US20110087056A1 - Adiabatic plug flow reactors and processes incorporating the same - Google Patents
Adiabatic plug flow reactors and processes incorporating the same Download PDFInfo
- Publication number
- US20110087056A1 US20110087056A1 US12/901,383 US90138310A US2011087056A1 US 20110087056 A1 US20110087056 A1 US 20110087056A1 US 90138310 A US90138310 A US 90138310A US 2011087056 A1 US2011087056 A1 US 2011087056A1
- Authority
- US
- United States
- Prior art keywords
- reactor
- design
- temperature
- chlorinated
- fluorinated
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 238000000034 method Methods 0.000 title claims description 54
- 230000008569 process Effects 0.000 title claims description 42
- 238000006243 chemical reaction Methods 0.000 claims abstract description 124
- 238000013461 design Methods 0.000 claims abstract description 66
- 238000004519 manufacturing process Methods 0.000 claims abstract description 46
- 239000006227 byproduct Substances 0.000 claims abstract description 45
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical class CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 26
- 150000001336 alkenes Chemical class 0.000 claims abstract description 19
- 150000001335 aliphatic alkanes Chemical class 0.000 claims abstract 3
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical class ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 claims description 57
- 230000015572 biosynthetic process Effects 0.000 claims description 22
- 239000000047 product Substances 0.000 claims description 22
- UMGQVBVEWTXECF-UHFFFAOYSA-N 1,1,2,3-tetrachloroprop-1-ene Chemical compound ClCC(Cl)=C(Cl)Cl UMGQVBVEWTXECF-UHFFFAOYSA-N 0.000 claims description 20
- 239000000376 reactant Substances 0.000 claims description 20
- 238000012546 transfer Methods 0.000 claims description 17
- FXRLMCRCYDHQFW-UHFFFAOYSA-N 2,3,3,3-tetrafluoropropene Chemical compound FC(=C)C(F)(F)F FXRLMCRCYDHQFW-UHFFFAOYSA-N 0.000 claims description 13
- 238000009413 insulation Methods 0.000 claims description 13
- 239000012035 limiting reagent Substances 0.000 claims description 13
- 239000003999 initiator Substances 0.000 claims description 11
- CDOOAUSHHFGWSA-OWOJBTEDSA-N (e)-1,3,3,3-tetrafluoroprop-1-ene Chemical compound F\C=C\C(F)(F)F CDOOAUSHHFGWSA-OWOJBTEDSA-N 0.000 claims description 10
- 238000010791 quenching Methods 0.000 claims description 10
- 239000011541 reaction mixture Substances 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 8
- 230000009467 reduction Effects 0.000 claims description 7
- 239000003085 diluting agent Substances 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- NBVXSUQYWXRMNV-UHFFFAOYSA-N fluoromethane Chemical class FC NBVXSUQYWXRMNV-UHFFFAOYSA-N 0.000 claims description 4
- ZYVSNYBYAYMMQV-UHFFFAOYSA-N 2-chloro-3-fluoroprop-1-ene Chemical compound FCC(Cl)=C ZYVSNYBYAYMMQV-UHFFFAOYSA-N 0.000 claims description 2
- XWCDCDSDNJVCLO-UHFFFAOYSA-N Chlorofluoromethane Chemical class FCCl XWCDCDSDNJVCLO-UHFFFAOYSA-N 0.000 claims description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical class C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 2
- 239000000460 chlorine Substances 0.000 description 56
- CYTYCFOTNPOANT-UHFFFAOYSA-N Perchloroethylene Chemical group ClC(Cl)=C(Cl)Cl CYTYCFOTNPOANT-UHFFFAOYSA-N 0.000 description 35
- 229940050176 methyl chloride Drugs 0.000 description 27
- 238000002156 mixing Methods 0.000 description 14
- VZGDMQKNWNREIO-UHFFFAOYSA-N tetrachloromethane Chemical compound ClC(Cl)(Cl)Cl VZGDMQKNWNREIO-UHFFFAOYSA-N 0.000 description 14
- 239000012071 phase Substances 0.000 description 10
- 150000003254 radicals Chemical class 0.000 description 10
- 239000012530 fluid Substances 0.000 description 8
- 210000002268 wool Anatomy 0.000 description 8
- 230000008901 benefit Effects 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- FPBWSPZHCJXUBL-UHFFFAOYSA-N 1-chloro-1-fluoroethene Chemical class FC(Cl)=C FPBWSPZHCJXUBL-UHFFFAOYSA-N 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 239000000919 ceramic Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 229910000831 Steel Inorganic materials 0.000 description 4
- 229910052801 chlorine Inorganic materials 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 4
- 238000010574 gas phase reaction Methods 0.000 description 4
- 239000011521 glass Substances 0.000 description 4
- 238000005658 halogenation reaction Methods 0.000 description 4
- 239000010959 steel Substances 0.000 description 4
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000003889 chemical engineering Methods 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 238000011143 downstream manufacturing Methods 0.000 description 3
- 230000026030 halogenation Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000000171 quenching effect Effects 0.000 description 3
- 238000007348 radical reaction Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- ZRNSSRODJSSVEJ-UHFFFAOYSA-N 2-methylpentacosane Chemical compound CCCCCCCCCCCCCCCCCCCCCCCC(C)C ZRNSSRODJSSVEJ-UHFFFAOYSA-N 0.000 description 2
- UXKIPTJTWDKGSX-UHFFFAOYSA-N CCl.[C] Chemical compound CCl.[C] UXKIPTJTWDKGSX-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 239000011449 brick Substances 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- -1 corkboard Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000003682 fluorination reaction Methods 0.000 description 2
- 239000010439 graphite Substances 0.000 description 2
- 229910002804 graphite Inorganic materials 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- ZDCWZRQSHBQRGN-UHFFFAOYSA-N 1,1,1,2,3-pentafluoropropane Chemical compound FCC(F)C(F)(F)F ZDCWZRQSHBQRGN-UHFFFAOYSA-N 0.000 description 1
- FBSPLEKACMFIFU-UHFFFAOYSA-N 1,1,2,3-tetrachlorobut-1-ene Chemical class CC(Cl)C(Cl)=C(Cl)Cl FBSPLEKACMFIFU-UHFFFAOYSA-N 0.000 description 1
- PGJHURKAWUJHLJ-UHFFFAOYSA-N 1,1,2,3-tetrafluoroprop-1-ene Chemical compound FCC(F)=C(F)F PGJHURKAWUJHLJ-UHFFFAOYSA-N 0.000 description 1
- SMCNZLDHTZESTK-UHFFFAOYSA-N 2-chloro-1,1,1,2-tetrafluoropropane Chemical compound CC(F)(Cl)C(F)(F)F SMCNZLDHTZESTK-UHFFFAOYSA-N 0.000 description 1
- OQISUJXQFPPARX-UHFFFAOYSA-N 2-chloro-3,3,3-trifluoroprop-1-ene Chemical compound FC(F)(F)C(Cl)=C OQISUJXQFPPARX-UHFFFAOYSA-N 0.000 description 1
- 235000007173 Abies balsamea Nutrition 0.000 description 1
- 239000004857 Balsam Substances 0.000 description 1
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 244000146553 Ceiba pentandra Species 0.000 description 1
- 235000003301 Ceiba pentandra Nutrition 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 244000018716 Impatiens biflora Species 0.000 description 1
- 239000005909 Kieselgur Substances 0.000 description 1
- 240000007182 Ochroma pyramidale Species 0.000 description 1
- 101100409194 Rattus norvegicus Ppargc1b gene Proteins 0.000 description 1
- 239000004965 Silica aerogel Substances 0.000 description 1
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical class ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 229910052794 bromium Inorganic materials 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- GSOLWAFGMNOBSY-UHFFFAOYSA-N cobalt Chemical compound [Co][Co][Co][Co][Co][Co][Co][Co] GSOLWAFGMNOBSY-UHFFFAOYSA-N 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000011152 fibreglass Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011491 glass wool Substances 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 229910000856 hastalloy Inorganic materials 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910001026 inconel Inorganic materials 0.000 description 1
- 229910001055 inconels 600 Inorganic materials 0.000 description 1
- 239000011810 insulating material Substances 0.000 description 1
- 229910052740 iodine Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000011490 mineral wool Substances 0.000 description 1
- 239000003607 modifier Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000011505 plaster Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000008542 thermal sensitivity Effects 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
- C07C17/20—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms
- C07C17/202—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms two or more compounds being involved in the reaction
- C07C17/206—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms two or more compounds being involved in the reaction the other compound being HX
-
- 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
- B01J19/0006—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
- B01J19/0006—Controlling or regulating processes
- B01J19/002—Avoiding undesirable reactions or side-effects, e.g. avoiding explosions, or improving the yield by suppressing side-reactions
- B01J19/0026—Avoiding carbon deposits
-
- 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
- B01J19/006—Baffles
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2405—Stationary reactors without moving elements inside provoking a turbulent flow of the reactants, such as in cyclones, or having a high Reynolds-number
-
- 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
- B01J19/2415—Tubular reactors
-
- 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
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/26—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton
- C07C17/263—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton by condensation reactions
- C07C17/269—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton by condensation reactions of only halogenated hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C21/00—Acyclic unsaturated compounds containing halogen atoms
- C07C21/02—Acyclic unsaturated compounds containing halogen atoms containing carbon-to-carbon double bonds
- C07C21/04—Chloro-alkenes
-
- 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
- B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
- B01J2204/002—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the feeding side being of particular interest
-
- 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
- B01J2219/00054—Controlling or regulating the heat exchange system
-
- 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
- B01J2219/00054—Controlling or regulating the heat exchange system
- B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
- B01J2219/00058—Temperature measurement
- B01J2219/00063—Temperature measurement of the reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00162—Controlling or regulating processes controlling the pressure
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00164—Controlling or regulating processes controlling the flow
- B01J2219/00166—Controlling or regulating processes controlling the flow controlling the residence time inside the reactor vessel
-
- 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
- B01J2219/00245—Avoiding undesirable reactions or side-effects
- B01J2219/00247—Fouling of the reactor or the process equipment
Definitions
- the present invention relates to plug flow reactors capable of adiabatic operation and suitable for conducting continuous, gas phase, free radical reactions to produce chlorinated and/or fluorinated propene and higher alkenes. Processes incorporating the same are also provided.
- Tubular reactors are ubiquitous in the manufacture of commodity chemicals, in particular in processes wherein continuous operation is desired or required.
- the ideal flow condition in a tubular reactor is ‘plug flow’, and under such ideal conditions, the residence time in the reactor is the same for all elements of fluid and there is typically a uniform velocity profile across the radius of the reactor.
- Product mixing is also ideally limited to material the same age, i.e. mixing occurs in the radial direction only. That is, as the plug flows through the reactor, the plug components are perfectly mixed in the radial direction, with mixing in the axial direction being nonexistent.
- plug flow provides greater separation between reacted and unreacted material than non plug flow. This is desirable for processes where reaction rate is affected by reactant concentration. And, good plug flow permits precise control of residence time, which can be critical in processes where conversion and/or selectivity are sensitive to the same.
- tubular reactor capable of approximating plug flow, while yet also providing optimal, e.g., residence time, heat transfer characteristics, temperature control and mixing.
- Such a reactor is provided herein. More specifically, the reactor described herein can provide one or more of more accurate temperature control, minimization of heat transfer into and/or out of the reactor, appropriate residence times of reaction components and or optimized mixing. As a result, desired conversions and/or selectivities can be seen.
- the reactor is thus particularly well suited for reactions comprising thermally sensitive components such as catalysts that may otherwise exhibit reduced lifetimes, or reaction components that undesirably react or decompose at temperatures within the processing specifications of the process desirably carried out within the reactor.
- an adiabatic plug flow reactor suitable for use in a continuous, gas phase, free radical process for the production of chlorinated and/or fluorinated propene and higher alkenes
- the reactor comprises a design that facilitates reduced backmixing and/or recirculation prior to entry into, or upon exit from, the reactor, or reduced formation of by-products during any backmixing that may occur.
- the reactor may further comprise a design that minimizes the production of by-products at a desired conversion.
