection ports 116.
  • Compartments are delineated by horizontal runs of folded rectangular fin with vertically oriented fins, 117.
  • the tiers are delineated by rectangular folded fin member 118, which also delineates the vapor manifolds supplying the injection ports 116.
  • Liquid sorbent advances from tier to tier through overflow pipes 119.
  • the horizontal array of locally cocurrent upflow pressure equalized compartments can be implemented in horizontal cylindrical annular configurations, in addition to the vertical cylindrical annular configurations and the plate fin configurations described above.
  • Figures 29 through 37 are directed to that arrangement
  • Figures 29 and 30 are front and side cutaway views of a diabatic absorber which has multiple horizontally arrayed locally cocurrent upflow absorption compartments which are pressure equalized.
  • Outer horizontal cylinder 120 and concentric inner cylinder 121 jointly form an annular space which is divided into a plurality of compartments by disc fins 122.
  • the fins are preferably in thermal contact with both cylinder walls, e.g. by press fit, heat shrinking, brazing, welding, or the like.
  • Each fin has a cutaway or vapor opening 123 at the top, and a liquid passage 124 preferably near the bottom.
  • the fins are spaced by curved baffles or shrouds 125, which also divide each side of each compartment into an inner and outer channel.
  • the baffles may be in the form of bent U channels, and may be affixed to the fins by pins or rods 126.
  • Figure 31 provides additional details on possible fin and baffle configurations.
  • Exterior vapor manifold 127 welded to the outer cylinder, supplies vapor to a pair of vapor injection ports 128 for each compartment. Vapor and liquid flow upward cocurrently outside baffle 125, any remaining vapor separates from the liquid above baffle 125, and the liquid recirculates to the bottom of the compartment inside baffle 125.
  • the horizontal annular configurations also have the advantage that there can be concentric heat exchange jackets both outside the outer cylinder and inside the inner cylinder. They may both contain the same heat transfer fluid, or each be different. Dependent on the desired temperature rise of the heat transfer fluid, it may be flowed cocurrently with the flow direction of liquid sorbent, or countercurrently to it.
  • cooling is supplied both via outer jacket 129 and inner jacket 130. Vapor is supplied at inlet 131 , and sorbent is supplied and withdrawn at ports 132 and 133.
  • Figures 32 and 33 are respectively front and side cutaway views of a horizontal cylindrical annular configuration of desorber.
  • Concentric outer cylinder 135 and inner cylinder 136 have annular disc fins 137 which divide the annular space into compartments.
  • Inner baffles 138 and outer baffles 139 divide each side of each compartment into three concentric channels.
  • the inner wall 136 of the inner channels in heated by flameholder 140, and hence is a desorption riser channel.
  • the outer wall 135 is heated by fluid in heating jacket 141 (e.g. GHX), and hence the outer channel is also a desorption riser channel.
  • the middle channel is thus a downcomer for both risers.
  • Sorbent enters at port 142, sequences through openings 143 in each disc fin 137, and exits at port 144.
  • the horizontal annular cylindrical configuration can also readily combine an absorber and a desorber in countercurrent heat exchange relationship, i.e. a GAX component.
  • Figures 34 through 37 illustrate that.
  • Figure 34 is a perspective view, Figure 35 a front cutaway, Figure 36 a top cutaway, and Figure 37, a side cutaway view of a globally non-cocurrent mass exchange desorber and globally crosscurrent mass exchange absorber in countercurrent heat exchange relationship.
  • outer cylinder 150 and intermediate cylinder 151 jointly define the desorption annular space
  • cylinder 151 and inner cylinder 152 define the absorption annulus.
  • the interior of inner cylinder 152 functions as the absorption vapor supply manifold, supplied via inlet port 153.
  • Hot depressurized strong sorbent is supplied to the absorption annulus at sorbent inlet port 154, and is withdrawn after absorption at exit port 155.
  • Weak cold pressurized sorbent is partially heated in an AHX and/or SCR and then fed via feed port 156 tot the colder end of the desorption annulus, then progresses sequentially to the warmer end, where it is withdrawn at withdrawal port 157.
  • Figures 35, 36, and 37 provide details of the interior construction of Figure 34.
  • Disc fins 160 form the compartments in the desorption annulus; baffles 161 provide riser and downcomer channels in each compartment to all cocurrent upflow and liquid recirculation; liquid ports 162 permit sequential flow of liquid through the compartments; and vapor injection ports 163 allow a multipass of the vapor from the exterior heated desorber.
  • baffles 165 separate the riser and downcomer channels; flow passages 166 allow sequential flow of sorbent through the compartments; and vapor injection ports 167 feed vapor to be absorbed into the riser channels of each compartment.
