US3759318A - Contactor improvements - Google Patents

Contactor improvements Download PDF

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Publication number
US3759318A
US3759318A US00234827A US3759318DA US3759318A US 3759318 A US3759318 A US 3759318A US 00234827 A US00234827 A US 00234827A US 3759318D A US3759318D A US 3759318DA US 3759318 A US3759318 A US 3759318A
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United States
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portions
tube
shell
internal diameter
impeller
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US00234827A
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English (en)
Inventor
D Putney
J Lindau
C West
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STRATFORD ENG CORP
STRATFORD ENGINEERING CORP US
Graham Engineering Corp
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STRATFORD ENG CORP
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Assigned to GRAHAM ENGINEERING CORPORATION reassignment GRAHAM ENGINEERING CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: PLAZA BANK & TRUST COMPANY OF KANSAS CITY
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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
    • F28D7/06—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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/60—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis
    • B01F27/71—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with propellers
    • B01F27/711—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with propellers co-operating with stationary guiding means, e.g. baffles
    • B01F27/7111—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with propellers co-operating with stationary guiding means, e.g. baffles the guiding means being tubes surrounding the propellers
    • 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
    • B01J14/00—Chemical processes in general for reacting liquids with liquids; Apparatus specially adapted 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1868—Stationary reactors having moving elements inside resulting in a loop-type movement
    • B01J19/1875—Stationary reactors having moving elements inside resulting in a loop-type movement internally, i.e. the mixture circulating inside the vessel such that the upwards stream is separated physically from the downwards stream(s)
    • 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
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00083—Coils
    • 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
    • B01J2219/182—Details relating to the spatial orientation of the reactor horizontal

Definitions

  • ABSTRACT An improved, horizontal, continuous contactingmixing device utilizing internal circulation and having therewith an impeller, a circulation tube and (usually) an indirect heat exchanging tube bundle; an improved type of horizontal circulating, mixing, reaction vessel or contactor; in a horizontal contactor vessel where the impeller is received in lesser internal diameter shell and circulating tube zones, offsetting the cones of the outer shell and circulation tube downwardly at the impeller end of the vessel, thereby to cure fluid flow deficiencies by removing tee necessity of lifting upwardly into the [56] References Cited impeller circulating liquids or fluids; reshaping both the UNITED STATES PATENTS circulation tube and outer shell of a horizontal contac- 2 774 654 12/1956 Reed 23/285 tor-type reaction vessel in the transition zone between z b 7/1957
  • a contactor is typically a high volume vessel with a high velocity internal circulation rate.
  • the contactor is a device for carrying out chemical reactions under conditions providing intimate contact between reactants, whether in a single phase or more than one phase.
  • a mixingcirculating impeller provides very high shear and turbulence to bring reactants into intimate contact so that the reaction can occur at a maximum rate.
  • the requirements for efficient reaction include l) temperature control with concurrent removal or addition of reaction heat, (2) intimate contact between the reactants and (3) control of the reaction time.
  • additional requirements include phase dispersion and a homogeneity of the reaction mix.
  • this type of reactor may be readily equipped with heat exchange means for the addition or removal of reaction heat thereby to maintain essentially isothermal conditions throughout the reaction zone. High internal circulation is maintained so that any heat generated or required by the reaction may be compensated by heat exchange and the reaction may be accomplished under isothermal conditions.
  • the contactor may be used with a number of combinations of phases.
  • it is effective for reactions taking place in a single liquid phase, and two or more immiscible liquid phases, with a combination of liquid and solid phases, gas-liquid phases, or gasliquid-solid phases.
  • the impeller accomplishes very complete dispersion of one phase in the other and provides an homogeneous mixture of the phases throughout the reaction zone. In these latter cases, the reaction not only proceeds at the phase boundry and a finely divided dispersion of the discontinuous phase for most of the completion of the reaction.
  • the contactor shell serves to contain the reaction mixture.
  • the circulation tube serves to establish an internal flow path in the contactor (down the center of the circulation tube and thereafter throughout the annulus between the circulation tube and the shell).