- a design that minimizes heat transfer to and/or from the reactor including i) a design that minimizes heat transfer to and/or from the reactor; ii) a design that optimizes the flow of the reaction components at the boundary between the reaction components and at least a portion of at least one reactor tube wall; iii) a design that facilitates a reduction of the temperature of a reactor effluent to a temperature below which substantial formation of by-products does not occur, and/or iv) a design that allows the production rate of a process conducted in the reactor to be adjusted by controlling the temperature of the reactor effluent. Combinations of one or more of these may be utilized, in which case the benefits provided by one may be further leveraged, perhaps even synergistically, by addition of the other(s).
- the present reactors are expected to provide time and cost savings to the continuous processes in which they are utilized, not only are processes utilizing the reactor provided, but the products produced thereby may be used to carry these advantages forward, i.e., to downstream processes, or to end-uses.
- processes for the use of a chlorinated and/or fluorinated propene or higher alkene which in some embodiments may be a chlorinated propene, produced in the present reactors to prepare a downstream product, which in some embodiments, may be 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze).
- FIG. 1 is a schematic representation in cross-section of a conventional mixer
- FIG. 2 is a schematic representation in cross-section of a mixer according to one embodiment of the invention.
- FIG. 3 is a graphical depiction of the temperature vs. reactor length in feet of an adiabatic plug flow reactor according to one embodiment of the invention.
- FIG. 4 is a graphical depiction of the production rate and selectivity, versus the exit reactor temperature.
- first”, “second”, and the like, as used herein do not denote any order, quantity, or importance, but rather are used to distinguish one element from another.
- the terms “a” and “an” do not denote a limitation of quantity, but rather denote the presence of at least one of the referenced item, and the terms “front”, “back”, “bottom”, and/or “top”, unless otherwise noted, are merely used for convenience of description, and are not intended to limit the part being described limited to any one position or spatial orientation.
- ranges are inclusive and independently combinable (e.g., ranges of “up to about 25 wt. %, or, more specifically, about 5 wt. % to about 20 wt. %,” is inclusive of the endpoints and all intermediate values of the ranges of “about 5 wt. % to about 25 wt. %,” etc.).
- the modifier “about” used in connection with a quantity is inclusive of the stated value and has the meaning dictated by the context (e.g., includes the degree of error associated with measurement of the particular quantity).
- percent (%) conversion is meant to indicate change in molar or mass flow of reactant in a reactor in ratio to the incoming flow
- percent (%) selectivity means the change in molar flow rate of product in a reactor in ratio to the change of molar flow rate of a reactant. It is to be understood that use of the term “plug flow” herein indicates that the reactor approximates ideal plug flow, not necessarily that ideal plug flow is achieved.
- the present invention provides an adiabatic plug flow reactor suitable for use in a continuous, gas phase, free radical process for the production of chlorinated and/or fluorinated propene and higher alkenes.
- the reactor comprises a design that minimizes the production of by-products, including decomposition products of reaction components that may foul the reactor.
- the percent conversion of the reaction carried out within the reactor may be kept within a desired range.
- the conversion can be caused to increase less than about 5%, or less than about 2%, or even less than about 1%, so that a desired selectivity can be seen.
- selectivity to the desired product can be as high as about 70%, or about 75%, or about 80%, or even about 85% or greater.
- the present tubular plug flow reactor is particularly well suited for conducting reactions for which an increase in percent conversion may typically indicate increased production of reaction by-products, and thus, reduced percent selectivity.
- the reactors described herein may be utilized in any continuous gas-phase, free radical process, and in particular, are well suited for such reactions that are also homogeneous and exothermic.
- the reactors described herein are also particularly appropriately employed for reactions involving at least one limiting reactant having a desired conversion far from exhaustion of the same, e.g., conversions of less than 80%, or less than 40%, or even less than 20% of the limiting reactant.
- the present reactors are also particularly well suited for such reactions particularly susceptible to the formation of by-products, and the effects thereof on reaction selectivity, or comprising thermally sensitive components, e.g., that may react, or degrade, to form undesirable by-products.
- Thermally sensitive components may include, for example, reactants, products, catalysts, and even by-products which may further react or thermally degrade to form other by-products. Reactions comprising combinations of thermally sensitive components may also find benefit from being carried out in the present reactors. Even at such low conversions of limiting reagent, and when used to conduct reactions susceptible to the formation of by-products, the present reactors can provide selectivity to the desired product of at least about 70%, or about 75%, or about 80%, or even about 85% or greater.
- reactions includes, but is not limited to, reactions that produce chlorinated and/or fluorinated propene and higher alkenes.
- Preferred alkenes include those having from about three to about six carbon atoms.
- Exemplary reactions include reactions of methanes, including chloromethanes, fluoromethanes or chlorofluoromethanes, having the formula CH 4-a-b Cl a F b , wherein each a and b are independently 0-3 and 4-a-b is greater than 0; and chloroethylenes or chlorofluoroethylenes to provide chlorinated and/or fluorinated propenes according to the formula CH 2-c-g Cl c F g ⁇ CH 1-d-h Cl d F h —CH 3-e-f Cl e F f wherein c is 0-2, d is 0-1, e is 0-3, f is 0-3, and g is 0-2 while c+g ⁇ 2, d+h ⁇ 1, and c+f ⁇ 3.
- Particular exemplary reactions include the reaction of methyl chloride with perchloroethylene to provide 1,1,2,3-tetrachloropropene, the reaction of methyl fluoride with perchloroethylene to provide 1,1,2-chloro-3-fluoro-propene, and the reaction of methyl fluoride with triflurochloroethylene to provide 1,1,2,3-tetrafluoropropene.
- these are intended only to be exemplary and are not to be construed as limiting to the concepts described herein.
- processes for the production of chlorinated or fluorinated propenes may typically result in the formation of larger quantities of reaction by-products than conventional halogenation processes. That is, in conventional free radical halogenation reactions, reactor promoted backmixing or recirculation, such as that provided by jet stirred reactors, is typically considered to increase productivity of the reactor, without concurrent increases in byproduct formation [Liu et al, Chemical Engineering Science 59 (2004) 5167-5176]. In the present processes, such backmixing or recirculation would result in the formation of unacceptable amounts of by-products.
- reactor fouling can effectively reduce the reactor volume available for the desired reaction to take place. Undesirable time or cost expense may also be added to the process, via the cleaning necessitated for a reactor fouled to such an extent that a commercially acceptable throughput is no longer possible.
- the present improved reactors for the production of chlorinated and/or fluorinated propenes or higher alkenes that minimize the formation of by-products at least by minimizing or eliminating the amount of backmixing and/or recirculation that occurs in the reactor.
- backmixing and/or recirculation is not detrimental, and may even be desired, since the limiting reagent experiences a 100% conversion.
- the conversion of the limiting reagent may be less than 80% or less than 40%, or even less than 20%. Substantially increasing the conversion of such reactions is typically not desirable, since the same can result in the increased formation of by-products rather than increased formation of desired end-product.
- the present reactors can provide selectivity to the desired product of at least about 70%, or about 75%, or about 80%, or even about 85% or greater.
- One example of a design that facilitates reduced backmixing and/or recirculation zone to reduce formation of by-products during any backmixing that may occur, prior to entry into, or upon exit from, the reactor involves the use of the reactor without a mixer and/or collector, or the redesign of any mixer and/or collector desirably utilized to minimize backmixing. That is, many tubular reactors may be configured with a mixer and/or collector fluidly connected thereto, wherein reactants are provided to the reactor, or reactor effluent is dispensed therefrom, as the case may be. Backmixing may typically occur in such conventional mixers/collectors, and/or mixers/collectors arranged conventionally with respect to the reactor.
- FIG. 1 One example of a conventional mixer, within which backmixing may occur, is shown in FIG. 1 .
- mixer 100 as shown in FIG. 1 is a conventional T-mixer comprising inlets 102 and 104 and conduit 106 .
- FIG. 1 also shows reactor 108 and the relationship thereof to mixer 100 .
- inlets 102 and 104 would be fluidly connected to feed sources (not shown) and provide feedstreams 110 and 112 , respectively, of, e.g., reactants and/or diluents to and through conduit 106 .
- Conduit 106 in turn, is fluidly connected with reactor 108 .
- feedstream 110 contacts feedstream 112 within conduit 106 . Due to the fluid dynamics created by the perpendicular relationship of inlet 102 and inlet 104 , suboptimal mixing of feedstream 110 and feedstream 112 may typically occur.
- Cross section 114 taken at line A-A across mixer 100 , shows the relationship of feedstream 110 and feedstream 112 that may typically result from this suboptimal mixing.
- the combined feedstreams 110 and 112 are expected to fan out upon entry into reactor 108 in a generally conical pattern, creating deadspaces 116 and 118 , within which undesirable backmixing or recirculation may occur.
- deadspaces 116 and 118 many conventional processes/reactions conducted in reactors comprising such a conventional mixer rely on a reduced inlet temperature at which the undesirable reactions do not occur, or occur to a lesser extent.
- a reduced inlet temperature requires an increased reaction volume, which may be undesirable in many applications.
- the present reactors may be provided without a conventional mixer and/or collector, so that the reactants are fed substantially directly into the reactor and/or the reactor effluent is passed from the reactor directly to a liquid quench zone.
- the diameter/shape of the reactor and any mixer and/or collector may be configured to be substantially the same, so that areas of backmixing or recirculation are not created in dead space created by disparate geometries between the reactor and collector.
- Any such mixer/collector will also desirably be placed about the same longitudinal axis as the reactor, so that the reactants and the reactor effluent flow in a direction substantially parallel to the longitudinal axis.
- Reduced backmixing or recirculation may also be provided by providing the reactor with a mixer design that minimizes the same.
- a mixer design that minimizes the same.
- FIG. 2 One example of such a design is shown in FIG. 2 .
- mixer 200 is generally of a shell and tube configuration, i.e., mixer 200 comprises inlet 202 fluidly connected to tubes 206 .
- Inlet 202 provides feedstream 210 from a feed source (not shown) to reactor 208 .
- Mixer 200 also comprises inlet 204 , which is fluidly connected to shell 216 .
- Inlet 204 provides feedstream 212 from a feed source (not shown) therethrough to reactor 208 .
- feedstreams 210 and 212 are more uniformly and optimally mixed than the mixing provided by conventional mixer 100 shown in FIG. 1 , as further illustrated by cross section 214 taken at interface 218 .
- mixer 200 substantially eliminates the deadspaces present in many conventional mixers (such as deadspaces 116 and 118 shown in FIG. 1 ), and thus, substantially eliminates backmixing that may occur in such deadspaces.
- the temperature at the reactor inlet can be optimized for the reaction, rather than adjusted to minimize backmixing reactions.
- the reactor may additionally comprise one or more other design features to further minimize the formation of by-products, or to reduce or eliminate the impact of any by-products that are formed.
- the reactors provided herein may comprise one or more of i) a design that minimizes heat transfer to and/or from the reactor; ii) a design that optimizes the flow of the reaction components at the boundary between the reaction components and at least a portion of at least one reactor tube wall; iii) a design that facilitates a reduction of the temperature of a reactor effluent to a temperature below which substantial formation of by-products does not occur, and/or iv) a design that allows the production rate of a reaction conducted in the reactor to be adjusted by controlling the temperature of the reactor effluent. Any number of the reactor designs described herein may be used in any combination.
- the present reactors may be provided with a design that facilitates minimized heat transfer to and/or from the reactor, i.e., that facilitate the capability of the reactor to operate substantially adiabatically.
- adiabatically as applied to the tubular reactors described herein means that any substantial heating or cooling within the reactor is provided by the exothermic or endothermic reactions being conducted therein, with little or no heating or cooling provided from outside sources.
- Insulating the reactor with any amount of insulation of one type, or a combination of types, in any number of layers, is but one exemplary method to minimize heat transfer.
- utilization of an insulation having an effective thermal conductivity of 0.05 W/M/° C. is expected to maintain reagent conversion close to 10% in a reactor with 6 ft ID.
- Examples of insulating material with approximately this effective thermal conductivity value include, but are not limited to, wool, fiber glass wool, Kapok, rock wool, balsam wool, cardboard, corkboard, silica aerogel, wood shavings, balsa, plaster gypsum, diatomaceous earth brick, or combinations of these.
