Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F28—HEAT EXCHANGE IN GENERAL
  • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
  • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
  • F28F9/02—Header boxes; End plates
  • F28F9/026—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits
  • F28F9/0265—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits by using guiding means or impingement means inside the header box
• • 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
• • 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
  • B01J19/0053—Details of the reactor
• • 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
  • B01J19/18—Stationary reactors having moving elements inside
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
  • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
  • C07C2/56—Addition to acyclic hydrocarbons
  • C07C2/58—Catalytic processes
  • C07C2/62—Catalytic processes with acids
• • 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
  • F28D7/06—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 having a single U-bend
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F28—HEAT EXCHANGE IN GENERAL
  • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
  • F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
  • F28F27/02—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus for controlling the distribution of heat-exchange media between different channels
• • 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
  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
  • B01J2219/00081—Tubes
• • 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
  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
  • B01J2219/00108—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
• • 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
  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
  • B01J2219/0011—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling involving reactant liquids

Definitions

• the invention is related to flow distributors for enhancing distribution of the reactor hydrocarbon effluent in the channel head of al ylation reactors to improve reactor refrigeration and to minimize tube fouling and corrosion.
• the invention may be applied to improve the distribution of liquid in the channel head of any heat exchanger that has a combined liquid/vapor stream entering the channel head.
• Description of Related Art In the alkylation process, isobutane is reacted with light olefins in the presence of a sulfuric or hydrofluoric acid emulsion. Depending on the carbon number and iso er configuration of the olefin molecule, a branched chain isoparaffin results whose octane number ranges from the high 80' s to 100. In the sulfuric acid process the reaction usually takes place at 4. °C (40°F) -10°C (50°F) , requiring re rigeration .
• FIG. 1 A schematic of the process known to those skilled in the art is shown in Figure 1 where liquid phase olefins 10 and isobutane 12 are continuously fed to the reactor 14 at about 4.4°C(40°F).
• An emulsion of immiscible hydrocarbon and sulfuric acid is formed in the reactor 14 by a mixing impeller 16.
• the impeller 16 also circulates the emulsion across chilling tubes (not shown) in the reactor 14.
• the emulsion is forced up from the reactor 14 through line 17 to a settler 18 where the hydrocarbon and acid phases separate.
• the acid is then returned to the reactor 14 by gravity through line 20.
• the hydrocarbon phase which contains the motor alkylate, excess isobutane, propane and normal butane, is released from the settler 18 through line 19 to a flash valve 22 and proceeds into the inlet nozzle 23 of channel head 24 of the reactor 14. From the inlet nozzle 23 of channel head 24, the hydrocarbon vapor and liquid flows through the tube bundle 26 (see Figure 2) which may comprise, e.g., 300 to 1000+ U-shaped tubes, and exits through outlet nozzle 25. Part of the excess isobutane and light hydrocarbon vaporizes as the reactor effluent flows through the U-tubes, thereby providing refrigeration to the process. The reactor effluent 30 goes to a flash drum 32.
• the vapor from flash drum 32 is compressed in compressor 34 and routed through chiller 36 and then via line 37a to separator 37.
• the propane rich stream 37c from separator 37 is fractionated in depropanizer column 38, with the LPG product stream 38a being purged from the unit.
• the liquid stream 35a from flash drum 32 is fractionated in deisobutanizer column 35.
• the bottoms alkylate 35c leaves the unit and is typically routed to gasoline blending..
• the normal butane side draw stream 35b also leaves- the unit., '
• the overhead stream 35d, rich in nonreacted isobutane is combined with the isobutane-rich stream 37b from separator 37 and stream 38b from depropanizer column 38 and recycled to reactor 14.
• the industry standard design for an alkylation reactor tube bundle assembly may comprise hundreds of U-shaped tubes.
• a typical channel head 24 with tube assembly 26 is shown in Figure 2.
• a partition 24a in the channel head 24 separates the channel head into an inlet side 23a and an outlet side 25a.
• the reactor effluent vapor/liquid flow from flash valve 22 enters through an inlet nozzle 23 and proceeds into the inlet chamber 23a of channel head 24.
• the two-phase flow enters the inlet chamber 23a of channel head 24 with reasonably high velocity, since it has already begun to flash, and will impinge on the partition 24a. No provision is made for turning the incoming flow towards the tube sheet 24b on which the tube bundle 26 is mounted.
• This same device may be used to improve the distribution of liquid in a two-phase inlet stream on the tube sheet of any similarly configured heat exchanger channel head.
• the instant invention will promote said uniform distribution.
• the uniform distribution will enhance the vaporization of the liquid and the heat transfer in the exchanger.
• an alkylation reactor comprising a shell having a channel head, said channel head having an inlet nozzle and an outlet nozzle separated by a partition, a tube sheet mounted transversely of said shell for mounting thereon a plurality of u-shaped tubes wherein said tubes traverse the length of said reactor shell from the inlet side of said channel head
• the improvement comprising:- a flow distributor mounted within the inlet side of said channel head for uniformly distributing, over the inlet side of said tube sheet, any fluid entering said inlet side of said channel head, said flow distributor having an ' inlet side for sealingly surrounding said inlet nozzle of said inlet side of said channel head, said flow distributor being a diverging horn-shaped duct adapted to turn said fluid flow from said inlet direction toward the tube sheet and toward the input side of said tubes.
• FIGURE 1 is a schematic diagram of a typical alkylation unit process flow diagram of a prior art system.
• FIGURE 2 is a cross-section of a typical industry standard design of a prior art alkylation reactor.
• FIGURE 3A is a side ⁇ elevation sectional view of a flow distributor according to the instant invention.
• FIGURE 3B is a side elevation sectional view of an alternate embodiment of a flow distributor according to the instant invention.
• FIGURES 4A and 4B are sectional views showing the details of the trip ring and aspirator slots.
• FIGURES 5A, 5B and 5C are elevational views of the flow distributor including the trip ring and angular trip bar.
• FIGURES 6A, 6B and 6C show rear, front and top views respectively of the flow distributor of Figure 3.