  • the hydraulic head contains shaft sealing means and any required bearings for the impeller shaft, also incorporating a reversal zone for the flow leaving the impeller (or going to the impeller if the flow is reversed).
  • the impeller efiects mixing and circulation in the contactor.
  • Indirect heat exchanging means containing a heat exchanging medium.
  • a heat exchanging medium Generally shown as a tube bundle for addition or removal of heat absorbed or generated during the reaction.
  • the bundles may be of the U-tube type, bayonet tube or others.
  • Also sometimes used for heat exchange are jacketed shells and jacketed circulation tubes.
  • the conventional flow path within the contactor is through the reversal area in the hydraulic head, thereafter through the annular space between the circulation tube and the outer shell, thereafter through a reversal area in the opposite end of the contactor, and, finally through the center section of the contactor within the circulation tube back to the impeller.
  • the reactants are normally fed as near as possible to the eye of the impeller so that they are immediately and thoroughly mixed and dispersed into the main body of the reaction mix.
  • the contactor may be advantageous to reverse the flow within the contactor, thus going first through the center section within the circulation tube, into a first reversal zone at the end of the circulation tube opposite that containing the impeller and then back through the annular space between the circulation tube and the shell into the hydraulic head, thence into the other side of the impeller.
  • the reactants are conventionally fed into the annular space between the shell and circulation tube as near as possible to the impeller.
  • olefin feed, isobutane recycle and acid recycle feeds enter the contactor immediately before the impeller through suitable nozzles.
  • the emulsion After mixing in the impeller, the emulsion thereafter flows through the annular space outside of the circulating tube and then down past the cooling tubes inserted in the opposite end of the circulating tube from the impeller.
  • Take-off of the mixture going to the acid settler may be through a nozzle drawing from the top annular space or the bottom annular space. Samples taken from the top side nozzle show a higher hydrocarbon content than samples taken from the bottom side nozzle.
  • inspection of the individual tubes of the tube bundle and experience with leading tubes indicate that most of the erosioncorrosion of tubes occurs in the upper portion thereof.
  • the cones of both the outer shell and the circulation tube are offset downwardly so that the fluids moving toward the impeller within the circulation tube have a straight path to the lower side of the impeller or drain directly into same. Therefore, it is unnecessary to lift any of the circulating emulsion into the impeller. This description is true even in the case of reversed circulation in that there is less lift in the annulus upwardly to the impeller. This results in an increase in velocity of the circulating mixture moving from the tube bundle to the impeller in the lower part of the tube bundle which in turn decreases the velocity through the upper portion thereof. Thus it is seen that the velocity of circulation throughout the entire unit tends to equalize.
  • An object of the invention is to provide improvements in circulating, mixing reaction vessels of the contactor type which typically utilize internal circulation involving an impeller, a circulation tube and (usually) a heat exchange tube bundle.
  • Another object of the invention is to provide improvements in the shaping and configuration of both the outer shell and the internal circulation tube in circulating mixing reaction vessels of the contactor type operating to cure fluid flow deficiencies which have become evident in very large volume conventional vessels of this type.
  • Another object of the invention is to provide improved contactor reaction vessel structural configurations directed to the outer shell and concentric circulation tubes therewithin which regularize, equalize and advantageously control the relative velocities of flow both within the annulus between the shell and the circulating tube (both upper and lower portions) and, se-
  • Another object of the invention is to reshape both the circulation tube and outer shell of a contactor reaction vessel in the transition zone between the lesser internal diameter portions thereof which conventionally house the mixing and driving impeller and the larger outer diameter portions thereof which conventionally usually include a large indirect heat exchanging tube bundle, this improvement and modification involving shaping the transition zone, in a horizontal contactor, into an offset cone shape, or ofiset frusto-conical configuration.
  • Another object of the invention is to remove the necessity from large circulating reaction and mixing vessels of the contactor type, of lifting upwardly into the impeller the circulating liquids or fluids from the lower portion of the heat exchanger or tube bundle (if the circulation is down the tube bundles to the impeller) or same upwardly in the outer annulus (if the circulation in the vessel is in the other direction).
  • Another object of the invention is to provide, within the circulating tube of an improved contactor type circulating, mixing reaction vessel a novel configuration or geometry wherein the reaction components or inputs into the contactor are so placed as to optimize their mixing with the circulating reaction product within the shell.