- the present reactor may comprise an insulation layer of carbon steel, brick, or ceramic to minimize corrosion and an insulation layer of a less exotic and/or costly material, such as e.g., glass wool to provide a heat transfer barrier.
- Reactor diameter may also be optimized so that heat transfer to and/or from the reactor is minimized.
- the reactor diameter may desirably be at least about 0.5 feet, or at least about 4 feet or greater, so that heat transfer to and/or from the reactor is minimized.
- Increased residence time through conventional tubular reactors may also lead to the formation of undesirable by-products, and may generally occur due to the velocity gradient layer at the interface between an internal wall of a reactor tube and the reaction mixture flowing therethrough.
- the velocity of the reaction mixture in this layer is typically less than the velocity of the reaction mixture in the bulk velocity. Indeed, the velocity of the velocity gradient layer can approach zero at the reactor wall. Because of this lower velocity, reactants in this layer may experience longer residence time(s) during which unwanted side reactions may occur. Minimizing any such layer can assist in the optimization of the residence time of the reaction components within the reactor, and thus, reduced formation of by-products that may otherwise be formed.
- the reactor(s) may be provided with a design that optimizes the flow of the reaction components within the velocity gradient layer. In one embodiment, this can be achieved by minimizing the depth/thickness of the layer, as can be achieved by providing a turbulence flow region within at least a portion of the reactor definable by a Reynolds number (Re) of at least about 2100.
- Re Reynolds number
- the Reynolds number can be determined by the equation
- G is the mass flow rate (kg/s)
- D is the tube inner diameter (m)
- ⁇ is the viscosity (1/kg/m/s), respectively) of at least about 2100.
- one such embodiment may comprise providing a flow rate of about 3.6 MM#/d through a reactor having an internal diameter of about 6 ft or less is be expected to exhibit a Reynolds number of greater than 580,000 for the exemplary reaction of methyl chloride and perchloroethylene to produce 1,1,2,3-tetrachloropropene.
- the Reynolds number can be determined dividing the hydraulic diameter D h , which, in turn, is 4 times the cross-sectional area of flow, by the wetted perimeter, w. In such embodiments, the equation used to determine the Reynolds number would be
- G is the mass flow rate (kg/s)
- ⁇ is the viscosity (1/kg/m/s)
- the present reactors may also be provided with a design that facilitates providing a reactor effluent with a temperature that discourages reactions that form by-products in any collector provided in connection with the reactor, or as the reaction effluent is provided to a downstream process prior to a reaction zone within at least one reactor tube.
- a temperature will depend upon the reaction desirably taking place within the reactor, and it is expected that those of ordinary skill in the art will be able to determine the same.
- the effluent temperature will desirably be less than 350° C., or less than 270° C., so that the methyl chloride and perchloroethylene, do not substantially react to provide by-products such as, e.g., tetrachlorobutenes, graphite and other carbonaceous deposits and/or hydrogen chloride.
- the temperature of the reactor effluent is desirably reduced quickly, i.e., before any substantial amount of such by-products has had the opportunity to form.
- the temperature of the reactor effluent will desirably be cooled to below 350° C. or below about 270° C. in less than about 5 seconds, or even less than about 1 second.
- the reactor effluent will desirably be cooled at a rate of at least about 20° C./sec, or 50° C./sec, or even about 100° C./sec.
- the desired temperature can be affected using any suitable method of doing so at the desired rate, and in some embodiments may be accomplished via liquid quenching.
- the quench function may be performed by any suitable method, such as, e.g., application of a temperature adjusting fluid via at least one nozzle, spray nozzle or weir nozzle.
- the temperature adjusting fluid utilized in the quench function can be any suitable fluid capable of providing the desired temperature within the desired amount of time.
- the temperature adjusting fluid may be a reaction component, so that further components are not added to the process, requiring later separation and thereby adding to process cost.
- a recycled reaction product may be utilized to perform the quench function, and may be purified, e.g., via filtration, prior to being so utilized, or may be utilized in unpurified form.
- the reactor provided herein may comprise a design that allows the production rate to be adjusted by controlling the temperature of the reactor effluent. Many methods of doing so are known to those of ordinary skill in the art, and any of these may be utilized in the present reactors.
- One exemplary method comprises providing the reactor with a design that allows for individual adjustment of the flow rate and/or temperature of one or more reactants, initiator(s), and/or diluent(s).
- Individual flow rate adjustment can be provided by providing separate inlets for the reaction components desirably adjusted, and further providing each inlet with an adjustable valve.
- individual temperature adjustment can be provided by providing a separate method of temperature control for each reaction component desirably controlled or adjusted. For example, individual preheaters can be provided for each reaction component for which individual temperature adjustment is desirable.
- the flow rate and/or temperature provided to the reactant(s), initiator(s), and/or diluents(s) will depend upon the particular reaction being carried out, and the production rate desirably achieved.
- methyl chloride and perchloroethylene to produce e.g., 1,1,2,3-tetrachloropropene
- flow rates of methyl chloride and perchloroethylene of from about 1.5 to about 2.0 MM#/d (millions of pounds per day) and from about 2.0 to about 2.7 MM#/d, respectively, are expected to be suitable.
- the flow rate of the same may be from about 0.20 to about 0.25 MM#/d.
- Appropriate temperatures to achieve such a production rate for the reactants of this particular reaction are from about 350° C. to about 500° C. for methyl chloride (preferably 400° C. to 450° C.), from about 250 to 400° (preferably) 300° C. to about 375° C. for perchloroethylene, and from about 300° C. to about 325° C. for carbon tetrachloride, if an initiator is utilized.
- One or more of the improved design concepts may advantageously be employed in a reactor for use in a continuous gas phase, free-radical process and are expected to minimize production of by-products, including decomposition products, within the reactor.
- any two of the design concepts may be employed, any three of the design concepts may be employed, any four of the design concepts may be employed, or all five of the design concepts may be employed.
- the reactor comprises one, two, three, four or all five of the design concepts, the percent conversion of the reaction carried out within the reactor may be kept within a desired range, e.g., the percent conversion may vary by less than about 2%, or even less than about 1%, from the desired conversion, so that the desired percent selectivity may be seen.
- the present reactors are particularly well suited for conducting reactions for which an increase in percent conversion may typically indicate increased production of reaction by-products, and thus, reduced percent selectivity.
- Such reactions may also typically include at least one limiting reactant having desired conversions that are far from exhaustion, e.g., conversions of less than 80%, or less than 40%, or even less than 20%.
- at a limiting reagent conversion of at least about 5%, or at least about 10%, or at least about 15%, or even at least about 20% selectivity to the desired product can be as high as about 70%, or about 75%, or about 80%, or even about 85% or greater.
- the reduced production of by-products can also reduce fouling of the reactor tube wall, thereby preserving reactor capacity and thus, reaction yield.
- One example of a continuous, gas-phase, free radical process that may advantageously be carried out in the present reactors includes processes for the production of chlorinated and/or fluorinated alkenes comprising from about three to about six carbon atoms, in particular those making use of catalysts/initiators comprising chlorine.
- Such catalysts can be thermally sensitive and can degrade or otherwise undesirably react to result in reactor fouling.
- the reaction product itself is not only thermally unstable, but also, prone to react further with reactants and reaction by-products to form yet other by-products.
- 1,1,2,3-tetrachloropropene is reactive at 370° C. with methyl chloride and perchloroethylene, thermally unstable at 400° C.-500° C., and especially unstable at conventional reaction conditions for its production, i.e., at temperatures of from about 500° C. to about 750° C.
- the ensuing undesired reactions and/or decompositions lead to high concentrations of impurities, and ultimately thermal coking at these higher temperatures.
- coking is well known to cause further loss of reactor production capacity with time and often requires shutting down a reactor for cleaning and maintenance.
- Processes performed in the present reactors can be provided with minimized production of by-products and/or decomposition products with at least 5% conversion of the limiting reagent or at least about 10%, or at least about 15%, or even at least about 20%, while maintaining selectivity to the desired product as high as about 70%, or about 75%, or about 80%, or even about 85% or greater.
- the limiting reagent perchloroethylene is expected to conversion to the desired product at 90% selectivity when converted at least 5%.
- use of the present reactors in continuous processes for the production of chlorinated and/or fluorinated propene and higher alkenes can provide significant time and cost savings.
- the efficiencies provided by the present reactors can be further leveraged by providing the chlorinated and/or fluorinated propene and higher alkenes produced therein to further downstream processes.
- 1,1,2,3-tetrachloropropene produced using the described reactors can be processed to provide further downstream products including hydrofluoroolefins, such as, for example, 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze).
- HFO-1234yf 2,3,3,3-tetrafluoroprop-1-ene
- HFO-1234ze 1,3,3,3-tetrafluoroprop-1-ene
- the conversion of chlorinated and/or fluorinated propene and higher alkenes to provide hydrofluoroolefins may broadly comprise a single reaction or two or more reactions involving fluorination of a compound of the formula C(X) m CCl(Y) n (C)(X) m to at least one compound of the formula CF 3 CF ⁇ CHZ, where each X, Y and Z is independently H, F, Cl, I or Br, and each m is independently 1, 2 or 3 and n is 0 or 1.
- a more specific example might involve a multi-step process wherein a feedstock of 1,1,2,3-tetrachloropropene is fluorinated in a catalyzed, gas phase reaction to form a compound such as 2-chloro-3,3,3-tri-fluoropropene.
- the 2-chloro-2,3,3,3-tetrafluoropropane is then dehydrochlorinated to 2,3,3,3-tetrafluoropropene via a catalyzed, gas phase reaction.
- a 1′′ ID Hastelloy reactor is heated to from about 450° C. to about 480° C.
- Methyl chloride and perchloroethylene flow are established at from about 50 ml/hr to about 150 ml/hr and from about 180 ml/hr to about 123 ml/hr liquid flow, respectively, to achieve a residence time of from about 10 seconds to about 23 seconds.
- the liquid feeds are evaporated separately and preheated to achieve the same temperature as the reactor temperature in the feed line before they are mixed in 1 ⁇ 2′′ line before feeding into the reactor.
- the reactor pressure is set at 14.7 psia.
- the front section (conventional mixing zone) of the 1′′ reactor was filled with Rashig rings at a depth of 2 inches to provide at least approximated plug flow and proper mixing.
- perchloroethylene and methyl chloride are reacted in the presence of the initiator carbon tetrachloride to provide 1,1,2,3 -tetrachloropropene in a reactor comprising both a design that allows the production rate to be adjusted by controlling the temperature of the reactor effluent and a design that facilitates reduced backmixing prior to entry into the adiabatic plug flow reactor.
- the reactor comprises a mixer having the design shown in FIG. 2 , and, separate evaporators for the perchloroethylene and methyl chloride.
- Perchloroethylene will be introduced into a 6 foot internal diameter tubular reactor at a temperature of about 325° C. and a feed rate of about 2.65 MM#/day. Methyl chloride will be fed at a rate of 2.01 MM#/day and a temperature of 430° C., while carbon tetrachloride will be provided to the reactor at a feed rate of 0.25 MM#/day and at a temperature of 325° C. Because the perchloroethylene is set at a lower temperature than the methyl chloride stream, the reaction fluid enters the reactor at a temperature of 383° C. with the pressure of the reactor maintained at 260 psig.
- perchloroethylene and methyl chloride are reacted in the presence of the initiator carbon tetrachloride to provide 1,1,2,3 -tetrachloropropene in a reactor comprising both a design that allows the production rate to be adjusted by controlling the temperature of the reactor effluent and a design that facilitates reduced backmixing and/or recirculation prior to entry into the adiabatic plug flow reactor.
- the reactor utilized comprises a mixer having the design shown in FIG. 2 , and, separate evaporators for the perchloroethylene/carbon tetrachloride and methyl chloride.
- Methyl chloride, perchloroethylene and carbon tetrachloride were fed to a 2′′ ID Inconel 600 reactor at the rate of 3500-4500 SCCM, 1400-17000 SCCM, and 700-980 SCCM respectively to achieve about 30-40 seconds residence time at 260 psig.
- the reactor is equipped with the mixer shown in FIG. 2 .
- the methyl chloride stream was preheated to from about 340° C. to about 370° C. while the perchloroethylene/carbon tetrachloride stream was preheated to from about 310° C. to about 360° C.