• FIGURE 7 is a schematic drawing of the tube sheet and tube configuration used for obtaining the data of Table 1. Description of the Invention
• a major flaw of the industry standard design described above is that it does not address flow maldistribution across the tube sheet.
• the trend in the industry is to modify the tube inlet by using restriction orifices that will increase the pressure drop. While this will increase the liquid fraction in the flow, and possibly increase the liquid drop size, it will not significantly improve flow distribution.
• the industry trend of using tube inserts might, in fact, worsen the flow maldistribution by causing the complete segregation of the vapor and liquid phases.
• Applicants' invention does not require dividing the inlet stream into a plurality of streams by means of internal vanes or baffles.
• Internal vanes and baffles have to be welded inside the channel head and are, therefore, subject to breaking off and obstructing the inlet nozzle of the reactor.
• the design of the inlet device disclosed herein can also be broadly applied to improving flow distribution to tube bundle assemblies in general, including heat exchangers.
• Applicants' invention is directed to an improvement of the alkylation reactors known in the prior art, such reactors also being sometimes referred to as the contactor.
• One of the major limitations in the alkylation process is the reactor temperature. Lowering the reactor temperature by increasing the overall heat transfer from the emulsion to the reactor effluent will allow significant increase in rates (and yield) .
• the overall heat transfer rate is, to a large extent, influenced by the degree of distribution of the vapor/liquid flow through the tubes comprising the tube bundle.
• Tubes that are liquid deficient, such as in the outside, or peripheral, tubes as known in the prior art, will have very low heat transfer rates. Therefore, a maldistributed liquid flow across the tube bundle will lead to significantly lower overall heat transfer.
• a maldistributed flow, where some of the tubes see minimal liquid and therefore run hotter, will also lead to accelerated tube corrosion and subsequently to tube leaks.
• Typical experience from alkylation units show that tube leaks are a major cause for unit shut downs and premature replacement of bundle assemblies.
• the invention disclosed herein is directed to a method and apparatus for receiving the vapor/liquid flow that emerges from the inlet nozzle and uniformly distributing it across the inlet side of the tube sheet. This is accomplished by using a flow distributor 50 as shown in Figure 3A.
• the flow distributor 50 is attached to the inlet nozzle 23 of the reactor channel head as shown in Figure 3A.
• the flow distributor 50 is welded flush to the inlet nozzle 23 inside the channel head 24.
• the internal cross section of the flow distributor 50 is similar to that of a curved funnel and changes continually from that of the inlet nozzle 23, at its inlet, to that of the tube sheet 24b (shown without tube bundle 26 attached) , at its discharge towards the tube sheet 24b as shown in Figure 3A.
• the cross-sectional area change may be either smooth or mitered in several steps as shown in Figure 3A.
• the flow distributor 50 receives the two-phase flow of reactor effluent that emerges from the inlet nozzle 23, turns it approximately 90 degrees while allowing it to diverge and delivers a uniform mixture across the inlet tubes (not shown) of the tube sheet 24b.
• a separation 53 is maintained between the face of the flow distributor 50 and the tube sheet 24b. This spacing 53 is required in order to allow communication of the vapor and liquid inside the horn with the remainder of channel head 24. Part of the purpose of this communication is to permit liquid that does not enter the tubes to be collected by aspiration through slots 52a, described in the following paragraph.
• the face 50b of flow distributor 50 may be placed flush against the tube sheet 24b.
• the flow that enters the channel head 24 through the inlet nozzle 23 is a mixture of vapor and liquid with a portion of the liquid being present as a film along the inside diameter of the inlet pipe and nozzle 23.
• a trip ring 52 is installed at the inlet of the flow distributor 50 as shown in Figures 3A and 3B and, in more detail, in Figure 4A.
• the trip ring 52 dislodges the liquid film and helps to break up the film into drops that are subsequently transported by the vapor through the flow distributor 50.
• Slots (or windows) 52a are cut along and through the bottom (around the circumference) of the flow distributor 50 as shown in Figures 4A and 4B.
• the slots 52a are located immediately downstream of the trip ring 52.
• the "venturi" action of the trip ring 52 aspirates any liquid, that accumulates in the bottom 24c of the channel head 24, into the flow distributor 50 through the slots 52a, thereby further enhancing the distribution of the liquid phase.
• FIGS 5A-C show aspects of the flow distributor 50, trip ring 52 and trip bar 54.
• the trip bar 54 is installed on the roof 50a of flow distributor 50 at an angle of approximately 20 - 180 degrees, preferably 120 degrees, to the direction of flow.
• the trip bar 54 breaks up the liquid film on the roof 50a of the distributor 50 and enhances the uniformity of the liquid distribution.
• the trip bar 54 may include other embodiments such as separating the bar , into discrete segments and individually installing each segment on the roof 50a. In still another embodiment, the trip bar may also be serrated with "grooves" or "notches” cut into the bar.
• Figures 6A-C show rear, front and top views, respectively, of the distributor 50.
• Applicants' invention significantly improves the distribution of vapor/liquid flow across the inlet tubes of a tube bundle 26 of alkylation reactors, compared to the industry standard.
• the distribution is accomplished by preventing the impingement of the inlet flow through inlet nozzle 23 onto the partition 24a. Instead, the flow distributor 50 changes the inlet flow direction by approximately 90 degrees while allowing expansion of the flow and directs it uniformly across the inlet side of the tube sheet 24a.
• the flow distributor 50 described herein does not rely on equally splitting the inlet flow into a plurality of streams.
• the improved flow distribution will allow the reactors to be operated at lower temperatures thereby increasing capacity and improving yield.
• better flow uniformity across the tube bundle 26 will minimize tube fouling and corrosion and, as a result, is expected to increase the life of the bundle assembly.
• the flow distributor described above was developed using detailed two-phase flow computer simulations of the process and through testing of a scale model of a commercial alkylation reactor channel head.
• Figure 7 shows a tube sheet with the tube layout arrangement used to obtain the data of Table 1.
• the two-phase vapor/liquid flow into the channel head 24 and across the tube sheet was simulated for the existing design (prior art) and with the newly conceived flow distributor 50.
• a marked improvement in distribution of the flow across the tube bundle is seen with the current invention as shown in Table 1.
• the liquid distribution across the tube sheet was determined by measuring the liquid flow rate out of each tube from the scale model.
• the scale model consisted of a tube assembly of 48 tubes arranged as shown in Figure 7. Table 1 shows the liquid flow rates from each row of tubes expressed as a percentage of the total liquid at the inlet to the channel head.