  • FIG. 1 is a sectional plan view of the improved contactor-reactor.
  • FIG. 2 is a side sectional view of the device of FIG. 1, the improved contactor-reactor.
  • FIG. 3 is a view taken along the lines 3-3 of FIG. 2 in the direction of the arrows.
  • FIG. 4 is a view taken along the line 4-4 of FIG. in the direction of the arrows.
  • FIG. 5 is a sectional plan view of a modification of the improved contactor reactor.
  • FIG. 6 is a side sectional view of the device of FIG.
  • FIG. 7 is a view taken along the line 77 of FIG. 6 in the direction of the arrows.
  • FIG. 8 is a view taken along the line 8-8 of FIG. 6 in the direction of the arrows.
  • BASIC CONTACTOR STRUCTURE Referring to the figures, the structure will be first generally described with respect to parts common to all horizontal contactor-reactors of its class, and, thereafter, the particular improvements comprising the instant invention described.
  • the horizontal contactor reactor therein shown comprises an outer shell generally designated 10, same closed at one end by a tube sheet 11 and at the other end by an hydraulic pumping head 12.
  • a circulating tube generally designated 13
  • Heating or cooling elements generally designated 14
  • U-bends made of tubing are rolled into or otherwise attached to tube sheet 11. These elements extend through the open end of circulating tube 13 to the left in FIGS. 1 and 2 and occupy an appreciable portion of the space enclosed by the circulating tube.
  • a tube bundle of alternative form such as those seen in Putney U.S. Pat. No. 2,800,307, supra, may be optionally provided as an alternative to that form shown.
  • a typical heat exchange channel or cover 15 equipped with a central partition or bafile 16 is provided for distribution of heating or cooling medium to the tubes of tube bundle 14.
  • a pumping impeller (generally designated 17) is located in the open end of circulating tube 13 at the end thereof opposite that receiving tube bundle l4. Impeller 17 is mounted on shaft 18 rotating in a bearing 19 in pumping head 12, sealed by suitable packing glands. Impeller 17 is driven by any suitable prime mover 20, such as a driving motor, turbine or engine, diagramatically illustrated.
  • Horizontal nozzles 21 and 22 are provided for feeding components of the blend or mixture into the contactor-reactor.
  • Nozzles 21 and 22 extend both through the outer shell and inner circulating tube whereby to discharge the reaction mixture components immediately in front of (typically on the upstream side) impeller 17.
  • Impeller 17 is thus arranged for taking suction from circulating tube 13 and discharging into hydraulic head 12. Within the latter, the flow of fluid is reversed and directed into the annular space between the outer shell and circulating tube.
  • Nozzle 23 is provided on the outer shell for withdrawing the finished blend of components.
  • a separate drain nozzle24 is provided on the under side of the outer shell to serve in emptying the shell or machine.
  • Heat exchange channel 15 is provided with inlet connection 25 and outlet connection 26 for the heating or cooling exchange medium, whichever is being used.
  • heat exchange elements can be installed in the annular space between the circulating tube and the outer shell of the exchanger.
  • the heat exchange elements can be in the form of pipe coils, thus eliminating the tube sheet and channel construction.
  • the outer shell may be jacketed for the circulation of heating or cooling medium be-- tween the jacket and outer shell to supplement or replace the tubular or coil elements shown.
  • the circulating tube may likewise be jacketed to give a double wall construction for the circulation of heat transfer fluid therebetween, thus providing a heat exchange medium within the body of the circulating stream.
  • this is a horizontal contactorreactor with ground level seen at 27 and suitable support members for the shell provided at 28 and 29.
  • Straightening vanes to control the direction of fluid flow may be provided within the circulating tube as at 30 around the input nozzles 21 and 22 and at 31 adjacent the impeller.
  • Straightening vanes additionally may be provided within the annulus between the shell and circulating tube in the hydraulic head as at 32 in the uniform diameter portion annulus thereafter at 33, in the eccentric cone portion (to be described) as at 34 and the cylindrical annulus portion therefollowing as at 35.