- Reactor temperatures of from about 405° C. to about 415° C. resulted in a perchloroethylene conversion of from about 7.2% to about 9.6% and 1,1,2,3-tetrachloropropene selectivity of from about 87% to about 90%.
- the reactor productivity was found to be 80-120 gr/hr/l. After about 7 days of continuous operation, the reactor was shut down and inspected. The reaction zone was found to have a slight coating of carbon deposit.
- Chlorinated and/or fluorinated propenes having the formula CH 2-c-g Cl c F g ⁇ CH 1-d-h Cl d F h —CH 3-e-f Cl e F f wherein c is 0-2, d is 0-1, e is 0-3, f is 0-3, and g is 0-2 while c+g ⁇ 2, d+h ⁇ 1, and e+f ⁇ 3 are prepared using a reactor having a design that minimizes heat transfer to and/or from the reactor, and in accordance with Examples 2 and 3. With overall reactor volume similar to that described in Example 2, Table 1 shows that at least 10 cm insulation with effective thermal conductivity of 0.05 W/M/° C. is expected to maintain reagent conversion close to 10% in a reactor with 6 ft ID.
- Table 1 also shows that removing the insulation, leaving the reactor metal wall of Inconel results in an effective thermal conductivity of 20 W/M/° C. and this is expected to drop the conversion or productivity by more than 50% if the same reactor length is used. Reducing the reactor diameter to 1 ft keeping the same reactor volume and insulation thickness the same results in about 10% drop in reactor productivity. Increasing the insulation thickness by 150% is expected to regain the productivity by 5%.
- Chlorinated and/or fluorinated propenes having the formula CH 2-c-g Cl c F g ⁇ CH 1-d-h Cl d F h —CH 3-e-f Cl e F f wherein c is 0-2, d is 0-1, e is 0-3, f is 0-3, and g is 0-2 while c+g ⁇ 2, d+h ⁇ 1, and e+f ⁇ 3, are prepared using a reactor having a design that minimizes heat transfer to and/or from the reactor as shown in Table 2, and in accordance with Examples 2 and 3.
- “Cony” means conversion
- “Sel” means selectivity.
- Chlorinated and/or fluorinated propenes having the formula CH 2-c-g Cl c F g ⁇ CH 1-d-h Cl d F h —CH 3-e-f Cl e F f wherein c is 0-2, d is 0-1, e is 0-3, f is 0-3, and g is 0-2 while c+g ⁇ 2, d+h ⁇ 1, and e+f ⁇ 3 are prepared using a reactor having a design that optimizes the flow of the reaction components within the velocity gradient layer, and in accordance with Example 2. As shown in Table 3, a large reactor inner diameter must be used to maintain a Reynolds number below 2100 and to achieve laminar flow condition even at 100 ⁇ lower production rate with similar reactor volume and other operating condition as used in Example 2.
- Chlorinated and/or fluorinated propenes having the formula CH 2-c-g Cl c F g ⁇ CH 1-d-h Cl d F h —CH 3-e-f Cl e F f wherein c is 0-2, d is 0-1, e is 0-3, f is 0-3, and g is 0-2 while c+g ⁇ 2, d+h ⁇ 1, and e+f ⁇ 3, are prepared using a reactor having a design that optimizes the flow of the reaction components within the velocity gradient layer as shown in Table 4, and in accordance with Example 2.
- Chlorinated and/or fluorinated propenes having the formula CH 2-c-g Cl c F g ⁇ CH 1-d-h Cl d F h —CH 3-e-f Cl e F f wherein c is 0-2, d is 0-1, e is 0-3, f is 0-3, and g is 0-2 while c+g ⁇ 2, d+h ⁇ 1, and e+f ⁇ 3 are prepared using a reactor and operating conditions in accordance with Example 3.
- the reactor effluent is at a temperature of from about 410° C. to about 420° C. and is cooled to a temperature of from about 270° C. to about 350° C. at a residence time of about less than 10 seconds before being condensed in a 0.5inch ID cooling coil at temperature of less than about 80° C.
- a week of run time at low perchloroethylene conversion of from about 3.8% to about 5.0% the reactor is severely fouled in the cool down zone and the condensing coil and is shutdown due to plugging.
- Chlorinated and/or fluorinated propenes having the formula CH 2-e-g Cl c F g ⁇ CH 1-d-h Cl d F h —CH 3-e-f Cl e F f wherein c is 0-2, d is 0-1, e is 0-3, f is 0-3, and g is 0-2 while c+g ⁇ 2, d+h ⁇ 1, and e+f ⁇ 3 are prepared using a reactor having a design that facilitates providing a reactor effluent with a temperature that discourages reactions that form by-products as shown in Table 5, and also in accordance with Example 3.
- Chlorinated and/or fluorinated propenes having the formula CH 2-c-g Cl c F g ⁇ CH 1-d-h Cl d F h —CH 3-e-f Cl e F f wherein c is 0-2, d is 0-1, e is 0-3, f is 0-3, and g is 0-2 while c+g ⁇ 2, d+h ⁇ 1, and e+f ⁇ 3 are prepared using a reactor having a given volume and a design that allows the production rate to be adjusted by controlling the temperature of the reactor effluent, and also in accordance with Example 2.
- Chlorinated and/or fluorinated propenes having the formula CH 2-c-g Cl c F g ⁇ CH 1-d-h Cl d F h —CH 3-e-f Cl e F f wherein c is 0-2, d is 0-1, e is 0-3, f is 0-3, and g is 0-2 while c+g ⁇ 2, d+h ⁇ 1, and e+f ⁇ 3, are prepared using a reactor having a given volume and a design that allows the production rate to be adjusted by controlling the temperature of the reactor effluent, and also in accordance with Example 2.
- reactant 1 (R1) CH 4-a-b Cl a F b and reactant 2 (R2) is a chlorofluoroethylene.
- Hydrofluoroolefins are prepared from the chlorinated and/or fluorinated propenes prepared according to Examples 1-4 by any of several methods known in the art. For example, the conversion of 1,1,2,3-tetrachlororopropene to HFO-1234yf using HF with Chromium/Cobalt base catalyst may be prepared in accordance with the methodology described in WO2008054781A1.
- WO 2009003084 describes a multi-step process wherein a feedstock of 1,1,2,3 tetrachloropropene is fluorinated in a liquid phase without a catalyst followed by a catalyzed, gas phase reaction to form 2-3,3,3-tetrafluoropropene (HFO1234yf) that is also suitable.
- US20090030244A1 describes the production of HFO-1234yf using 1,1,2,3-tetrachloropropene using a catalytic process with HF with HCFC-1233xf as intermediate, and this process may also be used.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US12/901,383 US20110087056A1 (en) | 2009-10-09 | 2010-10-08 | Adiabatic plug flow reactors and processes incorporating the same |
US15/204,462 US10189756B2 (en) | 2009-10-09 | 2016-07-07 | Adiabatic plug flow reactors and processes incorporating the same |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US25002309P | 2009-10-09 | 2009-10-09 | |
US12/901,383 US20110087056A1 (en) | 2009-10-09 | 2010-10-08 | Adiabatic plug flow reactors and processes incorporating the same |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US15/204,462 Division US10189756B2 (en) | 2009-10-09 | 2016-07-07 | Adiabatic plug flow reactors and processes incorporating the same |
Publications (1)
Publication Number | Publication Date |
---|---|
US20110087056A1 true US20110087056A1 (en) | 2011-04-14 |
Family
ID=43664358
Family Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US12/901,383 Abandoned US20110087056A1 (en) | 2009-10-09 | 2010-10-08 | Adiabatic plug flow reactors and processes incorporating the same |
US15/204,462 Expired - Fee Related US10189756B2 (en) | 2009-10-09 | 2016-07-07 | Adiabatic plug flow reactors and processes incorporating the same |
Family Applications After (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US15/204,462 Expired - Fee Related US10189756B2 (en) | 2009-10-09 | 2016-07-07 | Adiabatic plug flow reactors and processes incorporating the same |
Country Status (7)
Country | Link |
---|---|
US (2) | US20110087056A1 (zh) |
EP (1) | EP2485833A2 (zh) |
JP (2) | JP5947214B2 (zh) |
KR (1) | KR20120093202A (zh) |
CN (2) | CN102665890B (zh) |
BR (1) | BR112012007913A2 (zh) |
WO (1) | WO2011044522A2 (zh) |
Cited By (25)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20140182726A1 (en) * | 2012-12-28 | 2014-07-03 | Horiba Stec, Co., Ltd. | Fluid mixing element |
US8889930B2 (en) | 2013-01-22 | 2014-11-18 | Axiall Ohio, Inc. | Process for producing chlorinated hydrocarbons |
US8957268B2 (en) | 2009-10-12 | 2015-02-17 | Elevance Renewable Sciences, Inc. | Methods of refining natural oil feedstocks |
US9051519B2 (en) | 2009-10-12 | 2015-06-09 | Elevance Renewable Sciences, Inc. | Diene-selective hydrogenation of metathesis derived olefins and unsaturated esters |
US9139497B2 (en) | 2013-10-23 | 2015-09-22 | Axiall Ohio, Inc. | Process for producing chlorinated hydrocarbons in the presence of a polyvalent bismuth compound |
US9199899B2 (en) | 2011-12-02 | 2015-12-01 | Blue Cube Ip Llc | Process for the production of chlorinated alkanes |
US9233896B2 (en) | 2011-08-07 | 2016-01-12 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9289758B2 (en) | 2013-01-22 | 2016-03-22 | Axiall Ohio, Inc. | Processes for producing chlorinated hydrocarbons and methods for recovering polyvalent antimony catalysts therefrom |
US9321707B2 (en) | 2012-09-20 | 2016-04-26 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9353029B2 (en) | 2013-03-14 | 2016-05-31 | Honeywell International, Inc. | Fluorination process and reactor |
US9359273B2 (en) | 2011-10-14 | 2016-06-07 | Honeywell International Inc. | Process for producing 2,3,3,3-tetrafluoropropene |
US9365487B2 (en) | 2009-10-12 | 2016-06-14 | Elevance Renewable Sciences, Inc. | Methods of refining and producing dibasic esters and acids from natural oil feedstocks |
US9382502B2 (en) | 2009-10-12 | 2016-07-05 | Elevance Renewable Sciences, Inc. | Methods of refining and producing isomerized fatty acid esters and fatty acids from natural oil feedstocks |
US9382176B2 (en) | 2013-02-27 | 2016-07-05 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
JP2016135490A (ja) * | 2016-05-02 | 2016-07-28 | 株式会社堀場エステック | 流体混合素子 |
US9403741B2 (en) | 2013-03-09 | 2016-08-02 | Blue Cube Ip Llc | Process for the production of chlorinated alkanes |
US9475740B2 (en) | 2012-12-19 | 2016-10-25 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9475739B2 (en) | 2011-08-07 | 2016-10-25 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9512053B2 (en) | 2012-12-18 | 2016-12-06 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9512049B2 (en) | 2011-12-23 | 2016-12-06 | Dow Global Technologies Llc | Process for the production of alkenes and/or aromatic compounds |