Landscapes

• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Engineering & Computer Science (AREA)
• Physics & Mathematics (AREA)
• Thermal Sciences (AREA)
• Mechanical Engineering (AREA)
• General Engineering & Computer Science (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
• Details Of Heat-Exchange And Heat-Transfer (AREA)
• Physical Or Chemical Processes And Apparatus (AREA)

Priority Applications (6)

Applications Claiming Priority (2)

Publications (1)

Family

ID=28790811

Family Applications (1)

Country Status (10)

Families Citing this family (11)

Citations (2)

Family Cites Families (10)

• 2002
  • 2002-04-16 US US10/123,767 patent/US6863121B2/en not_active Expired - Fee Related
• 2003
  • 2003-04-16 EP EP03726291A patent/EP1506055A1/en not_active Withdrawn
  • 2003-04-16 MX MXPA04010022A patent/MXPA04010022A/es not_active Application Discontinuation
  • 2003-04-16 AU AU2003231529A patent/AU2003231529B2/en not_active Ceased
  • 2003-04-16 CA CA002482925A patent/CA2482925A1/en not_active Abandoned
  • 2003-04-16 CN CNB03808581XA patent/CN1327947C/zh not_active Expired - Fee Related
  • 2003-04-16 KR KR1020047016672A patent/KR20050060030A/ko not_active Ceased
  • 2003-04-16 EA EA200401375A patent/EA006358B1/ru not_active IP Right Cessation
  • 2003-04-16 WO PCT/US2003/011555 patent/WO2003089134A1/en not_active Ceased
  • 2003-04-16 JP JP2003585876A patent/JP2005526884A/ja active Pending

Patent Citations (2)

Also Published As

Similar Documents

Legal Events