  • the impeller picks up the components introduced through the nozzles and causes them to circulate as blend through the annular space between the outer shell and the circulating tube.
  • the travel of the flowing stream is reversed and the blend or mixture caused to pass through the interior of the circulating tube, at the same time being brought in heat exchanging relationship with the heat exchange elements.
  • nozzles 21 and 22 and valves provided to control the quantity of feed input elements introduced into the vessel.
  • Suitable sources of supply are also provided and suitable pipe connections thereto.
  • connections are made to heat exchange inlets at outlets 25 and 26 and valves provided to control the circulation of the heat exchanging medium into the vessel in desired quantity and at proper circulating rate.
  • the temperature of the heat exchanging medium is governed according to the requirements of the particular fluid which is being tempered.
  • Discharge pipes are in each case connected to outlets 23 and 24 equipped with suitable valves to drain off the fluids when desired.
  • each of the outer shell 10 and the circulating tube 13 therewithin have three parts. First there is a greater internal diameter portion of each, 100 and 13a. These portions are cylindrical, circular in cross section, and comprise and include the greater volume portion of the entire vessel. A second portion of each of the outer shell 10 and circulating tube 13 are designated 10c and 13c, respectively. These are concentric, relatively lesser internal diameter portions, also cylindrical and circular in cross section.
  • Frustoconical eccentric portions 10b and 13b of the outer shell and circulating tube, respectively, are concentric with one another. (Said otherwise, these are frustums of an eccentric cone.)
  • the annulus between the circulating tube and the shell, in the lower or underside portions thereof, has a straight run, the entire length of the shell and the circulation tube.
  • the annulus between the shell and the circulation tube in the upper or overhead portions thereof angles upwardly, while flaring to a greater internal diameter in the passage from the lesser diameter portions of the shell and circulating tube and 13c) to the greater diameter portions thereof 13a and 10a).
  • the lower portions of the circulating tube and outer shell, in the entire running length thereof are substantially straight line and cylindrical, whereby the annulus therebetween is of substantially uniform cross-sectional area with straight line flow therethrough.
  • the direction of flow of the fluids being mixed and heat exchanged in the horizontal contacting vessel shown is preferably as shown by the arrows within the circulating tube and the annulus therewithout.
  • FIGS. 1-4, inclusive are reapplied precisely to the same structures in FIGS. 5-8, inclusive, but primed. This is because there is no significant change in construction whatsoever between the two modifications (FIGS. 1-4, inclusive, and FIGS. 5-8, inclusive) except that, in the modification of FIGS. 5-8, inclusive, in vertical section, the underside b of outer shell 10 is somewhat downwardly angled running from the right side of the figure toward the left side as one moves away from impeller 17'. That is, comparing the construction of FIG. 6 to that of FIG. 2, in FIG. 2, the bottom wall of the outer shell 10 is perfectly flat, straight or horizontal.
  • a mixing device having an outer enclosing shell, a circulating tube positioned within said outer shell and spaced inwardly therefrom both concentrically and longitudinally whereby to provide therebetween a continuous annulus, an impeller positioned within one end of said circulating tube, driving means provided for said impeller, an output product opening in said shell and at least one input flow line for reaction mixture components extending into said shell, both the shell and circulating tube being generally horizontally oriented, the improvement which comprises the shell and circulating tube in first portions thereof being cylindrical and of relatively large inner diameter,
  • each of said shell and circulating tube also being cylindrical, of lesser internal diameter, containing the impeller and spaced from said larger internal diameter portions of the shell and circulating tube, and
  • annulus between the circulation tube and the shell, in the lower portions thereof, has a straight run the length of the shell and the circulation tube and is generally of cylindrical shape
  • An apparatus for reducing the temperature change of a blend of fluids including an elongate casing having a discharge opening,
  • animpeller at one end of the circulating tube for creating a cyclic flow of fluids through said tube and in the annular space surrounding the tube
  • third, concentric, transitional portions located between the first and second portions of offset, frusto-conical configuration
  • a device as in claim 4 including a header at the other end of the casing from the impeller and a plurality of relatively small diameter heat exchange tubes connected into said header with all of said tubes extending axially of said casing into the larger internal diameter portion of the circulating tube.