US9598334B2 (en) | 2012-09-20 | 2017-03-21 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9795941B2 (en) | 2012-09-30 | 2017-10-24 | Blue Cube Ip Llc | Weir quench and processes incorporating the same |
US10065157B2 (en) | 2012-10-26 | 2018-09-04 | Blue Cube Ip Llc | Mixer and processes incorporating the same |
US10076739B1 (en) * | 2014-07-22 | 2018-09-18 | Precision Combustion, Inc. | Chemical reactor for use with overly reactive chemicals |
CN115106019A (zh) * | 2022-06-23 | 2022-09-27 | 天津大学 | 平推流反应器和平推流反应器实验*** |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9150841B2 (en) * | 2012-06-29 | 2015-10-06 | Shire Human Genetic Therapies, Inc. | Cells for producing recombinant iduronate-2-sulfatase |
US10870613B2 (en) * | 2016-11-29 | 2020-12-22 | Srf Limited | Process for the preparation of 2,3,3,3-tetrafluoropropene |
CN107918277A (zh) * | 2017-11-13 | 2018-04-17 | 浙江大学 | 一种基于自适应控制网格的活塞流管式反应器最优控制*** |
FR3082202B1 (fr) | 2018-06-12 | 2020-08-28 | Arkema France | Procede de production de 2,3,3,3-tetrafluoropropene et installation pour la mise en oeuvre de celui-ci. |
FR3082203B1 (fr) | 2018-06-12 | 2020-08-14 | Arkema France | Procede de production de 2,3,3,3-tetrafluoropropene et installation pour la mise en oeuvre de celui-ci. |
FR3082200B1 (fr) * | 2018-06-12 | 2020-08-28 | Arkema France | Procede de production de 2,3,3,3-tetrafluoropropene et reacteur pour la mise en oeuvre de celui-ci. |
FR3098127B1 (fr) | 2018-06-12 | 2022-10-21 | Arkema France | Procédé de production de 2,3,3,3-tétrafluoropropène et réacteur pour la mise en œuvre de celui-ci |
FR3082201A1 (fr) | 2018-06-12 | 2019-12-13 | Arkema France | Procede de production de 2,3,3,3-tetrafluoropropene, reacteur et installation pour la mise en oeuvre de celui-ci. |
FR3082204B1 (fr) * | 2018-06-12 | 2020-08-14 | Arkema France | Procede de production de 2-chloro-3,3,3-trifluoropropene et installation pour la mise en oeuvre de celui-ci. |
CN110746265B (zh) * | 2019-10-09 | 2021-02-26 | 浙江大学 | 一种液相法管道化连续化生产氟化烷烃的方法 |
FR3098216B1 (fr) | 2020-07-03 | 2023-01-13 | Arkema France | Procédé de production de 2,3,3,3-tétrafluoropropène et installation pour la mise en œuvre de celui-ci |
Citations (100)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2119484A (en) * | 1935-05-06 | 1938-05-31 | Du Pont | Chlorination of propylene dichloride |
US2179378A (en) * | 1936-07-18 | 1939-11-07 | Air Reduction | Production of acetylene |
US2207193A (en) * | 1937-09-14 | 1940-07-09 | Shell Dev | Production of allyl type halides |
US2299441A (en) * | 1939-09-02 | 1942-10-20 | Shell Dev | Catalytic halo-substitution of saturated organic compounds |
US2302228A (en) * | 1940-04-02 | 1942-11-17 | Du Pont | Method of chlorination with sulphuryl chloride and production of monochloro-trimethyl acetic acid |
US2370342A (en) * | 1940-04-30 | 1945-02-27 | Tide Water Associated Oil Comp | Halogenation |
US2378859A (en) * | 1941-08-08 | 1945-06-19 | Distillers Co Yeast Ltd | Splitting-off of hydrogen halide from halogenated hydrocarbons |
US2435983A (en) * | 1945-12-01 | 1948-02-17 | Universal Oil Prod Co | Production of liquid hydrocarbons |
US2449286A (en) * | 1945-07-16 | 1948-09-14 | Shell Dev | Production of 1, 3-dihalopropylenes |
US2588867A (en) * | 1948-10-25 | 1952-03-11 | Dow Chemical Co | Pyrolytic production of chlorohydrocarbons |
US2630461A (en) * | 1953-03-03 | Production of acetylene by incom | ||
US2688592A (en) * | 1950-10-21 | 1954-09-07 | Diamond Alkali Co | Photochemical process for preparing carbon tetrachloride |
US2762611A (en) * | 1952-02-28 | 1956-09-11 | Pfaudler Co Inc | Tubular heat exchangers |
US2765359A (en) * | 1953-02-10 | 1956-10-02 | Hydrocarbon Research Inc | Production of acetylene |
US2964579A (en) * | 1958-10-09 | 1960-12-13 | Houdry Process Corp | Selective hydrogenation of diolefins with copper chromite catalyst |
US2973393A (en) * | 1958-10-02 | 1961-02-28 | Dow Chemical Co | Chlorination of acetylenes |
US3000980A (en) * | 1958-04-07 | 1961-09-19 | Dow Chemical Co | Preparation of alkyl bromides |
US3094567A (en) * | 1960-02-25 | 1963-06-18 | Monsanto Chemicals | Chlorination of propynes |
US3112988A (en) * | 1960-02-26 | 1963-12-03 | Sheil Oil Company | Mixing gases at supersonic velocity |
US3444263A (en) * | 1966-11-09 | 1969-05-13 | Gulf Research Development Co | Method for converting ethylene to alpha olefins in the presence of an organic sulfide |
US3446859A (en) * | 1962-06-11 | 1969-05-27 | Hooker Chemical Corp | Vapor phase condensation process |
US3502734A (en) * | 1966-05-11 | 1970-03-24 | Du Pont | Process for partially chlorinating methyl chloride and/or methylene chloride |
US3525595A (en) * | 1967-05-19 | 1970-08-25 | Bayer Ag | Concentric cross flow nozzle apparatus for carrying out reactions between gases |
US3551512A (en) * | 1968-11-01 | 1970-12-29 | Diamond Shamrock Corp | Pressure process for preparing acetylene |
US3558438A (en) * | 1968-10-30 | 1971-01-26 | Du Pont | Distillation process and apparatus |
US3651019A (en) * | 1961-09-28 | 1972-03-21 | Yeda Res & Dev | Production of adducts of carbon tetrachloride or chloroform with olefinically unsaturated substances |
US3676508A (en) * | 1969-01-30 | 1972-07-11 | Hornig Anneliese | Process for the manufacture of carbon tetrachloride |
US3819731A (en) * | 1960-03-23 | 1974-06-25 | Stauffer Chemical Co | Production of chlorinated unsaturated hydrocarbons |
US3823195A (en) * | 1971-12-27 | 1974-07-09 | Monsanto Co | Preparation of 1,1,2,3-tetrachloropropene from 1,2,3-trichloropropane |
US3872664A (en) * | 1973-10-15 | 1975-03-25 | United Aircraft Corp | Swirl combustor with vortex burning and mixing |
US3914167A (en) * | 1974-08-26 | 1975-10-21 | Dow Chemical Co | Process for making cis-1,3-dichloropropene |
US3926758A (en) * | 1971-12-27 | 1975-12-16 | Monsanto Co | Preparation of 1,1,2,3-tetrachloropropene from 2,3-trichloropropane |
US3948858A (en) * | 1973-09-22 | 1976-04-06 | Akzo N.V. | Polymerization of ethylenically unsaturated compounds |
US3954410A (en) * | 1972-11-21 | 1976-05-04 | Merck Patent Gesellschaft Mit Beschraenkter Haftung | Solvents for NMR spectroscopy |
US4038372A (en) * | 1976-05-05 | 1977-07-26 | The United States Of America As Represented By The Secretary Of The Navy | Process for manufacturing chloramine |
US4051182A (en) * | 1976-04-12 | 1977-09-27 | Stauffer Chemical Company | Process for the manufacture of α-chloropropionyl chloride |
US4319062A (en) * | 1976-08-02 | 1982-03-09 | The Dow Chemical Company | Allyl chloride process |
US4513154A (en) * | 1971-07-30 | 1985-04-23 | Allied Corporation | Process for consecutive competitive gas phase reaction |
US4535194A (en) * | 1983-07-06 | 1985-08-13 | Monsanto Co. | Process for producing 1,1,2,3-tetrachloropropene |
US4614572A (en) * | 1985-07-08 | 1986-09-30 | The Dow Chemical Company | Liquid phase chlorination of chlorinated methanes |
US4644907A (en) * | 1985-11-29 | 1987-02-24 | Hunter Edward H | Boiler tubes of enhanced efficiency and method of producing same |
US4650914A (en) * | 1983-07-06 | 1987-03-17 | Monsanto Company | Process for producing 1,1,2,3-tetrachloropropene |
US4661648A (en) * | 1984-08-20 | 1987-04-28 | Solvay & Cie (Societe Anonyme) | Process for carrying out substitution chlorination reactions of organic compounds by means of molecular chlorine in the presence of a chlorinated product serving as a radical initiator, and radical initiators used in such a process |
US4702809A (en) * | 1984-04-25 | 1987-10-27 | Huels Aktiengesellschaft | Process for the production of 1,2,3-trichloro-2-methylpropane |
US4714792A (en) * | 1984-09-06 | 1987-12-22 | Huels Aktiengesellschaft | Process for the production of 1,2,3-trichloropropane |
US4716255A (en) * | 1983-08-25 | 1987-12-29 | Huels Aktiengesellschaft | Process for the production of 3,3-dichloro-2-methylpropene |
US4727181A (en) * | 1986-04-21 | 1988-02-23 | The Dow Chemical Company | Process for the preparation of α-halocinnamate esters |
US4726686A (en) * | 1985-07-30 | 1988-02-23 | Hartmut Wolf | Swirl chamber |
US4849554A (en) * | 1987-04-10 | 1989-07-18 | Imperial Chemical Industries Plc | Production of tetrafluoroethylene and hexafluoropropylene |
US4894205A (en) * | 1987-09-18 | 1990-01-16 | Shell Oil Company | Multitube reactor |
US4902393A (en) * | 1983-08-25 | 1990-02-20 | Huels Aktiengesellschaft | Process for the production of 1,1,2-trichloro-2-methylpropane |
US4999102A (en) * | 1988-12-16 | 1991-03-12 | The Amalgamated Sugar Company | Liquid transfer manifold system for maintaining plug flow |
US5057634A (en) * | 1989-12-19 | 1991-10-15 | E. I. Du Pont De Nemours And Company | Multistep synthesis of hexafluoropropylene |
US5132473A (en) * | 1988-05-17 | 1992-07-21 | Daikin Industries, Ltd. | Process for production of 1,1,1-trifluoro-2,2-dichloroethane |
US5171899A (en) * | 1988-05-17 | 1992-12-15 | Daikin Industries Ltd. | Process for production of 1,1,1-trifluoro-2,2-dichloroethane |
US5178844A (en) * | 1990-04-03 | 1993-01-12 | Phillips Petroleum Company | Method and apparatus for producing nitride products |
US5254771A (en) * | 1989-07-14 | 1993-10-19 | Hoechst Aktiengesellschaft | Process for the preparation of 1,1,1-trifluoro-2-2-dichloroethane under elevated pressure |
US5254788A (en) * | 1991-09-10 | 1993-10-19 | Stone And Webster Engineering Corporation | Process for the production of olefins from light paraffins |
US5254772A (en) * | 1991-03-12 | 1993-10-19 | Imperial Chemical Industries Plc | Chemical process |
US5262575A (en) * | 1992-08-04 | 1993-11-16 | The Dow Chemical Company | Production of allylic chlorides |
US5414166A (en) * | 1993-11-29 | 1995-05-09 | Korea Institute Of Science And Technology | Process for the preparation of 1,1,1-trifluoro-2,2-dichloroethane |
US5684219A (en) * | 1995-08-28 | 1997-11-04 | Laroche Industries Inc. | Process for preparing fluorinated aliphatic compounds |
US5689020A (en) * | 1996-03-11 | 1997-11-18 | Laroche Industries Inc. | High temperature chlorination process for the preparation of polychloroolefins |
US5789644A (en) * | 1994-06-29 | 1998-08-04 | Basf Aktiengesellschaft | Preparation of acetylene and synthesis gas |