  • Figures 32 and 33 are respectively front and side cutaway views of a horizontal cylindrical annular configuration of desorber
  • the plate fin configuration can also incorporate tiering and multipassing, as illustrated by Figures 27 (front cutaway) and 28 (side cutaway).
  • Pressure boundaries 110 and 111 enclose a vertical stack of absorption tiers, each respectively fed vapor crosscurrently by vapor injection manifold 112, 113, and 114.
  • Each tier is comprised of channel baffles 115, and vapor injection ports 116.
  • Compartments are delineated by horizontal runs of folded rectangular fin with vertically oriented fins, 117.
  • the tiers are delineated by rectangular folded fin member 118, which also delineates the vapor manifolds supplying the injection ports 116.
  • Liquid sorbent advances from tier to tier through overflow pipes 119.
  • Desorbed vapor is withdrawn from the GAX component at exit port 169, at the low temperature end.
  • the embodiment illustrated in Figures 34 through 37 has the absorber inside the desorber, it will be recognized that that geometry could be invented, in which case exhaust gas could be routed through the inner cylinder, recouping more heat. Similarly in the configuration illustrated exhaust gas can be routed through a jacket surrounding the outer cylinder. For either of these cases the desorber compartments should have dual riser channels as illustrated in Figures 32 and 33.
  • FIG 20 the check valve 141 and level control valve 137 function to convert the GAX to a liquid heat exchanger when GAX overlap is lost. That technique applies generally to all GAX cycles, and is not limited to the locally cocurrent configurations disclosed here.
  • FIGs 38 through 40 three views (respectively side, top, and end) of a shell and tube configuration of the disclosed recirculating bubble absorber are depicted.
  • Pressure vessel shell 301 encloses U tube bundle 302, with divider plate 303 separating the two sides of the U tube bundle.
  • the tubes are affixed to tube sheet 304.
  • the tubes in the bundle are positioned by a series of baffles: taller ones 305, defining recirculation compartments, and shorter ones 306, defining weirs within each compartment which separate riser zones from downcomer zones.
  • Underneath the bundle is vapor distribution plate 307, having means for vapor injection 308 under each riser zone.
  • the vapor injectors may be valves as shown, or other known types.
  • Vapor inlet nozzles 309 supply vapor to the vapor plenum under plate 307.
  • Absorbent solution inlet port 310 and outlet port 311 provide solution in a sequential path through said compartments countercurrent to the cooling fluid flowing through U tube bundle 302 .
  • Modules 401 contain fin 402 for both strength and heat transfer enhancement. Between adjacent modules are absorbing channels comprised of riser section 403, downcomer sections 404, separator plate 405 and vapor-liquid separation section 406. Below all the modules and absorbing channels is vapor distributor plate 407 with vapor injectors beneath each riser section.
  • the injectors may be hollow core rivets as shown or other known types, e.g., valves, orifices, or bubble caps.
  • the modules are headered together at each end for connection to coolant supply and return, and coolant is flowed countercurrently to absorbents.
  • Figures 42, 43, and 44 are respectfully end, top, and side views of a more complete embodiment of the modular plate fin recirculating bubble absorber.
  • the absorbing entity between adjacent modules 420 alternates between riser channels 421 and downcomer channels 422.
  • the channels are delineated and strengthened by vertically-oriented fin, e.g. , rectangular fin.
  • the downcomer fin 423 extends below the modules, and the riser fin 424 extends above the modules.
  • Vapor distributor plate 425 directs vapor bubbles (from perforations) into the riser channels, and deflectors 426 help prevent the vapor bubbles from entering the downcomer channels while allowing liquid to pass.
  • the modules contain horizontally-oriented rectangular fin 427, (or equivalent) except at the ends where flow distribution geometry may by found, entering or exiting the headers 428.
  • Pressure vessel shell 429 can be designed such that the modular bundle of absorbing channels can be inserted in the shell and bolted at flange 430. Coolant is supplied via nozzle 431 to the lower header 428, and then exits upper header 428 to exit nozzle 432. Strong absorbent (strong in absorbing power) is supplied countercurrently to the coolant, through entrance nozzle 433 and U bend 434 into liquid distributor 435 and thence into the absorbing channels. The absorbent is withdrawn through exit port 436.
  • the vertically-oriented rectangular fin 423, 424 in the in the absorbing channels is depicted in Figure 43. With this absorbing channel geometry, the two-phase mixture from the riser channel must rise above the top of the modules to fall into adjacent downcomers; hence splash preventers 437 are helpful.

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  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Thermal Sciences (AREA)
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  • Mechanical Engineering (AREA)
  • Dispersion Chemistry (AREA)
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  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

Cet absorbeur destiné à absorber la vapeur dans un liquide sorbant comporte des cylindres verticaux (1, 2) formant un espace annulaire subdivisé en plusieurs compartiments par des cloisons, en l'occurrence des éléments transversaux (7) et des élément perpendiculaires (5). On injecte de la vapeur dans la partie inférieure de chaque compartiment par des orifices d'injection (10), ce qui donne lieu à une absorption en cocourant ascendant. Des orifices d'équilibrage (10) permettent d'équilibrer la pression dans les compartiments qui peuvent être en contact thermique par le biais d'un compartiment échangeur de chaleur (12). Le liquide s'écoule au travers des compartiments selon des trajectoires successives par des conduits pour transferts liquides (4). Cet absorbeur peut être édifié selon des configurations géométriques autres que des cylindres verticaux.
EP97940589A 1997-08-22 1997-08-22 Absorbeur a barbotage avec remise en circulation Withdrawn EP1015100A4 (fr)

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Application Number Priority Date Filing Date Title
PCT/US1997/014773 WO1999010091A1 (fr) 1997-08-22 1997-08-22 Absorbeur a barbotage avec remise en circulation

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EP1015100A4 true EP1015100A4 (fr) 2001-02-28

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US8702851B2 (en) 2012-03-02 2014-04-22 Hamilton Sundstrand Space Systems International, Inc. Heat exchanger
US8696802B2 (en) 2012-03-02 2014-04-15 Hamilton Sunstrand Space Systems International, Inc. Heat exchanger
US9155992B2 (en) * 2013-09-16 2015-10-13 Savannah River Nuclear Solutions, Llc Mass transfer apparatus and method for separation of gases
DE102016225704A1 (de) * 2016-12-21 2018-06-21 Robert Bosch Gmbh Absorbervorrichtung
IT202100021524A1 (it) * 2021-08-09 2023-02-09 Ariston S P A Scambiatore a tubo di fiamma per pompe di calore ad assorbimento

Citations (2)

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Publication number Priority date Publication date Assignee Title
EP0129272A1 (fr) * 1983-05-27 1984-12-27 FDO Technische Adviseurs B.V. Dispositif pour exécuter un procédé d'échange de matière
US5660049A (en) * 1995-11-13 1997-08-26 Erickson; Donald C. Sorber with multiple cocurrent pressure equalized upflows

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Publication number Priority date Publication date Assignee Title
FR96322E (fr) * 1968-11-26 1972-06-16 Rhone Poulenc Sa Nouveau réacteur étagé.
US3790141A (en) * 1971-07-19 1974-02-05 Creusot Loire Apparatus for producing a flow in a liquid mixture
US4329234A (en) * 1980-04-15 1982-05-11 Exxon Research & Engineering Co. Multi-stage gas liquid reactor

Patent Citations (2)

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Publication number Priority date Publication date Assignee Title
EP0129272A1 (fr) * 1983-05-27 1984-12-27 FDO Technische Adviseurs B.V. Dispositif pour exécuter un procédé d'échange de matière
US5660049A (en) * 1995-11-13 1997-08-26 Erickson; Donald C. Sorber with multiple cocurrent pressure equalized upflows

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of WO9910091A1 *

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WO1999010091A1 (fr) 1999-03-04

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