  • a mixing device having an outer enclosing shell, a circulating tube positioned within said outer shell and spaced inwardly therefrom both concentrically and longitudinally whereby to provide therebetween a continuous annulus, an impeller positioned within one end of said circulating tube, driving means provided for said impeller, an output product opening in said shell and at least one input flow line for reaction mixture components extending into said shell, both the shell and circulating tube being generally horizontally oriented, the improvement which comprises the shell and circulating tube in first portions thereof being cylindrical and of relatively large inner diameter,
  • each of said shell and circulating tube also being cylindrical, of lesser internal diameter, containing the impeller and spaced from said larger internal diameter portions of the shell and circulating tube, and
  • An apparatus for reducing the temperature change of a blend of fluids including an elongate casing having a discharge opening,
  • third, concentric, transitional portions located between the first and second portions of offset, frusto-conical configuration
  • Apparatus as in claim 11 including a header at the other end of the casing from the impeller and a plurality of relatively small diameter heat exchange tubes connected into said header with all of said tubes extending axially of said casing into the larger internal di ameter portion of the circulating tube.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
US00234827A 1972-03-15 1972-03-15 Contactor improvements Expired - Lifetime US3759318A (en)

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JP (1) JPS523615B2 (en:Method)
CA (1) CA972348A (en:Method)
DE (1) DE2301636C2 (en:Method)
GB (1) GB1356512A (en:Method)
IT (1) IT963820B (en:Method)

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3965975A (en) * 1974-08-21 1976-06-29 Stratford Engineering Corporation Baffling arrangements for contactors
US4305454A (en) * 1978-12-20 1981-12-15 Alfa-Laval Agrar Gmbh Heat exchanger with recirculation
US4872501A (en) * 1986-03-17 1989-10-10 Fmc Corporation Heat exchanger for mobile aircraft deicing machine and method of use
US20030176755A1 (en) * 2001-08-21 2003-09-18 Catalytic Distillation Technologies Paraffin alkylation
US6852902B2 (en) 2002-03-15 2005-02-08 Catalytic Distillation Technologies Method of removing entrained sulfuric acid from alkylate
US20060155156A1 (en) * 2005-01-13 2006-07-13 Catalytic Distillation Technologies Method of removing organic sulfur compounds from alkylate
US20060278568A1 (en) * 2005-06-08 2006-12-14 Catalytic Distillation Technologies Method of removing oxygenated sulfur compounds from hydrocarbons
US20070131972A1 (en) * 2005-12-14 2007-06-14 Hong-Jyh Li Semiconductor devices and methods of manufacture thereof
US20080033227A1 (en) * 2006-08-03 2008-02-07 David Campbell Graves Recovery of sulfur value in an alkylation process
US20080063593A1 (en) * 2006-09-08 2008-03-13 Catalytic Distillation Technologies Low temperature process for regenerating spent sulfuric acid
US7344692B2 (en) 2005-05-05 2008-03-18 Catalytic Distillation Technologies Process for regenerating spent sulfuric acid
US20080264601A1 (en) * 2004-04-23 2008-10-30 Aarbuskarlshamn Denmark A/S Method, Apparatus, System And Heat Exchanger For Increasing the Temperature Of A Substance Which Is Initially In An At Least Partly Solidified State In A Container
WO2010107881A1 (en) 2009-03-17 2010-09-23 Dow Global Technologies, Inc. Tube-side sequentially pulsable-flow shell-and-tube heat exchanger apparatus, system, and method
WO2014176581A1 (en) * 2013-04-26 2014-10-30 E. I. Du Pont De Nemours And Company Improved continuous mixing reactor and method of use
CN105536676A (zh) * 2016-01-28 2016-05-04 兰州寰球工程公司 一种设有循环酸进料分布管的卧式烷基化反应器
WO2019046554A1 (en) 2017-08-31 2019-03-07 E. I. Du Pont De Nemours And Company CONVERTING A HYDROGEN FLUORIDE ALKYLATION UNIT TO A SULFURIC ACID ALKYLATION UNIT AND THE CORRESPONDING APPARATUSES

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US10486131B2 (en) 2017-10-26 2019-11-26 Chevron U.S.A. Inc. Integrated reactor system for ionic liquid-catalyzed hydrocarbon conversion

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Publication number Priority date Publication date Assignee Title
US2800307A (en) * 1954-06-04 1957-07-23 Stratford Eng Corp Apparatus for controlling temperature change of blends of fluids or fluids and finely divided solids
US3284537A (en) * 1965-01-14 1966-11-08 Stratford Eng Corp Method of charging reactants through concentric feed tubes

Cited By (36)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3965975A (en) * 1974-08-21 1976-06-29 Stratford Engineering Corporation Baffling arrangements for contactors
US4305454A (en) * 1978-12-20 1981-12-15 Alfa-Laval Agrar Gmbh Heat exchanger with recirculation
US4872501A (en) * 1986-03-17 1989-10-10 Fmc Corporation Heat exchanger for mobile aircraft deicing machine and method of use
US6995296B2 (en) 2001-08-21 2006-02-07 Catalytic Distillation Technologies Paraffin alkylation
US7250542B2 (en) 2001-08-21 2007-07-31 Catalytic Distillation Technologies Paraffin alkylation
US20040260136A1 (en) * 2001-08-21 2004-12-23 Smith Lawrence A. Paraffin alkylation
US20030176755A1 (en) * 2001-08-21 2003-09-18 Catalytic Distillation Technologies Paraffin alkylation
US6858770B2 (en) 2001-08-21 2005-02-22 Catalytic Distillation Technologies Paraffin alkylation
US20040171901A1 (en) * 2001-08-21 2004-09-02 Smith Lawrence A. Paraffin alkylation
US20050113624A1 (en) * 2001-08-21 2005-05-26 Catalytic Distillation Technologies Paraffin alkylation
US7319180B2 (en) 2001-08-21 2008-01-15 Catalytic Distillation Technologies Paraffin alkylation
US20050085679A1 (en) * 2002-03-15 2005-04-21 Catalytic Distillation Technologies Method of removing entrained sulfuric acid from alkylate
US7126038B2 (en) 2002-03-15 2006-10-24 Catalytic Distillation Technologies Method of removing entrained sulfuric acid from alkylate
US6852902B2 (en) 2002-03-15 2005-02-08 Catalytic Distillation Technologies Method of removing entrained sulfuric acid from alkylate
EP2258673A1 (en) 2002-08-15 2010-12-08 Catalytic Distillation Technologies Paraffin alkylation
US8746961B2 (en) * 2004-04-23 2014-06-10 Aarhuskarlshamn Denmark A/S Method, apparatus, system and heat exchanger for increasing the temperature of a substance which is initially in an at least partly solidified state in a container
US20080264601A1 (en) * 2004-04-23 2008-10-30 Aarbuskarlshamn Denmark A/S Method, Apparatus, System And Heat Exchanger For Increasing the Temperature Of A Substance Which Is Initially In An At Least Partly Solidified State In A Container
US8734005B2 (en) 2004-04-23 2014-05-27 Aarbuskarlshamn Denmark A/S Method, apparatus, system and heat exchanger for increasing the temperature of a substance which is initially in an at least partly solidified state in a container
US7119244B2 (en) 2005-01-13 2006-10-10 Catalytic Distillation Technologies Method of removing organic sulfur compounds from alkylate
US20060155156A1 (en) * 2005-01-13 2006-07-13 Catalytic Distillation Technologies Method of removing organic sulfur compounds from alkylate
US7344692B2 (en) 2005-05-05 2008-03-18 Catalytic Distillation Technologies Process for regenerating spent sulfuric acid
US20060278568A1 (en) * 2005-06-08 2006-12-14 Catalytic Distillation Technologies Method of removing oxygenated sulfur compounds from hydrocarbons
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DE2301636A1 (de) 1973-09-27
JPS492776A (en:Method) 1974-01-11
GB1356512A (en) 1974-06-12
IT963820B (it) 1974-01-21
JPS523615B2 (en:Method) 1977-01-28
CA972348A (en) 1975-08-05
DE2301636C2 (de) 1984-09-27

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