US5811605A (en) * | 1997-02-19 | 1998-09-22 | Ppg Industries, Inc. | Preparation of 1,2,3,3-tetrachloropropene |
US5895825A (en) * | 1997-12-01 | 1999-04-20 | Elf Atochem North America, Inc. | Preparation of 1,1,1,3,3-pentafluoropropane |
US5986151A (en) * | 1997-02-05 | 1999-11-16 | Alliedsignal Inc. | Fluorinated propenes from pentafluoropropane |
US6111150A (en) * | 1996-06-20 | 2000-08-29 | Central Glass Company, Limited | Method for producing 1,1,1,3,3,-pentafluoropropane |
US6118018A (en) * | 1999-12-06 | 2000-09-12 | Occidental Chemical Corporation | Chlorination and bromination of aromatic compounds at atmospheric pressure |
US6160187A (en) * | 1997-12-18 | 2000-12-12 | The Dow Chemical Company | Method for making glycol in an adiabatic reactor system |
US6187976B1 (en) * | 1998-04-09 | 2001-02-13 | Alliedsignal Inc. | Process for the preparation of fluorine containing hydrohalocarbons |
US6229057B1 (en) * | 1993-07-26 | 2001-05-08 | Zeneca Limited | Chlorination process |
US20010018962A1 (en) * | 1998-12-23 | 2001-09-06 | American Air Liquide Inc. | Heat exchanger for preheating an oxidizing gas |
US20020110711A1 (en) * | 2000-11-04 | 2002-08-15 | Stefan Boneberg | Method and device for starting a reacator in a gas-generating system |
US6472573B1 (en) * | 1998-03-23 | 2002-10-29 | Daikin Industries, Ltd. | Process for producing 1,1,1,3,3-pentafluoropropane |
US6538167B1 (en) * | 1996-10-02 | 2003-03-25 | Exxonmobil Chemical Patents Inc. | Process for producing light olefins |
US6545176B1 (en) * | 1998-11-04 | 2003-04-08 | Rohm And Haas Company | Apparatus and process for the high yield production of methyl methacrylate or methacrylic acid |
US6551469B1 (en) * | 2001-11-27 | 2003-04-22 | Honeywell International | Photochlorination of 1,1,1,3,3-pentafluoropropane |
US6613127B1 (en) * | 2000-05-05 | 2003-09-02 | Dow Global Technologies Inc. | Quench apparatus and method for the reformation of organic materials |
US6683216B1 (en) * | 2002-11-06 | 2004-01-27 | Eastman Chemical Company | Continuous process for the preparation of amines |
US20040205996A1 (en) * | 2003-03-26 | 2004-10-21 | Bernd Bartenbach | Process for the scale-up of a reactor for carrying out a high-temperature reaction, reactor and use |
US6825383B1 (en) * | 2003-09-22 | 2004-11-30 | Council Of Scientific And Industrial Research | Catalytic process for regiospecific chlorination of alkanes, alkenes and arenes |
US6924403B2 (en) * | 2002-06-26 | 2005-08-02 | E. I. Du Pont De Nemours And Company | Synthesis of hexafluoropropylene |
US6958135B1 (en) * | 1999-06-15 | 2005-10-25 | Methanol Casale S.A. | Isothermal reactor for exothermic or endothermic heterogeneous reactions |
US20060150445A1 (en) * | 2003-01-24 | 2006-07-13 | Redding John H | Underwater sediment management |
US7117934B2 (en) * | 2002-03-15 | 2006-10-10 | H2Gen Innovations, Inc. | Method and apparatus for minimizing adverse effects of thermal expansion in a heat exchange reactor |
US20060258891A1 (en) * | 2005-05-12 | 2006-11-16 | Honeywell International Inc. | Method for producing fluorinated organic compounds |
US20060292046A1 (en) * | 2003-07-31 | 2006-12-28 | Dow Global Technologies Inc. | Oxidation process and reactor with modified feed system |
WO2007018298A1 (en) * | 2005-08-09 | 2007-02-15 | Canon Kabushiki Kaisha | Fluid-processing device and fluid-processing method |
US7189884B2 (en) * | 2004-04-29 | 2007-03-13 | Honeywell International | Processes for synthesis of tetrafluoropropene |
US20070112229A1 (en) * | 2004-04-29 | 2007-05-17 | Honeywell International Inc. | Method for producing fluorinated organic compounds |
US7226567B1 (en) * | 1999-03-16 | 2007-06-05 | Basf Aktiengesellschaft | Multi-tube fixed-bed reactor, especially for catalytic gas phase reactions |
US20070197841A1 (en) * | 2004-04-29 | 2007-08-23 | Honeywell International Inc. | Method for producing fluorinated organic compounds |
US20070197842A1 (en) * | 2004-04-29 | 2007-08-23 | Honeywell International Inc. | Method for producing fluorinated organic compounds |
US7282120B2 (en) * | 1999-06-16 | 2007-10-16 | Solvay Fluor Gmbh | UV-activated chlorination process |
US20070265368A1 (en) * | 2004-12-22 | 2007-11-15 | Velliyur Nott Mallikarjuna Rao | Functionalized Copolymers of Terminally Functionalized Perfluoro (Alkyl Vinyl Ether) Reactor Wall for Photochemical Reactions, Process for Increasing Fluorine Content in Hydrocaebons and Halohydrocarbons and Olefin Production |
US7297814B2 (en) * | 2002-01-11 | 2007-11-20 | Mitsubishi Chemical Corporation | Multitube reactor, vapor phase catalytic oxidation method using the multitube reactor, and start up method applied to the multitube reactor |
US20080021229A1 (en) * | 2004-05-21 | 2008-01-24 | Maughon Bob R | Process for Preparing Epichlorhydrin from Ethane |
US7345209B2 (en) * | 2004-04-29 | 2008-03-18 | Honeywell International Inc. | Processes for synthesis of 1,3,3,3-tetrafluoropropene |
US8614363B2 (en) * | 2007-12-19 | 2013-12-24 | Occidental Chemical Corporation | Methods of making chlorinated hydrocarbons |
Family Cites Families (32)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA990738A (en) * | 1971-07-30 | 1976-06-08 | Bruce E. Kurtz | Isothermal chlorination of methane, ethane and other compounds in a porous tube reactor |
US4100142A (en) * | 1972-09-13 | 1978-07-11 | Fiber Industries, Inc. | Polyester process and product |
JP2510932Y2 (ja) * | 1990-11-09 | 1996-09-18 | 川崎製鉄株式会社 | 微粉、超微粉製造装置 |
JP2584913B2 (ja) | 1991-07-15 | 1997-02-26 | 日本電信電話株式会社 | マルチビーム制御方式 |
JP2813100B2 (ja) * | 1992-10-23 | 1998-10-22 | 株式会社トクヤマ | アリルクロライドの製造方法および製造装置 |
JPH08119885A (ja) * | 1994-10-25 | 1996-05-14 | Central Glass Co Ltd | フッ素化炭化水素の製造方法 |
US5504266A (en) * | 1995-05-24 | 1996-04-02 | The Dow Chemical Company | Process to make allyl chloride and reactor useful in that process |
JP3769050B2 (ja) * | 1995-07-07 | 2006-04-19 | 三井化学株式会社 | フェノールの製造方法 |
DE19541266A1 (de) * | 1995-11-06 | 1997-05-07 | Bayer Ag | Verfahren und Vorrichtung zur Durchführung chemischer Reaktionen mittels eines Mikrostruktur-Lamellenmischers |
JPH09194404A (ja) * | 1996-01-17 | 1997-07-29 | Central Glass Co Ltd | 1−クロロ−3,3,3−トリフルオロプロペンの製造法 |
US6031141A (en) * | 1997-08-25 | 2000-02-29 | E. I. Du Pont De Nemours And Company | Fluoroolefin manufacturing process |
US6054057A (en) | 1997-09-26 | 2000-04-25 | General Atomics | Downflow hydrothermal treatment |
US6392079B1 (en) * | 1999-03-30 | 2002-05-21 | General Electric Company | Method and apparatus for preparing monofunctional aromatic chloroformates suitable for use as chainstopping agents |
AR027590A1 (es) * | 2000-03-02 | 2003-04-02 | Dow Chemical Co | Reactor tubular, proceso para conducir las reacciones multifase de liquido/liquido en un reactor tubular, y un proceso para compuestos aromaticos denitracion de anillo en un reactor tubular |
JP4857459B2 (ja) * | 2000-03-06 | 2012-01-18 | 栗田工業株式会社 | 水熱反応方法および装置 |
GB0023781D0 (en) * | 2000-09-28 | 2000-11-08 | Kvaerner Process Tech Ltd | Process |
DE10158160A1 (de) * | 2001-11-28 | 2003-06-12 | Basf Ag | Herstellung von Isocyanaten in der Gasphase |
EP1740521B1 (en) * | 2004-04-29 | 2015-05-20 | Honeywell International Inc. | Processes for synthesis of 1,3,3,3-tetrafluoropropene |
JP4501158B2 (ja) * | 2005-03-30 | 2010-07-14 | 富士フイルム株式会社 | マイクロ化学装置の運転方法 |
JP4724619B2 (ja) * | 2005-08-09 | 2011-07-13 | キヤノン株式会社 | 流体処理装置及び流体処理方法 |
CN101415664B (zh) * | 2006-03-31 | 2012-05-30 | 纳幕尔杜邦公司 | 氢氟烯烃的同时制备 |
CN103483141B (zh) | 2006-10-31 | 2015-09-16 | 纳幕尔杜邦公司 | 氟丙烷、卤代丙烯以及2-氯-3,3,3-三氟-1-丙烯与hf的共沸组合物和1,1,1,2,2-五氟丙烷与hf的共沸组合物的制备方法 |
CN101652403B (zh) * | 2007-04-10 | 2012-11-21 | 旭硝子株式会社 | 具有有机配体的复合金属氰化物配位催化剂、其制造方法及聚醚多元醇的制造方法 |
JP2009000592A (ja) * | 2007-06-19 | 2009-01-08 | Hitachi Ltd | 反応器および反応システム |
US8076521B2 (en) | 2007-06-27 | 2011-12-13 | Arkema Inc. | Process for the manufacture of hydrofluoroolefins |
US7795480B2 (en) | 2007-07-25 | 2010-09-14 | Honeywell International Inc. | Method for producing 2-chloro-3,3,3,-trifluoropropene (HCFC-1233xf) |
US9079818B2 (en) | 2007-10-15 | 2015-07-14 | Honeywell International Inc. | Process for synthesis of fluorinated olefins |
US20090163694A1 (en) * | 2007-12-21 | 2009-06-25 | Michael Gann | Process for the continuous production of high efficient aqueous amino formaldehyde resin solutions |
US8071826B2 (en) * | 2008-04-04 | 2011-12-06 | Honeywell International Inc. | Process for the preparation of 2,3,3,3-tetrafluoropropene (HFO-1234yf) |
JP5604038B2 (ja) * | 2008-08-25 | 2014-10-08 | 株式会社日立製作所 | 反応装置及び反応プラント |
EP2349961B1 (en) * | 2008-10-13 | 2016-11-23 | Blue Cube IP LLC | Process for the production of chlorinated and/or fluorinated propenes |
WO2011044514A2 (en) * | 2009-10-09 | 2011-04-14 | Dow Global Technologies, Inc | Isothermal multitube reactors and processes incorporating the same |
-
2010
- 2010-10-08 KR KR1020127008934A patent/KR20120093202A/ko not_active Application Discontinuation
- 2010-10-08 BR BR112012007913A patent/BR112012007913A2/pt not_active IP Right Cessation
- 2010-10-08 CN CN201080044964.6A patent/CN102665890B/zh not_active Expired - Fee Related
- 2010-10-08 EP EP10768142A patent/EP2485833A2/en not_active Withdrawn
- 2010-10-08 JP JP2012533366A patent/JP5947214B2/ja not_active Expired - Fee Related
- 2010-10-08 US US12/901,383 patent/US20110087056A1/en not_active Abandoned
- 2010-10-08 WO PCT/US2010/052090 patent/WO2011044522A2/en active Application Filing
- 2010-10-08 CN CN201610086260.4A patent/CN105664811B/zh not_active Expired - Fee Related
-
2015
- 2015-12-01 JP JP2015234573A patent/JP6382786B2/ja not_active Expired - Fee Related
-
2016
- 2016-07-07 US US15/204,462 patent/US10189756B2/en not_active Expired - Fee Related
Patent Citations (102)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2630461A (en) * | 1953-03-03 | Production of acetylene by incom | ||
US2119484A (en) * | 1935-05-06 | 1938-05-31 | Du Pont | Chlorination of propylene dichloride |
US2179378A (en) * | 1936-07-18 | 1939-11-07 | Air Reduction | Production of acetylene |
US2207193A (en) * | 1937-09-14 | 1940-07-09 | Shell Dev | Production of allyl type halides |
