WO2001078890A2 - Cuve de reaction a temperature regulee - Google Patents

Cuve de reaction a temperature regulee Download PDF

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Publication number
WO2001078890A2
WO2001078890A2 PCT/US2001/011971 US0111971W WO0178890A2 WO 2001078890 A2 WO2001078890 A2 WO 2001078890A2 US 0111971 W US0111971 W US 0111971W WO 0178890 A2 WO0178890 A2 WO 0178890A2
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WO
WIPO (PCT)
Prior art keywords
reaction vessel
isothermal
isothermal mixing
channel coil
mixing baffle
Prior art date
Application number
PCT/US2001/011971
Other languages
English (en)
Other versions
WO2001078890A3 (fr
Inventor
José P. ARENCIBIA, Jr.
Original Assignee
Arencibia Jose P Jr
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from US09/548,511 external-priority patent/US6955793B1/en
Application filed by Arencibia Jose P Jr filed Critical Arencibia Jose P Jr
Priority to AU2001255341A priority Critical patent/AU2001255341A1/en
Publication of WO2001078890A2 publication Critical patent/WO2001078890A2/fr
Publication of WO2001078890A3 publication Critical patent/WO2001078890A3/fr

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Classifications

    • 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
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • 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
    • 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
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/04—Pressure vessels, e.g. autoclaves
    • B01J3/046—Pressure-balanced vessels
    • 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
    • F28D1/00—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators
    • F28D1/06—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with the heat-exchange conduits forming part of, or being attached to, the tank containing the body of fluid
    • 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
    • B01J2219/00078—Fingers
    • 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
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/0009—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
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00094—Jackets
    • 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
    • B01J2219/0015—Controlling the temperature by thermal insulation means
    • B01J2219/00155—Controlling the temperature by thermal insulation means using insulating materials or refractories

Definitions

  • the present invention relates to chemical or biological reactors generally, and in particular to an apparatus for controlling the temperature within a chemical reactor.
  • Temperature control of a chemical reaction is often the key to obtaining desired products. Where the temperature is controlled, generally the reaction kinetics are controlled. Where the reaction kinetics are controlled, undesired intermediates and byproducts can be diminished or avoided.
  • Traditional temperature control of industrial reactors is generally attained in one of two ways. One method is to control the temperature of the reactants as they enter the reactor. This method fails to address the heat of reaction, which is often responsible for the majority of heat produced or absorbed in a reaction. The heat of reaction can then alter the temperature of the reactants to produce undesirable products. This is especially true for tank reactors.
  • a second method of temperature control of industrial reactors involves the placement of a jacket around the outside of the reaction vessel. In such a case, a fluid of desired temperature is passed through the jacket, thereby cooling or heating the reaction medium. The effectiveness of the jacket is limited by heat transfer properties which are in turn limited by mechanical design characteristics and geometry, including specifically vessel diameter and length.
  • the temperature of the jacket fluid is calculated based on heat transfer requirements for a given reaction medium and reactor design.
  • the required jacket fluid temperature is often below the freezing point of the reactor medium.
  • the reactor contents can freeze along the inside of the reactor wall.
  • the formation of "ice” results in a thicker wall overall and decreased heat transfer efficiency, as well as potentially inconsistent reactor medium composition, and in some cases, destruction of some reactants or products through freezing.
  • the present invention is an insulated chemical or biological reactor (such as a fermenter) system comprising a reaction vessel, an evacuated insulation shell, a plurality of temperature controlling mixing baffles immersed in the reactor contents and a temperature controlling helical channel coil outside of the reactor but inside the evacuated shell.
  • a device designed to control the separation of phases of the working fluid chosen is required and may be external to the reactor. This device is referred to as the phase separator and has two outlets, one for each phase of the working fluid.
  • the temperature controlling mixing baffles are designed to accept the working fluid in a single phase proceeding from one outlet of the phase separator and to, in turn, cause this fluid to change phase therein without carryover of any of the inlet fluid in the evolved phase.
  • the changing of phase of the working fluid in the temperature controlling mixing baffles takes place at a uniform temperature, the level of which is dictated by the thermodynamic properties of the working fluid selected.
  • the temperature controlling mixing baffles are referred to as isothermal mixing baffles.
  • the channel coil is adapted to accept a circulating fluid, specifically of a single phase evolved by the mixing baffles and the other outlet of the phase separator.
  • the particular working fluid selected depends on the intended temperature control purposes, that is whether heating or cooling is desired and the degree of heating or cooling needed.
  • the channel coil is affixed to the outside wall of the reactor in a helical configuration and adapted to receive the single phase of the working fluid evolved by the mixing baffles and the other outlet of the phase separator which flows spirally upward or downward around the outside of the reactor.
  • the channel coil is shaped to have two straight, parallel sides of the coil in contact with the reactor, normal to the surface of the outside wall of the reactor. This right angle contact between the channel coil and reactor wall increases the section modulus of the vessel wall, and thereby increases the mechanical strength of the reactor wall under external pressure. The wall can thus be made thinner to promote better heat transfer across the wall.
  • the reactor, including the mixing baffles and the affixed coil are together enclosed within an evacuated jacket.
  • the separation of the phases of the working fluid is very important for the optimal and predictable operation of the present invention, particularly when cooling of the reactor contents is anticipated.
  • the isothermal cooling baffles are intended to boil the working fluids which enter as a liquid and evolve only a saturated vapor with no liquid carryover in the form of droplets or mist.
  • the isothermal mixing baffles therefore, operate in the boiling heat transfer regime exchanging the latent energy of vaporization (at constant temperature) with the reactor contents.
  • the vapor evolved from the isothermal mixing baffles, as well as the vapor evolved from the phase separator upstream therefrom is commingled and directed to enter the helical channel coil that serves as the reactor external jacket, wherein it exchanges sensible thermal energy with the reactor contents, gaining temperature to approach that of the reactor contents as it travels further along the inside of the coil.
  • the present invention thus controls heat transfer regimes by assuring that distinct single phases will exist in the isothermal mixing baffles (boiling liquid for cooling mode; condensing vapor for heating mode) and helical channel coil (vapor increasing in temperature for cooling mode; liquid decreasing in temperature for the heating mode).
  • the isothermal mixing baffles are vertically oriented, elongated, generally cylindrical devices with an inlet and an outlet.
  • the isothermal mixing baffles may be used for heating or cooling the contents of the reaction vessel. Where heating is desired, a hot liquid or gas can be introduced into the isothermal mixing baffles through the inlet. The resultant cooler liquid or condensed vapor or liquid can be removed via the outlet. Where cooling is desired, upstream of the isothermal mixing baffles inlet there is provided a phase separator to insure only a liquid stream enters the isothermal mixing baffles.
  • the inlet to the isothermal mixing baffles is typically placed into the top of the reactor and a liquid of desired boiling point is allowed to enter the isothermal mixing baffles while the reactor is in use. Where cooling is desired, the liquid selected would have a boiling point at or below the desired reaction temperature.
  • the heating and boiling of the liquid introduced into the isothermal mixing baffles provides for the removal of heat from the reactor contents.
  • the vapor produced from the boiling of the isothermal mixing baffles contents may be taken from the top of the isothermal mixing baffles, comingled with gas emanating from the phase separator and passed through the channel coil surrounding the outside of the reaction vessel.
  • the isothermal mixing baffles are designed and arranged so that their combined cross- sectional area will be such that the velocity of the vapor evolved from the liquid phase boiling therein will be below a critical value, Uc, above which droplets or slugs of the liquid phase will be entrained in the evolved gas and expelled from the isothermal mixing baffles.
  • Uc a critical value
  • the inlets and outlets of the isothermal mixing baffles will be piped in parallel.
  • the present invention is an insulated chemical reactor comprising; a reaction vessel having a wall with inner and outer surfaces, an evacuated insulation shell spaced apart from and surrounding the reaction vessel, at least one isothermal mixing baffle disposed within the reaction vessel, a phase separator in fluid communication with the baffle so that only one saturated or sub-cooled liquid phase of a heat transfer working fluid enters the isothermal mixing baffle, a temperature controlling helical channel coil fixed to the outer surface of the wall of the reaction vessel, the helical channel coil having at least two walls disposed normal to the outer surface of the wall of the vessel, thus defining an open helical channel coil fixed to the wall of the vessel, the helical channel coil having a winding pitch so that successive coils of the channel coil are spaced apart from each other, thus defining a closed path to receive a fluid to contact the wall of the reaction vessel, the wall of the reaction vessel being of a thickness less than that required for use under a given temperature and pressure regime, the channel coil serving to add structural strength to the wall of the
  • the present invention is an apparatus for isothermally cooling contents of a reaction vessel having a top and bottom, by allowing a saturated or subcooled liquid to boil inside an isothermal mixing baffle immersed in the reactor contents, to produce gas inside the isothermal mixing baffle, comprising; a vertically oriented, elongated generally cylindrical isothermal mixing baffle having a top and a bottom, the isothermal mixing baffle immersed in the contents in the reaction vessel, means for introducing the liquid into the top of the isothermal mixing baffle to a predetermined level, means for removing gas from the isothermal mixing baffle, and, means for controlling the level of liquid in the isothermal mixing baffle.
  • the present invention is an apparatus for supplying saturated or superheated gas to a temperature controlling helical channel coil disposed helically around a reaction vessel, comprising; an isothermal mixing baffle, immersed in contents contained in the reactor, as mixing baffle containing a saturated or subcooled liquid, means for supplying vapor discharged from the isothermal mixing baffle to the helical channel coil, means for monitoring flow of the vapor into the helical channel coil, and, means for controlling flow of vapor into the helical channel coil.
  • the present invention is a method for controlling the temperature in a reaction vessel comprising the steps of; disposing a helical channel temperature control coil around an outside surface of the reaction vessel, introducing a heat transfer working fluid into a phase separator, withdrawing a liquid portion of the working fluid from the phase separator and introducing the liquid portion into an isothermal mixing baffle disposed in contents contained in the reaction vessel, withdrawing a vapor portion of the working fluid from the phase separator and mixing it with a vapor phase working fluid withdrawn from the isothermal mixing baffle to produce a mixed heat exchange fluid; and introducing the mixed heat exchange fluid into said helical channel coil.
  • FIG 1A is a flow diagram that depicts the flow scheme of the present invention in a cooling mode for the phase separator and the reaction vessel, which contains internal isothermal mixing baffles and an external helical channel coil.
  • FIG IB is a flow diagram that depicts the flow scheme of the present invention in a heating mode for the phase separator and the reaction vessel, which contains internal isothermal mixing baffles and an external helical channel coil.
  • FIG. 2A is a side view of a reaction vessel having a cylindrical cross-sectional shape with an external channel coil according to the present invention.
  • FIG. 2B is a side view of reaction vessel with an external channel coil according to an alternate embodiment of the present invention.
  • FIG. 3 A is a cross-sectional view of the generally cylindrical reaction vessel of Figure 2A with an external helical channel coil, and integral isothermal mixing baffle entering the reactor vessel from the top in accordance with the present invention.
  • FIG. 3B is a cross-sectional view of the reaction vessel of Figure 2B with an external helical channel coil, and integral isothermal mixing baffle entering the reactor vessel from the top.
  • FIG. 4 is a cross-sectional view of a reaction vessel with an external channel coil, integral isothermal mixing baffle entering the reactor vessel from the top and evacuated jacket, in accordance with the present invention.
  • FIG. 5 A is a partial cross-sectional view of an isothermal mixing baffle according to the present invention with circular cross-section the isothermal mixing baffle shown entering the reactor vessel from the top.
  • FIG. 5B is a partial cross-sectional view of an isothermal mixing baffle according to the present invention with circular cross-section, the isothermal mixing baffle shown entering the reactor vessel from the bottom.
  • FIG. 5C is an alternate embodiment of the device of FIG. 5 A and 5B, showing the use of an internal snubber made to be removable from outside the reactor vessel without disturbing the reactor vessel contents or evacuated shell.
  • FIG. 5D is an alternate embodiment of the device of FIG. 5B showing the use of an internal snubber made to be removable from outside the reactor vessel without distributing the reactor vessel contents or evacuated skill.
  • FIG. 5E is a horizontal cross-sectional view of an alternate embodiment of the cross- sectional shape of the device of FIG. 5A.
  • FIG. 5F is a horizontal cross-sectional view of an alternate embodiment of the cross- sectional shape of the device of FIG. 5B.
  • FIG. 6A is a cross-sectional view of the reaction vessel with external channel coil, evacuated jacket, and integral isothermal mixing baffle according to the present invention showing the integral isothermal mixing baffle entering the reactor vessel from the top.
  • FIG. 6B is a cross-sectional view of the reaction vessel with affixed channel coil, evacuated jacket, and integral isothermal mixing baffle according to the present invention, showing the integral isothermal mixing baffle entering the reactor vessel from the bottom.
  • FIG. 7A is a partial cross-sectional view of the reaction vessel with external channel coil, evacuated jacket, two isothermal mixing baffles, and a mixing apparatus, according to the present invention, with the integral isothermal mixing baffles entering the reactor vessel from the top.
  • FIG. 7B is a partial cross-sectional view of the reaction vessel with affixed channel coil, evacuated jacket, two isothermal mixing baffles, and a mixing apparatus, according to the present invention, with the integral isothermal mixing baffles entering the reactor vessel from the bottom.
  • FIG. 8A is a fragmentary cross-sectional view of one embodiment of the channel coil according to the present invention.
  • FIG. 8B is a fragmentary cross-sectional view of an alternate embodiment of a channel coil according to the present invention.
  • FIG. 8C shows a comparison of a conventional half-pipe jacket cross-section to that of the present invention.
  • FIG. 8D is a fragmentary cross-sectional view of another alternate embodiment of the channel coil wherein the full reaction vessel wall can be exposed to the fluid in the channel coil.
  • FIG. 9A is a partial cross-sectional view of an alternate embodiment of the isothermal mixing baffle of the present invention.
  • FIG. 9B is a partial cross-sectional view of another embodiment of the isothermal mixing baffle of the present invention.
  • FIG. 10 is a cross-sectional view of a preferred embodiment of the phase separator of the present invention for use in cooling or heating according to the present invention.
  • FIG. 11 is a partial cross-sectional view of an alternative embodiment of the phase separator of the present invention for use in cooling or heating according to the present invention.
  • Foaming occurs because the evolved gas flux across the content/head space interface increases above a critical point.
  • the gas flux in question is defined as velocity /cross-sectional area. Once foaming occurs, some of the contents are out of solution and remain un-reacted, thus affecting the uniformity and extent of the desired reactions.
  • FIG 1A is a flow diagram that depicts the flow scheme of the present invention in a cooling mode for the phase separator 50 and the reaction vessel 110, which contains isothermal mixing baffles 400 and the helical channel coil 100 fixed to the outer surface of reaction vessel 110. For the purposes of illustration only one baffle is shown.
  • the helical channel coil 100 may also extend to cover the upper head 112 and lower head 113 of reaction vessel 110.
  • Low "quality" (low vapor content) working fluid shown by arrow 10 enters the phase separator 50 and is split into a vapor phase shown by line 13 and a liquid phase shown by line 11, the separation effected by gravitational means.
  • the liquid phase 11 from the phase separator is piped to the isothermal mixing baffle(s) 400, wherein it changes into a vapor shown by line 12 by boiling and absorbing thermal energy from the contents inside the reaction vessel 110.
  • the vapor 13 emanating from the phase separator 50 is commingled with the vapor 12 generated in the isothermal mixing baffles 400 in a mixing chamber 60.
  • the now combined vapor streams shown by line 14 are fed into the helical channel coil 100, wherein the vapor absorbs sensible thermal energy from the content inside the reaction vessel 100 until it exits the channel coil via line 15 at a temperature very close to that of the average temperature of the reactor content.
  • FIG IB is a flow diagram that depicts the flow scheme of the present invention in a heating mode for the phase separator 50 and the reaction vessel 110, which contains the isothermal mixing baffle(s) 400 and the helical channel coil 100 fixed to the outer surface of reaction vessel 110.
  • the helical channel coil 100 may also extend to cover the upper head 112 and lower head 113 of reaction vessel 110.
  • High "quality" (mostly vapor content) working fluid shown in line 10 enters the phase separator 50 and is split into a vapor phase shown by line 13 and a liquid phase shown by line 11, the separation effected by gravitational means.
  • the vapor phase 13 from the phase separator 50 is piped to the isothermal mixing baffle(s) 400, wherein it changes into a liquid shown as line 12 by condensing and delivering thermal energy to the content inside the reaction vessel 110.
  • the liquid 11 emanating from the phase separator is commingled with the condensate in line 12 generated in the isothermal mixing baffle(s) 400 in a separate mixing chamber 60.
  • the now combined liquid streams in line 14 are fed into the channel coil 100, wherein the liquid delivers sensible thermal energy to the content inside the reaction vessel 110 until it exits the channel coil in line 15 at a temperature very close to that of the average temperature of the reactor content.
  • FIG. 2A is a view of a reaction vessel 110 with a channel coil 100 fixed to the outer surface in a helical wound arrangement.
  • the reaction vessel 110 consists of a cylindrical section 111 and two "dished" heads, an upper head 112 and a lower head 113.
  • the inside wall of channel coil 100 is the outside surface of wall 120 of reaction vessel 110 and will be disposed along the axial length of the cylindrical section 111 of reaction vessel 110.
  • the channel coil 100 may also cover part of the upper head 112 and/or the lower head 113.
  • the channel coil 100, before it is fixed to the reaction vessel 110, has only three outer sides, 121, 122, and 123.
  • a fourth side of the channel coil 100 is formed by the outer surface of wall 120 of the reaction vessel 110.
  • a closed channel is only achieved when the channel coil 100 is fixed to the outer surface of reaction vessel 110.
  • the channel coil 100 surrounds the reaction vessel 110 in a helical configuration. The configuration allows for helical and corresponding downward or upward flow, with respect to the central vertical axis of the reaction vessel 110.
  • the channel coil 100 may be constructed from any suitable material, the most likely for industrial use being carbon steel, stainless steel, Inconel (trademark for an alloy of nickel and chromium available from the Huntington Alloy Products Division of International Nickel Co. Inc. of Huntington, West Virginia), and any number of Hastelloy alloys, including Hastelloy C-276 and Hastelloy B-2. Hastelloy is a trademark for nickel-based corrosion-resistant alloys obtained from Union Carbide Corp.
  • Hastelloy C-276 is a nickel-based alloy containing nickel, chromium, molybdenum, tungsten, iron, carbon and silicon.
  • Hastelloy B-2 differs from Hastelloy C-276 in that it does not contain tungsten and the other components appear in different concentrations.
  • FIG. 3 A is a sectional view of the cylindrical reaction vessel 110 of with integral channel coil 100 and integral isothermal mixing baffle 400 (one only shown for simplicity).
  • FIG. 3B is a sectional view of an alternate embodiment of reaction vessel 110 with truncated cone portion replacing the cylindrical portion with integral channel coil 100 and integral isothermal mixing baffle 400 (one only shown for simplicity).
  • FIG. 3 A is a sectional view of the cylindrical reaction vessel 110 of with integral channel coil 100 and integral isothermal mixing baffle 400 (one only shown for simplicity).
  • FIG. 3B is a sectional view of an alternate embodiment of reaction vessel 110 with truncated cone portion replacing the cylindrical portion with integral channel coil 100 and integral isothermal mixing baffle 400 (one only shown for simplicity).
  • FIG. 2A, FIG 2B, FIG. 3A and FIG. 3B show two characteristics of channel coil 100, which combine to add mechanical strength to reaction vessel 110.
  • the first is that the point of contact 130 is a right angle to the reaction vessel wall 120, 125 in the vertical section of the reaction vessel 111, as well in the upper head 112, 115 and lower heads 113, 116. That is, walls 121 and 123 form a right angle with wall 120. In the preferred embodiment, walls 121 and 123 must form a right angle with the axis of the cylinder reaction vessel 110 having a vertical cylindrical section where the channel coil is fixed to the wall 120.
  • walls 121 and 123 are perpendicular to the line tangent to the convex (external) surface of the head, 112 or 113, where the tangent point is at the bisector between 121 and 123.
  • the vertical section has cone shape wall 125 by fixing portions 121 and 123 perpendicular to wall 125.
  • the pe ⁇ endicularity of portion 121 and 123 of channel coil 100 to wall 120 or wall 125 of the reaction vessel 110 is required in order to meet the criteria established by section UG-28 of the ASME Boiler And Pressure Vessel Code Section VIII Division 1 so that elements 121, 122 and 123 can be considered as adding strength to the wall 120 under external pressure.
  • the second characteristic adding strength to reaction vessel 110 concerns the pitch at which the helical channel coil 100 is affixed to the reaction vessel wall 120.
  • the pitch is the slope of the coil 100, with respect to a horizontal radial plane which is pe ⁇ endicular to the vertical axis of the reactor. A larger slope is considered a higher pitch.
  • the channel coil 100 is affixed at a pitch less than or equal to a maximum pitch, which is that pitch beyond which the desired improvements in the reaction vessel wall 120 section modulus are no longer achieved, as dictated by the rules of pressure vessel design codes such as ASME Section VIII, Division 1, sections UG-27 and UG-28 thereof.
  • Section UG-27 explains how to calculate "Thickness of Shells Under Internal Pressure”
  • section UG-28 describes how to calculate "Thickness of Shells and Tubes Under External Pressure”. Exactly what this pitch is will depend on many factors including the diameter of reaction vessel 110, the material of construction of the reaction vessel 110 and the operating parameters for which the reactor is designed. As the pitch (or slope) of the coil increases, the distance between successive coils increases.
  • the coil is made of elements 121 and 123 that are pe ⁇ endicular to the vessel wall, 120, 125 which allows for the vessel, under the rules of pressure vessel design codes such as ASME Section VIII, Division 1 to take credit for the reinforcement to reaction vessel wall 120 125.
  • pressure vessel design codes such as ASME Section VIII, Division 1 to take credit for the reinforcement to reaction vessel wall 120 125.
  • the reinforcement required will depend upon the differential pressure between the inside and outside of reaction vessel wall 120. This is a design parameter easily calculated by one skilled in the art.
  • the maximum pitch of channel coil 100 will depend on the designed maximum operating pressure for reaction vessel 110, among other factors.
  • the pitch is the distance of each helical 360o course of the coil 100, with respect to the previous and/or subsequent helical 360o course. A greater separation is considered a higher pitch.
  • the channel coil 100 is fixed at a pitch less than or equal to a maximum pitch, which is that pitch beyond which the desired improvements in the reaction vessel wall 120 section modulus are no longer achieved, as dictated by the rules of pressure vessel design codes such as ASME Section VIII, Division 1, sections UG-27 and UG-28 thereof. Section UG-27 explains how to calculate "Thickness of Shells Under Internal Pressure", and section UG-28 describes how to calculate "Thickness of Shells and Tubes Under External Pressure”.
  • the point of contact 130 between reaction vessel wall 120 and channel coil 110 is a right angle, and the pitch of the channel coil 100 is less than or equal to the maximum pitch.
  • a thinner reaction vessel wall increases the overall heat transfer coefficient across the reaction vessel wall because the thermal resistance resulting from the thermal conductivity of the reaction vessel wall is reduced.
  • pressure vessel design codes such as ASME Section VIII, Division 1
  • ASME Section VIII, Division 1 the greatest advantage of the present invention is realized in larger diameter reaction vessels that operate at relatively low pressures, e.g., up to 10 bar and at full vacuum (FV).
  • FV full vacuum
  • the FV condition inside the reaction vessel dictates the use of thicker wall 120, 125 than otherwise be required to withstand positive internal pressure only.
  • the wall thickness 120, 125 is controlled by positive internal pressure in the reaction vessel and will be thinner.
  • FIG. 8C depicts a comparison of a conventional half-pipe jacket cross-section to that of the present invention with proportional dimensions.
  • the cross-sectional area of a jacket coil 100 in accordance with the present invention, compared to that of a conventional half-pipe jacket coil of proportional dimensions, is 4/ ⁇ or 27% greater. This allows for higher fluid flow for the same unit pressure drop, and thus greater heat transfer.
  • the channel coil 100 may be additionally insulated with insulation 700 attached directly to the three outer sides, 121, 122, and 123, of the coil 100 as shown in Figs. 8A or 8B.
  • insulation 700 may be wrapped around channel coil 100 and reaction vessel 110 as shown in FIG. 3 A and FIG. 3B, before placement in evacuation shell 300.
  • Insulation 700 may be any suitable material which does not out-gas when evacuated and/or heated. Reflective multilayer insulation, made of alternating layers of fiberglass cloth, cured of any residues, which would otherwise out-gas when evacuated and/or heated, and aluminum foil are preferred. These alternate layer method of application may varied, e.g. two layers of cloth and one layer of aluminum foil, etc. The "no out-gassing" requirement is essential for the evacuated multi-layer reflective insulation of the preferred embodiment to be successful.
  • An alternative insulation method for the reaction vessel entails the use of evacuated dry perlite powder in the annular space between the reaction vessel, which comprises the jacket coil 100 and vessel wall 120, and the evacuated shell 300, (FIG. 4).
  • the physical space between the jacket coil 100 and the evacuated shell 300 must be at least six (6) inches, but typically eight (8) to twelve (12) inches in order for evacuated dry perlite powder to serve as a suitable insulation medium.
  • FIG. 4 is a sectional view of reaction vessel 110 with the channel coil 100 fixed to the outer surface of reaction vessel 110, integral isothermal mixing baffle 400 (one only shown for simplicity) and an evacuated shell 300.
  • the evacuated shell 300 completely encloses reaction vessel 110 and channel coil 100, with the exception of related piping and utilities, which penetrate the evacuated shell 300.
  • the placement of the evacuated shell 300 around the apparatus as described above allows for additional insulation of reaction vessel 110 and channel coil 100 from the ambient air. Insulation from the ambient air results in decreased heat transfer through both the reaction vessel wall 120 and the channel coil walls 121, 122, and 123, as some of the energy is parasitically lost outwardly to the environment through the insulation 700.
  • evacuated shell 300 results in greater temperature control of the reaction vessel contents, making the insulation 700 more thermally efficient.
  • the evacuated shell may be constructed from any suitable material, including carbon steel, stainless steel, Inconel, or Hastelloy C. Further, evacuated shell 300 can also include reflective material on the inner or outer surface thereof to reduce radiant heat transfer.
  • FIG. 5 A is a partial cross-sectional view of an isothermal mixing baffle of uniform circular cross-section (a cylinder) in accordance with the present invention.
  • an isothermal mixing baffle 400 is used where there exists a need to cool the reaction vessel contents.
  • such isothermal mixing baffles can also be used where heating of the contents of reaction vessel 110 is needed.
  • the isothermal mixing baffle 400 is inserted into the reaction vessel contents through the top head 112 and evacuated shell 300 as shown in FIG. 6A. For cooling, a saturated or subcooled liquid is introduced into the isothermal mixing baffle 400 through an inlet pipe 410.
  • the liquid is selected primarily because of its boiling point, providing, of course, other factors do not prevent its use, such as availability, cost, reactivity, toxicity, etc.
  • a liquid having a boiling point lower than that of the reaction vessel contents will boil when heat is absorbed from the reaction vessel contents.
  • Fluids which may be used for cooling or heating in the present invention include, but are not limited to nitrogen, brine, steam, chilled water, carbon dioxide, ammonia, CF4, ethane, ethylene and hot water. Other fluids may also be used depending on the particular needs of the reaction for which the reactor is designed.
  • the ideal temperature (or range of temperatures) of the reaction vessel contents can be determined from the chemistry of the reaction. This temperature, along with the physical characteristics of the isothermal mixing baffle (dimensions, material of construction, number of baffles, etc.) and relevant heat transfer equations, are combined to give rise to a required amount of heat transfer which must occur across the wall 449 (FIGS. 5A, 5B, 5C, and 5D) of the isothermal mixing baffle 400 in order to maintain the reactor contents at the desired temperature. From this required value of heat transfer, a fluid is selected such that the latent heat of vaporization plus any sensible heat transfer occurring from any rise in temperature of the fluid to its boiling point, will give the desired total heat transfer.
  • a fluid with precisely the right characteristics does not have to exist for accurate control of the temperature. Controlling the flow rate of the fluid into the isothermal mixing baffle 400 or the liquid level thereof will allow for fine tuning the heat transfer and corresponding temperature of the reactor contents. Further, controlling the pressure of the liquid could help alter its boiling point and fine tune the cooling power and range of the liquid. The selected fluid need only fall within a range of necessary heat transfer requirements.
  • a hot gas such as gaseous ammonia
  • the condensed ammonia in line 12 is then combined with other condensed ammonia in line 11 emanating from the phase separator 50 and introduced via line 14 into the channel coil 100.
  • This hot gas and resultant condensate then heats the contents of reaction vessel 110.
  • fluid flow into the isothermal mixing baffle 400 can be increased. This will raise the level of boiling liquid 450 to a level shown as 448 in FIG. 5 A in the isothermal mixing baffle 400. This in turn will expose a greater surface area of boiling liquid 450 to wall 449 of isothermal mixing baffle 400, thus allowing greater heat transfer from the reaction vessel contents through wall 449 of baffle 400 into boiling liquid 450.
  • the isothermal mixing baffles 400 can be used in one of several different heating and cooling schemes.
  • the isothermal mixing baffles 400 may be used to gain only sensible heat, in which case they will serve as sensible energy mixing baffles.
  • the isothermal mixing baffles 400 can also be utilized with a liquid having a boiling point higher than the desired temperature of the reactor contents. Cooling or warming liquid could be passed through the isothermal (or sensible energy) mixing baffles.
  • a gas may be passed through the isothermal (or sensible energy) mixing baffles 400. Any fluid that provides the necessary heat transfer properties can be used in the isothermal (or sensible energy) mixing baffles for effective ,., temperature control of the reaction vessel contents. In these cases, the isothermal (or sensible energy) mixing baffles 400 act as simple heat exchangers.
  • Isothermal mixing baffles 400 can be inserted from the top of the reactor, as shown in FIG. 5 A and FIG. 6 A or from the bottom of the reactor, as shown in FIG. 5B and FIG. 6B.
  • isothermal mixing baffles 400 have been inserted from the top of the reactor as a matter of convenience and tradition.
  • the isothermal mixing baffles 400 are designed and arranged in so that their combined cross-sectional area will be such that the velocity of the vapor evolved from the liquid phase boiling therein will be below a critical value, Uc, above which droplets or slugs of the liquid phase will be entrained in the evolved gas and expelled from the isothermal mixing baffles. As shown in FIGs.
  • FIG. 5A and FIG 5B also show a sintered, porous metal phase separator or "snubber"
  • FIG. 5 A and FIG. 5B also show a means for the gas formed from the boiling liquid inside the inside the isothermal mixing baffle 400 to escape.
  • An annular space 420 surrounds the inlet pipe 410. Annular space 420 comprises the same atmosphere as that above the liquid level in the isothermal mixing baffle 400.
  • exiting gas may then be utilized in various ways. If environmentally safe gas is used, it may be exhausted to the atmosphere by venting it, although this is likely not cost effective. The gas may be recovered by piping it to a condenser, or used at another site where the particular vapor or gas is needed. Finally, the exiting gas may be transported, through vacuum jacketed or otherwise insulated pipe, to the channel coil 100 for further cooling of the reactor contents, as dictated by the preferred embodiment of this invention and depicted in FIG. 1A.
  • FIG. 5 A and FIG. 5B also show means for detecting the level of liquid in the isothermal mixing baffle 400.
  • a dual leg dip tube 440 is inserted into the isothermal mixing baffle 400.
  • the top opening 445 of the dip tube 440 is near the top of the isothermal mixing baffle 400, and the bottom opening 447 of the dip tube 440 is near the bottom of the isothermal mixing baffle 400.
  • the level of liquid 450 in the isothermal mixing baffle 400 is maintained below the top opening 445 and above the bottom opening 447 of the dip tube.
  • the pressure differential is detected as the pressure of the head of liquid in the dip tube.
  • the pressure at the top opening 445 is the pressure of the gas above the liquid 450.
  • the pressure at the bottom opening 447 is the pressure of the gas above the liquid 450 plus the pressure caused by the weight of the liquid 450 which is above the bottom opening 447.
  • the pressure created by the weight of liquid 450 above the bottom opening 447 can be found by subtracting the value of the pressure at the top opening 445 from the value of the pressure at the bottom opening 447. This pressure can be used (in conjunction with the density of the liquid) to calculate the height of liquid above the bottom opening 447.
  • FIG. 5C and 5D are alternative embodiments of FIG. 5A and 5B, respectively, wherein the internal sintered, porous metal phase separator or "snubber" 411 is made to be removable from outside the reactor vessel, without disturbing the reactor vessel contents or evacuated shell 300.
  • FIG. 5E and 5F are alternative embodiments of the isothermal mixing baffles 400 which employ non-circular cross-sectional geometries, such as ellipsoids and airfoils. These alternative embodiments may be prescribed to augment surface area and/or direct the flow of reactor contents to enhance mixing.
  • FIG. 6A shows the present invention including reaction vessel 110, channel coil 100, and one isothermal mixing baffle 400 inserted from the top of the reactor, which penetrates the upper head 112 and evacuated shell 300. It would be apparent to one of ordinary skill in the art that multiple isothermal mixing baffles 400 could be used to increase the overall rate of heat transfer between the reactor contents and isothermal mixing baffle contents. An additional advantage to utilizing multiple isothermal mixing baffles 400 is seen where the reactor contents are agitated with a mixing blade apparatus.
  • FIG. 7 A shows an embodiment where multiple isothermal mixing baffles 400 are used in conjunction with an agitator 460.
  • the isothermal mixing baffles 400 must be arranged outside the radius of mixing blades 490 of agitator 460.
  • the isothermal mixing baffles 400 also act as mixing baffles, thus our use of the term isothermal mixing baffles.
  • FIG. 6B shows an alternative embodiment of the present invention including reaction vessel 110, channel coil 100, and one isothermal mixing baffle 400 inserted from the bottom of the reactor, which penetrates the lower head 113 and evacuated shell 300.
  • Formation of ice on the surface of the isothermal mixing baffles 400 is detrimental as the temperature of the ice will be at the freezing point of the reactor content fluids, not the much lower boiling liquid 450 inside the isothermal mixing baffles 400.
  • the correlation between high turbulence and avoidance of ice (or solid) formation is due to the fact that heat transfer through a laminar layer is largely conduction controlled, but heat transfer through a turbulent fluid is largely convection controlled. Convective heat transfer takes place because a fluid is in motion and eddies within the fluid effectively carry heat throughout the fluid. This is very efficient heat transfer.
  • Conductive heat transfer is due to interaction (molecular) between the molecules comprising the medium through which the heat passes.
  • a further requirement to prevent the formation of ice on the external surface of the isothermal mixing baffles 400 is that the convective film heat transfer coefficient, on the outside of the isothermal mixing baffles 400 (in contact with the reactor contents), be greater than the convective film heat transfer coefficient on the inside of the isothermal mixing baffles 400 (in contact with the boiling liquid 450). This outcome can be achieved through a programmable control device available through Arencibia Associates Inc., Center Valley, PA.
  • FIG. 7A and 7B show alternative embodiments of the isothermal mixing baffles 400, wherein the cross-sectional area of the isothermal mixing baffles is increased at axial locations where there will not be interference with reaction blades 490 of agitator 460. This alternative embodiment results in increased heat transfer area.
  • FIG. 8 A and 8B show additional embodiments of the shape of channel coil 100.
  • the outside wall 122 of the channel coil 100 may be of nearly any shape. It is critical, however, that the walls 121 and 122 are both normal to the outside reaction vessel wall 120. In this configuration, channel coil 100 supports and strengthens reaction vessel wall 120, allowing use of a thinner wall and greater heat transfer.
  • FIG. 8D shows a particular embodiment wherein the cross-sectional area of channel coil 100 available for flow of heat transfer working fluid can be increased by joining adjacent coils with wall 124, which may be flat, as shown, or nearly any shape. If flat, like wall 122, wall 124 will also ad strength to the reaction vessel and further allow for the reduction of the thickness of the reaction vessel wall 120, if external pressure is controlling.
  • the channel defined by wall 124 and adjacent walls of the helical channel coil can be used to introduce additional fluid to contact wall 120 to thus further improve the heat transfer.
  • the fluid in this channel can be different than the fluid in the helical channel coil.
  • FIG. 9A and 9B are alternative embodiments of FIG. 5A and 5B, respectively, wherein the wall 449 comprises cylindrical sections of different diameters so that the smaller diameter accommodates the trajectory of agitator blades and the larger diameter allows for greater heat transfer area.
  • FIG. 10 is a cross-sectional view of a preferred embodiment of phase separator 50 having an internal vessel 59 and an evacuated shell 57 of the present invention for use in a cooling or heating mode application.
  • the evacuated shell 57 completely encloses internal vessel 59, with the exception of related piping and utilities, which penetrate the evacuated shell 57.
  • the placement of the evacuated shell 57 around the apparatus as described above allows for additional insulation of internal vessel from the ambient air. Insulation from the ambient air results in decreased heat transfer through the internal vessel 59, as some of the energy is parasitically lost outwardly to the environment through the insulation 58.
  • the utilization of evacuated shell 57 results in greater temperature control of the reaction vessel contents, making the insulation 58 more thermally efficient.
  • the evacuated shell 57 may be constructed from any suitable material, including carbon steel, stainless steel, Inconel, or Hastelloy C. Further, evacuated shell 57 can also include reflective material on the inner or outer surface thereof to reduce radiant heat transfer.
  • Working heat transfer fluid which may be sub-cooled, saturated or contain both phases enters the phase separator at the inlet nozzle 10 and is ducted vertically through an internal coaxial pipe 51 to a porous membrane diffuser 52 through which it enters the internal phase separator vessel 59.
  • the cross-sectional area of the internal vessel 59 of phase separator 50 will be such that the velocity of the vapor separated from the liquid phase entrained therein will be below a critical value, Uc, above which droplets or slugs of the liquid phase will be entrained in the evolved gas and expelled from the phase separator.
  • the liquid phase of the working heat transfer fluid enters the annulus between the external coaxial pipe 55 and the internal coaxial pipe 51 through apertures 56 on the external coaxial pipe 55 located at the lower end of the internal vessel 59.
  • the liquid phase of the working heat transfer fluid then exits the phase separator at the outlet liquid nozzle 11.
  • the vapor phase of the working heat transfer fluid then exits the phase separator at the outlet vapor nozzle 13.
  • FIG. 11 is a cross-sectional view of alternate embodiment of the phase separator of the present invention for use in a cooling or heating mode application.
  • the working heat transfer fluid inlet nozzle is located on top along with the outlet vapor nozzle 13.
  • the outlet liquid nozzle 11 is located in the bottom.
  • FIG. 11 detect liquid inventory of working heat transfer fluid in the phase separator 50, by the same mechanism described for determining liquid level in the isothermal mixing baffles 400, in connection with FIG. 5A.
  • Upper sensing line 53 in FIG. 10 and FIG. 11 is analogous to 447 in Figure 5A.
  • Lower sensing line 54 in FIG. 10 and FIG. 11 is analogous to 445 in Figure 5A.

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  • Chemical Kinetics & Catalysis (AREA)
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Abstract

L'invention concerne une cuve de réaction contenant des déflecteurs de brassage de régulation de température placés à l'intérieur de la cuve servant à l'ébullition d'un liquide. Cette cuve consiste en un puits thermique isotherme. L'énergie de la vaporisation est fournie par le contenu de la cuve de réaction. La vapeur produite par l'ébullition peut être acheminée vers des serpentins de canalisation entourant l'extérieur de la paroi de ladite cuve. Les serpentins de canalisation entrent en contact, de manière perpendiculaire, avec la paroi extérieure de la cuve. Le support mécanique procuré par les serpentins de canalisation permet, d'une part, de réduire l'épaisseur de la paroi de la cuve de réaction et, d'autre part, d'obtenir un rendement de transfert thermique amélioré entre le contenu des serpentins de canalisation et le contenu de la cuve de réaction. L'ensemble du dispositif décrit dans cette invention est confiné dans une coque sous vide, afin d'obtenir une isolation supplémentaire. Le dispositif comprend un appareil actionné de manière gravitationnelle garantissant l'entrée d'un liquide saturé ou sous-refroidis dans les déflecteurs de brassage isothermes. Ceci permet de garantir le déclenchement du changement de phase isotherme.
PCT/US2001/011971 2000-04-13 2001-04-12 Cuve de reaction a temperature regulee WO2001078890A2 (fr)

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US09/548,511 US6955793B1 (en) 1997-06-18 2000-04-13 Temperature controlled reaction vessel
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Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007029218A1 (fr) * 2005-09-09 2007-03-15 Pfizer Science And Technology Ireland Limited Appareil pour processus de reaction a basse temperature
WO2009101007A1 (fr) * 2008-02-12 2009-08-20 Ineos Manufacturing Belgium Nv Réacteur de polymérisation
WO2014089000A3 (fr) * 2012-12-03 2014-09-18 Ge Healthcare Bio-Sciences Corp. Surfaces de régulation de température et structures de support
CN105349334A (zh) * 2015-12-15 2016-02-24 乌毡帽酒业有限公司 一种米饭发酵池
US9340763B2 (en) 2008-03-25 2016-05-17 Ge Healthcare Bio-Sciences Corp. Temperature controlling surfaces and support structures
US9534196B2 (en) 2009-03-25 2017-01-03 Ge Healthcare Bio-Sciences Corp. Temperature controlled support surfaces for single use flexible wall systems
CN107552321A (zh) * 2017-10-10 2018-01-09 黄河科技学院 标线涂料导热油循环加热式料罐
WO2019239131A1 (fr) * 2018-06-13 2019-12-19 Process Technology Strategic Consultancy Limited Appareil de traitement discontinu
US10767154B2 (en) 2008-03-25 2020-09-08 Global Life Sciences Solutions Usa Llc Temperature controlling surfaces and support structures
CN112295432A (zh) * 2020-11-23 2021-02-02 李楠 一种沥青生产的搅拌设备
CN115193325A (zh) * 2022-09-16 2022-10-18 广东美赛尔细胞生物科技有限公司 一种用于药理学的药物加热搅拌反应器
CN115286992A (zh) * 2022-08-23 2022-11-04 黄山联固新材料科技有限公司 一种高固含低温抗开裂单组分水性聚氨酯防水涂料及制备方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3297412A (en) * 1963-12-11 1967-01-10 Exxon Research Engineering Co Apparatus for conducting exothermic reactions
US3732266A (en) * 1970-04-08 1973-05-08 Chemetron Corp Hydrogenation of oils
WO1998057741A2 (fr) * 1997-06-18 1998-12-23 Arencibia Associates, Inc. Cuve a reaction a regulation de temperature

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3297412A (en) * 1963-12-11 1967-01-10 Exxon Research Engineering Co Apparatus for conducting exothermic reactions
US3732266A (en) * 1970-04-08 1973-05-08 Chemetron Corp Hydrogenation of oils
WO1998057741A2 (fr) * 1997-06-18 1998-12-23 Arencibia Associates, Inc. Cuve a reaction a regulation de temperature

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007029218A1 (fr) * 2005-09-09 2007-03-15 Pfizer Science And Technology Ireland Limited Appareil pour processus de reaction a basse temperature
WO2009101007A1 (fr) * 2008-02-12 2009-08-20 Ineos Manufacturing Belgium Nv Réacteur de polymérisation
RU2495713C2 (ru) * 2008-02-12 2013-10-20 Инеос Мэньюфекчуринг Белджиум Нв Реактор-полимеризатор
US9174193B2 (en) 2008-02-12 2015-11-03 Ineos Manufacturing Belgium Polymerisation reactor
US9340763B2 (en) 2008-03-25 2016-05-17 Ge Healthcare Bio-Sciences Corp. Temperature controlling surfaces and support structures
US10774299B2 (en) 2008-03-25 2020-09-15 Global Life Sciences Solutions Usa Llc Temperature controlled support surfaces for single use flexible wall systems
US10767154B2 (en) 2008-03-25 2020-09-08 Global Life Sciences Solutions Usa Llc Temperature controlling surfaces and support structures
US9534196B2 (en) 2009-03-25 2017-01-03 Ge Healthcare Bio-Sciences Corp. Temperature controlled support surfaces for single use flexible wall systems
WO2014089000A3 (fr) * 2012-12-03 2014-09-18 Ge Healthcare Bio-Sciences Corp. Surfaces de régulation de température et structures de support
JP2016500433A (ja) * 2012-12-03 2016-01-12 ジーイー・ヘルスケア・バイオサイエンス・コーポレイション 温度制御面及び支持構造
CN104903674A (zh) * 2012-12-03 2015-09-09 通用电气医疗集团生物科学公司 温度控制表面和支承结构
CN105349334A (zh) * 2015-12-15 2016-02-24 乌毡帽酒业有限公司 一种米饭发酵池
CN105349334B (zh) * 2015-12-15 2018-01-05 乌毡帽酒业有限公司 一种米饭发酵池
CN107552321A (zh) * 2017-10-10 2018-01-09 黄河科技学院 标线涂料导热油循环加热式料罐
CN107552321B (zh) * 2017-10-10 2022-09-16 黄河科技学院 标线涂料导热油循环加热式料罐
WO2019239131A1 (fr) * 2018-06-13 2019-12-19 Process Technology Strategic Consultancy Limited Appareil de traitement discontinu
JP2021527567A (ja) * 2018-06-13 2021-10-14 プロセス テクノロジー ストラテジック コンサルタンシー リミテッドＰｒｏｃｅｓｓ Ｔｅｃｈｎｏｌｏｇｙ Ｓｔｒａｔｅｇｉｃ Ｃｏｎｓｕｌｔａｎｃｙ Ｌｉｍｉｔｅｄ バッチ処理装置
CN112261994A (zh) * 2018-06-13 2021-01-22 工艺技术战略咨询有限公司 批处理设备
US11446629B2 (en) 2018-06-13 2022-09-20 Process Technology Strategic Consultancy Limited Batch processing apparatus
JP7516360B2 (ja) 2018-06-13 2024-07-16 プロセス テクノロジー ストラテジック コンサルタンシー リミテッド バッチ処理装置
CN112295432A (zh) * 2020-11-23 2021-02-02 李楠 一种沥青生产的搅拌设备
CN112295432B (zh) * 2020-11-23 2022-04-12 临沂市玉泉沥青有限公司 一种沥青生产的搅拌设备
CN115286992A (zh) * 2022-08-23 2022-11-04 黄山联固新材料科技有限公司 一种高固含低温抗开裂单组分水性聚氨酯防水涂料及制备方法
CN115193325A (zh) * 2022-09-16 2022-10-18 广东美赛尔细胞生物科技有限公司 一种用于药理学的药物加热搅拌反应器
CN115193325B (zh) * 2022-09-16 2022-11-29 佛山市妇幼保健院 一种用于药理学的药物加热搅拌反应器

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