US2299441A (en) * | 1939-09-02 | 1942-10-20 | Shell Dev | Catalytic halo-substitution of saturated organic compounds |
US2302228A (en) * | 1940-04-02 | 1942-11-17 | Du Pont | Method of chlorination with sulphuryl chloride and production of monochloro-trimethyl acetic acid |
US2370342A (en) * | 1940-04-30 | 1945-02-27 | Tide Water Associated Oil Comp | Halogenation |
US2378859A (en) * | 1941-08-08 | 1945-06-19 | Distillers Co Yeast Ltd | Splitting-off of hydrogen halide from halogenated hydrocarbons |
US2449286A (en) * | 1945-07-16 | 1948-09-14 | Shell Dev | Production of 1, 3-dihalopropylenes |
US2435983A (en) * | 1945-12-01 | 1948-02-17 | Universal Oil Prod Co | Production of liquid hydrocarbons |
US2588867A (en) * | 1948-10-25 | 1952-03-11 | Dow Chemical Co | Pyrolytic production of chlorohydrocarbons |
US2688592A (en) * | 1950-10-21 | 1954-09-07 | Diamond Alkali Co | Photochemical process for preparing carbon tetrachloride |
US2762611A (en) * | 1952-02-28 | 1956-09-11 | Pfaudler Co Inc | Tubular heat exchangers |
US2765359A (en) * | 1953-02-10 | 1956-10-02 | Hydrocarbon Research Inc | Production of acetylene |
US3000980A (en) * | 1958-04-07 | 1961-09-19 | Dow Chemical Co | Preparation of alkyl bromides |
US2973393A (en) * | 1958-10-02 | 1961-02-28 | Dow Chemical Co | Chlorination of acetylenes |
US2964579A (en) * | 1958-10-09 | 1960-12-13 | Houdry Process Corp | Selective hydrogenation of diolefins with copper chromite catalyst |
US3094567A (en) * | 1960-02-25 | 1963-06-18 | Monsanto Chemicals | Chlorination of propynes |
US3112988A (en) * | 1960-02-26 | 1963-12-03 | Sheil Oil Company | Mixing gases at supersonic velocity |
US3819731A (en) * | 1960-03-23 | 1974-06-25 | Stauffer Chemical Co | Production of chlorinated unsaturated hydrocarbons |
US3651019A (en) * | 1961-09-28 | 1972-03-21 | Yeda Res & Dev | Production of adducts of carbon tetrachloride or chloroform with olefinically unsaturated substances |
US3446859A (en) * | 1962-06-11 | 1969-05-27 | Hooker Chemical Corp | Vapor phase condensation process |
US3502734A (en) * | 1966-05-11 | 1970-03-24 | Du Pont | Process for partially chlorinating methyl chloride and/or methylene chloride |
US3444263A (en) * | 1966-11-09 | 1969-05-13 | Gulf Research Development Co | Method for converting ethylene to alpha olefins in the presence of an organic sulfide |
US3525595A (en) * | 1967-05-19 | 1970-08-25 | Bayer Ag | Concentric cross flow nozzle apparatus for carrying out reactions between gases |
US3558438A (en) * | 1968-10-30 | 1971-01-26 | Du Pont | Distillation process and apparatus |
US3551512A (en) * | 1968-11-01 | 1970-12-29 | Diamond Shamrock Corp | Pressure process for preparing acetylene |
US3676508A (en) * | 1969-01-30 | 1972-07-11 | Hornig Anneliese | Process for the manufacture of carbon tetrachloride |
US4513154A (en) * | 1971-07-30 | 1985-04-23 | Allied Corporation | Process for consecutive competitive gas phase reaction |
US3823195A (en) * | 1971-12-27 | 1974-07-09 | Monsanto Co | Preparation of 1,1,2,3-tetrachloropropene from 1,2,3-trichloropropane |
US3926758A (en) * | 1971-12-27 | 1975-12-16 | Monsanto Co | Preparation of 1,1,2,3-tetrachloropropene from 2,3-trichloropropane |
US3954410A (en) * | 1972-11-21 | 1976-05-04 | Merck Patent Gesellschaft Mit Beschraenkter Haftung | Solvents for NMR spectroscopy |
US3948858A (en) * | 1973-09-22 | 1976-04-06 | Akzo N.V. | Polymerization of ethylenically unsaturated compounds |
US3872664A (en) * | 1973-10-15 | 1975-03-25 | United Aircraft Corp | Swirl combustor with vortex burning and mixing |
US3914167A (en) * | 1974-08-26 | 1975-10-21 | Dow Chemical Co | Process for making cis-1,3-dichloropropene |
US4051182A (en) * | 1976-04-12 | 1977-09-27 | Stauffer Chemical Company | Process for the manufacture of α-chloropropionyl chloride |
US4038372A (en) * | 1976-05-05 | 1977-07-26 | The United States Of America As Represented By The Secretary Of The Navy | Process for manufacturing chloramine |
US4319062A (en) * | 1976-08-02 | 1982-03-09 | The Dow Chemical Company | Allyl chloride process |
US4535194A (en) * | 1983-07-06 | 1985-08-13 | Monsanto Co. | Process for producing 1,1,2,3-tetrachloropropene |
US4650914A (en) * | 1983-07-06 | 1987-03-17 | Monsanto Company | Process for producing 1,1,2,3-tetrachloropropene |
US4716255A (en) * | 1983-08-25 | 1987-12-29 | Huels Aktiengesellschaft | Process for the production of 3,3-dichloro-2-methylpropene |
US4902393A (en) * | 1983-08-25 | 1990-02-20 | Huels Aktiengesellschaft | Process for the production of 1,1,2-trichloro-2-methylpropane |
US4702809A (en) * | 1984-04-25 | 1987-10-27 | Huels Aktiengesellschaft | Process for the production of 1,2,3-trichloro-2-methylpropane |
US4661648A (en) * | 1984-08-20 | 1987-04-28 | Solvay & Cie (Societe Anonyme) | Process for carrying out substitution chlorination reactions of organic compounds by means of molecular chlorine in the presence of a chlorinated product serving as a radical initiator, and radical initiators used in such a process |
US4714792A (en) * | 1984-09-06 | 1987-12-22 | Huels Aktiengesellschaft | Process for the production of 1,2,3-trichloropropane |
US4614572A (en) * | 1985-07-08 | 1986-09-30 | The Dow Chemical Company | Liquid phase chlorination of chlorinated methanes |
US4726686A (en) * | 1985-07-30 | 1988-02-23 | Hartmut Wolf | Swirl chamber |
US4644907A (en) * | 1985-11-29 | 1987-02-24 | Hunter Edward H | Boiler tubes of enhanced efficiency and method of producing same |
US4727181A (en) * | 1986-04-21 | 1988-02-23 | The Dow Chemical Company | Process for the preparation of α-halocinnamate esters |
US4849554A (en) * | 1987-04-10 | 1989-07-18 | Imperial Chemical Industries Plc | Production of tetrafluoroethylene and hexafluoropropylene |
US4894205A (en) * | 1987-09-18 | 1990-01-16 | Shell Oil Company | Multitube reactor |
US5132473A (en) * | 1988-05-17 | 1992-07-21 | Daikin Industries, Ltd. | Process for production of 1,1,1-trifluoro-2,2-dichloroethane |
US5171899A (en) * | 1988-05-17 | 1992-12-15 | Daikin Industries Ltd. | Process for production of 1,1,1-trifluoro-2,2-dichloroethane |
US5315044A (en) * | 1988-05-17 | 1994-05-24 | Daikin Industries Ltd. | Process for production of 1,1,1-trifluoro-2,2-dichloroethane |
US4999102A (en) * | 1988-12-16 | 1991-03-12 | The Amalgamated Sugar Company | Liquid transfer manifold system for maintaining plug flow |
US5254771A (en) * | 1989-07-14 | 1993-10-19 | Hoechst Aktiengesellschaft | Process for the preparation of 1,1,1-trifluoro-2-2-dichloroethane under elevated pressure |
US5057634A (en) * | 1989-12-19 | 1991-10-15 | E. I. Du Pont De Nemours And Company | Multistep synthesis of hexafluoropropylene |
US5178844A (en) * | 1990-04-03 | 1993-01-12 | Phillips Petroleum Company | Method and apparatus for producing nitride products |
US5254772A (en) * | 1991-03-12 | 1993-10-19 | Imperial Chemical Industries Plc | Chemical process |
US5254788A (en) * | 1991-09-10 | 1993-10-19 | Stone And Webster Engineering Corporation | Process for the production of olefins from light paraffins |
US5262575A (en) * | 1992-08-04 | 1993-11-16 | The Dow Chemical Company | Production of allylic chlorides |
US6229057B1 (en) * | 1993-07-26 | 2001-05-08 | Zeneca Limited | Chlorination process |
US5414166A (en) * | 1993-11-29 | 1995-05-09 | Korea Institute Of Science And Technology | Process for the preparation of 1,1,1-trifluoro-2,2-dichloroethane |
US5789644A (en) * | 1994-06-29 | 1998-08-04 | Basf Aktiengesellschaft | Preparation of acetylene and synthesis gas |
US5684219A (en) * | 1995-08-28 | 1997-11-04 | Laroche Industries Inc. | Process for preparing fluorinated aliphatic compounds |
US5689020A (en) * | 1996-03-11 | 1997-11-18 | Laroche Industries Inc. | High temperature chlorination process for the preparation of polychloroolefins |
US6111150A (en) * | 1996-06-20 | 2000-08-29 | Central Glass Company, Limited | Method for producing 1,1,1,3,3,-pentafluoropropane |
US6538167B1 (en) * | 1996-10-02 | 2003-03-25 | Exxonmobil Chemical Patents Inc. | Process for producing light olefins |
US5986151A (en) * | 1997-02-05 | 1999-11-16 | Alliedsignal Inc. | Fluorinated propenes from pentafluoropropane |
US5811605A (en) * | 1997-02-19 | 1998-09-22 | Ppg Industries, Inc. | Preparation of 1,2,3,3-tetrachloropropene |
US5895825A (en) * | 1997-12-01 | 1999-04-20 | Elf Atochem North America, Inc. | Preparation of 1,1,1,3,3-pentafluoropropane |
US6160187A (en) * | 1997-12-18 | 2000-12-12 | The Dow Chemical Company | Method for making glycol in an adiabatic reactor system |
US6472573B1 (en) * | 1998-03-23 | 2002-10-29 | Daikin Industries, Ltd. | Process for producing 1,1,1,3,3-pentafluoropropane |
US6187976B1 (en) * | 1998-04-09 | 2001-02-13 | Alliedsignal Inc. | Process for the preparation of fluorine containing hydrohalocarbons |
US6545176B1 (en) * | 1998-11-04 | 2003-04-08 | Rohm And Haas Company | Apparatus and process for the high yield production of methyl methacrylate or methacrylic acid |
US6610177B2 (en) * | 1998-11-04 | 2003-08-26 | Rohm And Haas Company | Apparatus and process for the high yield production of methyl methacrylate or methacrylic acid |
US20010018962A1 (en) * | 1998-12-23 | 2001-09-06 | American Air Liquide Inc. | Heat exchanger for preheating an oxidizing gas |
US7226567B1 (en) * | 1999-03-16 | 2007-06-05 | Basf Aktiengesellschaft | Multi-tube fixed-bed reactor, especially for catalytic gas phase reactions |
US6958135B1 (en) * | 1999-06-15 | 2005-10-25 | Methanol Casale S.A. | Isothermal reactor for exothermic or endothermic heterogeneous reactions |
US7282120B2 (en) * | 1999-06-16 | 2007-10-16 | Solvay Fluor Gmbh | UV-activated chlorination process |
US6118018A (en) * | 1999-12-06 | 2000-09-12 | Occidental Chemical Corporation | Chlorination and bromination of aromatic compounds at atmospheric pressure |
US6613127B1 (en) * | 2000-05-05 | 2003-09-02 | Dow Global Technologies Inc. | Quench apparatus and method for the reformation of organic materials |
US20020110711A1 (en) * | 2000-11-04 | 2002-08-15 | Stefan Boneberg | Method and device for starting a reacator in a gas-generating system |
US6551469B1 (en) * | 2001-11-27 | 2003-04-22 | Honeywell International | Photochlorination of 1,1,1,3,3-pentafluoropropane |
US7297814B2 (en) * | 2002-01-11 | 2007-11-20 | Mitsubishi Chemical Corporation | Multitube reactor, vapor phase catalytic oxidation method using the multitube reactor, and start up method applied to the multitube reactor |
US7117934B2 (en) * | 2002-03-15 | 2006-10-10 | H2Gen Innovations, Inc. | Method and apparatus for minimizing adverse effects of thermal expansion in a heat exchange reactor |
US6924403B2 (en) * | 2002-06-26 | 2005-08-02 | E. I. Du Pont De Nemours And Company | Synthesis of hexafluoropropylene |
US6683216B1 (en) * | 2002-11-06 | 2004-01-27 | Eastman Chemical Company | Continuous process for the preparation of amines |
US20060150445A1 (en) * | 2003-01-24 | 2006-07-13 | Redding John H | Underwater sediment management |
US20040205996A1 (en) * | 2003-03-26 | 2004-10-21 | Bernd Bartenbach | Process for the scale-up of a reactor for carrying out a high-temperature reaction, reactor and use |
US20060292046A1 (en) * | 2003-07-31 | 2006-12-28 | Dow Global Technologies Inc. | Oxidation process and reactor with modified feed system |
US6825383B1 (en) * | 2003-09-22 | 2004-11-30 | Council Of Scientific And Industrial Research | Catalytic process for regiospecific chlorination of alkanes, alkenes and arenes |
US20070197841A1 (en) * | 2004-04-29 | 2007-08-23 | Honeywell International Inc. | Method for producing fluorinated organic compounds |
US20070112229A1 (en) * | 2004-04-29 | 2007-05-17 | Honeywell International Inc. | Method for producing fluorinated organic compounds |
US7189884B2 (en) * | 2004-04-29 | 2007-03-13 | Honeywell International | Processes for synthesis of tetrafluoropropene |
US20070197842A1 (en) * | 2004-04-29 | 2007-08-23 | Honeywell International Inc. | Method for producing fluorinated organic compounds |
US7345209B2 (en) * | 2004-04-29 | 2008-03-18 | Honeywell International Inc. | Processes for synthesis of 1,3,3,3-tetrafluoropropene |
US20080021229A1 (en) * | 2004-05-21 | 2008-01-24 | Maughon Bob R | Process for Preparing Epichlorhydrin from Ethane |
US20070265368A1 (en) * | 2004-12-22 | 2007-11-15 | Velliyur Nott Mallikarjuna Rao | Functionalized Copolymers of Terminally Functionalized Perfluoro (Alkyl Vinyl Ether) Reactor Wall for Photochemical Reactions, Process for Increasing Fluorine Content in Hydrocaebons and Halohydrocarbons and Olefin Production |
US20060258891A1 (en) * | 2005-05-12 | 2006-11-16 | Honeywell International Inc. | Method for producing fluorinated organic compounds |
WO2007018298A1 (en) * | 2005-08-09 | 2007-02-15 | Canon Kabushiki Kaisha | Fluid-processing device and fluid-processing method |
US8614363B2 (en) * | 2007-12-19 | 2013-12-24 | Occidental Chemical Corporation | Methods of making chlorinated hydrocarbons |
Cited By (39)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9464258B2 (en) | 2009-10-12 | 2016-10-11 | Elevance Renewable Sciences, Inc. | Diene-selective hydrogenation of metathesis derived olefins and unsaturated esters |
US9469827B2 (en) | 2009-10-12 | 2016-10-18 | Elevance Renewable Sciences, Inc. | Methods of refining natural oil feedstocks |
US9732282B2 (en) | 2009-10-12 | 2017-08-15 | Elevance Renewable Sciences, Inc. | Methods of refining natural oil feedstocks |
US10689582B2 (en) | 2009-10-12 | 2020-06-23 | Elevance Renewable Sciences, Inc. | Methods of refining natural oil feedstocks |
US8957268B2 (en) | 2009-10-12 | 2015-02-17 | Elevance Renewable Sciences, Inc. | Methods of refining natural oil feedstocks |
US9051519B2 (en) | 2009-10-12 | 2015-06-09 | Elevance Renewable Sciences, Inc. | Diene-selective hydrogenation of metathesis derived olefins and unsaturated esters |
US9382502B2 (en) | 2009-10-12 | 2016-07-05 | Elevance Renewable Sciences, Inc. | Methods of refining and producing isomerized fatty acid esters and fatty acids from natural oil feedstocks |
US9365487B2 (en) | 2009-10-12 | 2016-06-14 | Elevance Renewable Sciences, Inc. | Methods of refining and producing dibasic esters and acids from natural oil feedstocks |
US9233896B2 (en) | 2011-08-07 | 2016-01-12 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9475739B2 (en) | 2011-08-07 | 2016-10-25 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9359273B2 (en) | 2011-10-14 | 2016-06-07 | Honeywell International Inc. | Process for producing 2,3,3,3-tetrafluoropropene |
US9199899B2 (en) | 2011-12-02 | 2015-12-01 | Blue Cube Ip Llc | Process for the production of chlorinated alkanes |
US9512049B2 (en) | 2011-12-23 | 2016-12-06 | Dow Global Technologies Llc | Process for the production of alkenes and/or aromatic compounds |
US9321707B2 (en) | 2012-09-20 | 2016-04-26 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9598334B2 (en) | 2012-09-20 | 2017-03-21 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9795941B2 (en) | 2012-09-30 | 2017-10-24 | Blue Cube Ip Llc | Weir quench and processes incorporating the same |
US10065157B2 (en) | 2012-10-26 | 2018-09-04 | Blue Cube Ip Llc | Mixer and processes incorporating the same |
US9512053B2 (en) | 2012-12-18 | 2016-12-06 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9475740B2 (en) | 2012-12-19 | 2016-10-25 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
KR102116746B1 (ko) * | 2012-12-28 | 2020-06-01 | 가부시키가이샤 호리바 에스텍 | 유체혼합소자 |
US20140182726A1 (en) * | 2012-12-28 | 2014-07-03 | Horiba Stec, Co., Ltd. | Fluid mixing element |
US9795936B2 (en) * | 2012-12-28 | 2017-10-24 | Horiba Stec, Co., Ltd. | Fluid mixing element |
JP2014128755A (ja) * | 2012-12-28 | 2014-07-10 | Horiba Ltd | 流体混合素子 |
KR20140086858A (ko) * | 2012-12-28 | 2014-07-08 | 가부시키가이샤 호리바 에스텍 | 유체혼합소자 |
US9688592B2 (en) | 2013-01-22 | 2017-06-27 | Axiall Ohio, Inc. | Processes for producing chlorinated hydrocarbons and methods for recovering polyvalent antimony catalysts therefrom |
USRE47429E1 (en) | 2013-01-22 | 2019-06-11 | Eagle Us 2 Llc | Process for producing chlorinated hydrocarbons |
US8889930B2 (en) | 2013-01-22 | 2014-11-18 | Axiall Ohio, Inc. | Process for producing chlorinated hydrocarbons |
US10112880B2 (en) | 2013-01-22 | 2018-10-30 | Eagle Us 2 Llc | Processes for producing chlorinated hydrocarbons and methods for recovering polyvalent antimony catalysts therefrom |
US9255048B2 (en) | 2013-01-22 | 2016-02-09 | Axiall Ohio, Inc. | Process for producing chlorinated hydrocarbons |
US9289758B2 (en) | 2013-01-22 | 2016-03-22 | Axiall Ohio, Inc. | Processes for producing chlorinated hydrocarbons and methods for recovering polyvalent antimony catalysts therefrom |
US9382176B2 (en) | 2013-02-27 | 2016-07-05 | Blue Cube Ip Llc | Process for the production of chlorinated propenes |
US9403741B2 (en) | 2013-03-09 | 2016-08-02 | Blue Cube Ip Llc | Process for the production of chlorinated alkanes |
US9353029B2 (en) | 2013-03-14 | 2016-05-31 | Honeywell International, Inc. | Fluorination process and reactor |
US9676687B2 (en) | 2013-03-14 | 2017-06-13 | Honeywell International. Inc. | Fluorination process and reactor |
US9139497B2 (en) | 2013-10-23 | 2015-09-22 | Axiall Ohio, Inc. | Process for producing chlorinated hydrocarbons in the presence of a polyvalent bismuth compound |
US10076739B1 (en) * | 2014-07-22 | 2018-09-18 | Precision Combustion, Inc. | Chemical reactor for use with overly reactive chemicals |
US10525434B1 (en) | 2014-07-22 | 2020-01-07 | Precision Combustion, Inc. | Chemical reactor for use with overly reactive chemicals |
JP2016135490A (ja) * | 2016-05-02 | 2016-07-28 | 株式会社堀場エステック | 流体混合素子 |
CN115106019A (zh) * | 2022-06-23 | 2022-09-27 | 天津大学 | 平推流反应器和平推流反应器实验*** |
Also Published As
Publication number | Publication date |
---|---|
BR112012007913A2 (pt) | 2019-09-24 |
CN105664811A (zh) | 2016-06-15 |
EP2485833A2 (en) | 2012-08-15 |
WO2011044522A3 (en) | 2011-07-14 |
CN102665890A (zh) | 2012-09-12 |
JP2013507241A (ja) | 2013-03-04 |
JP5947214B2 (ja) | 2016-07-06 |
CN102665890B (zh) | 2016-02-24 |
US10189756B2 (en) | 2019-01-29 |
JP2016034644A (ja) | 2016-03-17 |
WO2011044522A2 (en) | 2011-04-14 |
US20160347692A1 (en) | 2016-12-01 |
CN105664811B (zh) | 2018-10-09 |
KR20120093202A (ko) | 2012-08-22 |
JP6382786B2 (ja) | 2018-08-29 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US10189756B2 (en) | Adiabatic plug flow reactors and processes incorporating the same | |
US8926918B2 (en) | Isothermal multitube reactors | |
RU2162459C2 (ru) | Способ получения аллилгалогенида и реактор для его осуществления | |
US9758451B2 (en) | Process for the preparation of fluorinated compounds | |
US9795941B2 (en) | Weir quench and processes incorporating the same | |
US11465956B2 (en) | Process for producing C3 chlorinated alkane and alkene compounds | |
JP2004250453A (ja) | ジイソシアネートの製造方法 | |
CN107667085B (zh) | 用于合成1,2,3,4-四氯-六氟-丁烷的方法 | |
CN102686544A (zh) | 用于生产氯化和/或氟化丙烯和高级烯烃的方法 | |
JP2013507393A5 (zh) | ||
JP2014114214A (ja) | 2,3,3,3−テトラフルオロプロペンの製造方法 | |
KR101613808B1 (ko) | 2-클로로-3,3,3-트리플루오로프로펜의 제조방법 | |
JP2014129260A (ja) | 2,3,3,3−テトラフルオロプロペンの製造方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: THE DOW CHEMICAL COMPANY, MICHIGAN Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:DOW DEUTSCHLAND GMBH & CO. OHG;REEL/FRAME:035733/0932 Effective date: 20100618 Owner name: DOW DEUTSCHLAND GMBH & CO. OHG, GERMANY Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:EIFFLER, JUERGEN;GROENEWALD, HEINZ;KOKOTT, MANFRED;AND OTHERS;SIGNING DATES FROM 20100205 TO 20100224;REEL/FRAME:035733/0569 Owner name: DOW GLOBAL TECHNOLOGIES INC., MICHIGAN Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:TIRTOWIDJOJO, MAX M.;BAI, HUA;CHAKRABORTY, DEBASHIS;AND OTHERS;SIGNING DATES FROM 20100208 TO 20100305;REEL/FRAME:035733/0798 Owner name: DOW GLOBAL TECHNOLOGIES INC., MICHIGAN Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:THE DOW CHEMICAL COMPANY;REEL/FRAME:035734/0066 Effective date: 20100618 Owner name: DOW GLOBAL TECHNOLOGIES LLC, MICHIGAN Free format text: CHANGE OF NAME;ASSIGNOR:DOW GLOBAL TECHNOLOGIES INC.;REEL/FRAME:035785/0199 Effective date: 20101231 |
|
AS | Assignment |
Owner name: BLUE CUBE IP LLC, MICHIGAN Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:DOW GLOBAL TECHNOLOGIES LLC;REEL/FRAME:035887/0193 Effective date: 20150610 |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |