WO2005016509A1 - Procede d'oxydation et reacteur comprenant un systeme d'alimentation modifie - Google Patents

Procede d'oxydation et reacteur comprenant un systeme d'alimentation modifie Download PDF

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Publication number
WO2005016509A1
WO2005016509A1 PCT/US2003/023933 US0323933W WO2005016509A1 WO 2005016509 A1 WO2005016509 A1 WO 2005016509A1 US 0323933 W US0323933 W US 0323933W WO 2005016509 A1 WO2005016509 A1 WO 2005016509A1
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WO
WIPO (PCT)
Prior art keywords
reactor
feed
short bed
gas mixture
plenum
Prior art date
Application number
PCT/US2003/023933
Other languages
English (en)
Inventor
Olan Stanley Fruchey
Brian Robert Keyes
Carl David Murphy
Original Assignee
Dow Global Technologies Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Dow Global Technologies Inc. filed Critical Dow Global Technologies Inc.
Priority to JP2005507860A priority Critical patent/JP2007521126A/ja
Priority to US10/565,923 priority patent/US20060292046A1/en
Priority to MXPA06001255A priority patent/MXPA06001255A/es
Priority to PCT/US2003/023933 priority patent/WO2005016509A1/fr
Priority to EP03818197A priority patent/EP1660225A1/fr
Priority to CN03826973.2A priority patent/CN1819869A/zh
Priority to BRPI0318401-3A priority patent/BR0318401A/pt
Publication of WO2005016509A1 publication Critical patent/WO2005016509A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/215—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • B01J8/0085—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction promoting uninterrupted fluid flow, e.g. by filtering out particles in front of the catalyst layer
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0476—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds
    • B01J8/048—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds the beds being superimposed one above the other
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/25—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
    • C07C51/252—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring of propene, butenes, acrolein or methacrolein
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00212—Plates; Jackets; Cylinders
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00522—Controlling the temperature using inert heat absorbing solids outside the bed
    • 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
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/304—Composition or microstructure of the elements
    • B01J2219/30416—Ceramic

Definitions

  • TECHNICAL FIELD This invention relates to improvements for processes using shell and tube reactors. More specifically, the invention relates to using a short bed of packing material to direct leakage of contaminants such as heat exchange media or derivatives thereof away from the headspace of a tubular reactor and prevent formation of combustible gas mixtures.
  • BACKGROUND Tubular reactors are often times used for exothermic reactions, for example, the oxidation of propylene to acrylic acid and the manufacture of maleic anhydride.
  • production of acrylic acid is a two-stage gaseous catalytic oxidation of propylene.
  • the method employs a first stage reactor with a first stage catalyst for oxidation of propylene to acrolein and a second stage reactor charged with a second stage catalyst suitable for oxidation of acrolein to acrylic acid.
  • admixed feed reactants for example, propylene, air and steam used to produce acrylic acid are not expected to ignite at temperatures lower than about 450°C.
  • 5,080,872 discloses a method of regulating temperature inside a reaction vessel using a bed of solid particles having varied temperature zones through which a reactant fluid phase is passed.
  • United States Patent No. 6,028,220 discloses to the oxidation of propylene during which there is a reduction of hot spots in the catalyst layer by varying the catalyst activity; whereas, United States Patent No. 6,563,000 describes a process of producing acrylic acid from acrolein that includes multiple reaction zones wherein each such reaction zone comprises a catalyst of a different activity level, as compared to an adjacent zone, as is well known. Controlling temperature by circulating particulate matter, in general, has been disclosed, see, for example, United States Patent No.
  • United States Patent No. 4,672,918 discloses circulating temperature controlled solids to control the temperature of a fluidized bed.
  • United States Patent No. 4,899,695 discloses a process for controlling heat transfer and erosion in a fluidized bed combustion reactor by introducing particles into the combustion unit along with or in the presence of combustion reactants whereby some of the particles may be recycled.
  • United States Patent No. 5,505,907 describing a method for controlling the temperature of an incoming gas stream by incorporating coated solid particles into the gas stream, circulating and separating such particles and thereafter recycling same for repeat use.
  • 4,029,636 which discloses a method for removing molybdenum trioxide from reactor effluent gases issuing from reactors containing molybdenum-based catalysts by causing the effluent gases to pass over a bed of cooled solids located at the exit end of the tubular reactor on which the molybdenum trioxide is deposited.
  • United States Patent No. 5,413,699 discloses removal of NO x by forcing NO x containing gas through a DeNO catalyst bed.
  • 5,538,544 discloses a pressure swing adsorption system whereby a gas is introduced into the vessel head of such a pressure swing system and caused to distribute uniformly on an adsorbent bed as a result of passing through a graded ball bed support system.
  • the methods described above for controlling contamination require somewhat specialized environments and/or construction and use, and accordingly, they are simply not practical for retrofitting existing equipment to limit contamination in the event of a reactor breach, for example, where heat exchange fluid may leak and form derivatives and mix with the reactor feed.
  • the invention is based, in part, on the discovery that a short bed of packing material in the vicinity of the inlets of reactor tubes of a shell and tube reactor can restrict migration of decomposition gases (i.e., NOx) from heat exchange media into the reactor headspace. It has been found that such a bed placement virtually eliminates auto-ignition problems stemming from heat-exchange media leaks. It has been found that a short bed suffices to ameliorate contaminant problems without the need for a deeper bed and its associated pressure drop and material expense.
  • decomposition gases i.e., NOx
  • the invention relates to an improved process for high temperature oxidation of a gaseous reactant in a shell and tube reactor of the class with a plurality of reactor tubes wherein the reactor tubes are immersed in a heat exchange medium contained within the shell and the interior volume of the reactor tubes is thereby isolated from the heat exchange medium.
  • the reactor tube interior inlets are in communication with a feed plenum or headspace having a characteristic cross-sectional area in the vicinity of the reactor tube inlets generally free from obstruction, such that the velocity of a feed gas mixture to the reactor tube inlets is the volume rate of flow of the feed gas mixture divided by the characteristic cross-sectional area of the plenum in the vicinity of the reactor tube inlets.
  • the process is also of the class wherein the feed gas mixture is fed from the plenum to the reactor tubes.
  • the improvement of the present invention includes disposing a short bed of packing material adjacent to the reactor tube inlets.
  • the short bed can include a voidage of from about 0.3 to about 0.75 to increase the velocity of the feed gas mixture in the vicinity of the reactor tube inlets whereby contamination of the feed plenum by the decomposition gases of the heat exchange medium is controlled in the event of a reactor breach in the vicinity of the reactor tube inlets, as might occur when heat exchange medium leaks between the tubes and end plate due to corrosion.
  • the short bed occupies less than 20 percent of the headspace volume and preferably less than about 10 percent of the headspace volume.
  • the packing material comprises spherical macroparticles having diameters from about 0.125 to about 4 inches. Most preferred are ceramic macroparticles having a diameter of less than about 2 inches.
  • Alternate packing material shapes may be selected from pellets, disks, rods and plates of various shapes. DENSTONE® balls, available from Norton (Akron, OH, USA) are particularly preferred.
  • the inventive process and apparatus may be used in connection with the manufacture of methacrylic acid, maleic anhydride, acrylic acid and potentially other partial oxidations as may occur in the manufacture of ethylene oxide or vinyl acetate monomer, for example.
  • an improvement to a shell and tube reactor having tubes immersed in a heat-exchange medium at a temperature of 200-400°C which includes adding a short bed of packing material about the reactor tube inlets as described below.
  • the short bed has a depth of from about 10 to about 25 inches, while the reactor tubes have an inside diameter of about 0.75 to about 2 inches in preferred embodiments.
  • the improved reactor is suitably employed in the manufacture of acrylic acid as described below. Controlling contaminants, for example, oxidizers such as nitrogen oxides, can control flammability and undesired spontaneous auto-ignition. Adequate flow velocity prevents temperature excursions when the feed gas mixture and contaminants combine to form a mixture of increased flammability.
  • the bed placement could prevent undesirable migration of contaminants to the headspace whether or not contaminants increase flammability.
  • a contaminant could be a catalyst poison, thus, the contaminant needs to be restricted to localized regions of the reactor rather than be ubiquitous in the headspace so that it is fed to all of the tubes.
  • FIGURE 1 is a schematic diagram illustrating the process and apparatus of the present invention.
  • FIGURE 2 is a graph illustrating the spontaneous ignition of feed gas stream in the presence of 0.2% NO.
  • Like reference symbols in the various drawings indicate like elements.
  • Nitrogen oxides can include nitric oxide (NO), nitrous oxide (N 2 O), and nitrogen dioxide (NO ) among others. Presence of nitrogen oxides in low levels, for example, 10 to 9000 ppm can act as an oxidizer and lower ignition temperature of the feed gas mixture as may occur when the heat exchange medium leaks into the headspace. For example, a feed gas mixture of 7% propylene / 60% air / 30% steam is stable at a temperature of about 450°C.
  • Presence of 5000 ppm of nitrogen oxides can lower the ignition temperature to, for example, 300°C.
  • Presence of a short bed of packing material adjacent to the reactor tube inlets may prevent migration of contaminants into the headspace, or quench autoignition in the presence of nitrogen oxides or decrease residence time of combustible mixture in the reactor or confine the contaminants to the area where the leakage occurred or alternatively, alter the temperature profile of the reactor. Regardless of theory, the short bed has been found remarkably effective in ameliorating autoignition problems.
  • "macroparticle” is any solid three-dimensional object having a volume of at least about 0.015 ml or more; preferably more than about 0.1 ml or more.
  • FIGURE 1 shows a shell and tube reactor 10, which includes a head 15 defining a feed plenum or headspace 20, a short bed of packing material 30, a heat exchanger shell 40 and a plurality of reactor tubes 50 disposed in the reactor.
  • the feed plenum includes a distributor 60 for admixing reactants in a feed gas mixture.
  • the feed plenum 20 is in communication with the plurality of reactor tubes 50 in a heat exchanger 40, through an end plate 55.
  • the dimensions of the feed plenum or headspace 20 can vary with the cross-section area of the reactor tubes in the reactor 10.
  • the feed plenum can be from about 5 to about 14 feet tall, with a diameter of the feed plenum from about 2 to about 20 feet.
  • the plurality of reactor tubes 50 with reactor tube inlets 70 are surrounded by a heat exchanger medium 80.
  • the heat exchange medium 80 can be a salt.
  • the salt coolant can include melts of salts. Suitable salts include potassium nitrate, potassium nitrite, sodium nitrite and/or sodium nitrate or metals having a low melting point, for example, sodium, mercury or alloys of various metals.
  • the temperature of the heat exchange medium can be less than 450°C, more preferably about 420°C.
  • Dupont's HITEC salt can be used, which includes about 53% potassium nitrate, about 40% sodium nitrate, and about 7% sodium nitrate.
  • Contaminants formed by decomposition of anions in salt coolant can leak through the end plate area 65 into the feed plenum 20 in the event of a reactor break. It is believed that the salt leaks first and then decomposes in the presence of rust and oxidation catalyst.
  • the short bed of packed material 30 is disposed adjacent to the reactor tube inlets 70, extending horizontally in the plenum.
  • the short bed 30 includes discrete inert macroparticles of, for example, ceramic material.
  • the short bed of packing material 30 can vary in dimensions. Suitable depth, H, of the short bed can be less than 24 inches or so but at least 5 inches; typically, 1 foot or so. Shape of such inert macroparticles is not critical.
  • the macroparticles may be granular, such as a sphere, pellet, disk, hollow tube, spherical, cylindrical, ring-formed, or may be in the forms of rods, plates, and wire net or in the form of aggregates thereof.
  • Suitable macroparticles can be spheres. When granular or other inert substances are used, their sizes are not necessarily uniform.
  • the diameter of the sphere can be from about 1/16 inch to about 2 inches, preferably about 0.25 inch diameter.
  • the size of the macroparticles is most preferably not larger than the diameter of reactor tubes (ca. 1") in the reactor, so as to not occlude the reactor tubes.
  • the short bed 30 has a substantial voidage so as not to cause too much of a pressure drop or pressure differential during the passage of feed gas mixture to the reactor tubes.
  • the voidage of the macroparticles in the short bed 30 can be from about 0.25 to about 0.75, preferably from about 0.3 to 0.5 and most preferably 0.4.
  • the packing density of the macroparticles can be from about 70 lbs/ft 3 to about 110 lbs/ft 3 , with from about 80-90 lbs/ft 3 being somewhat typical.
  • the spheres can be, for example, DENSTONE® spheres, which are commercially available for Norton Chemicals (Akron, OH, USA).
  • the DENSTONE® spheres can be, for example, DENSTONE®57, DENSTONE® 2000 or DENSTONE® 99.
  • the macroparticles can be ceramic, alumina, silica or clay in composition.
  • the short bed of packed material 30 provides an increase in velocity of the feed gas mixture to the reactor tube inlets because the cross section available for flow is decreased by the area occupied by the macroparticles.
  • Such an increase in velocity of the feed gas mixture sweeps contaminants such as oxidizers, for example, nitrogen oxides, stemming from end plate breaches into the reactor tubes 50 before they migrate into the plenum generally.
  • Adequate flow velocity and a streamlined flow path can reduce flammability in the feed plenum 20, where the feed gas mixture and contaminants can mix to cause a potential spontaneous ignition of the feed gas mixture.
  • Spontaneous auto-ignition can be controlled by passing the feed gas mixture to the reactor tubes in a time that is less than the time required for auto-ignition.
  • a method for producing acrylic acid from propylene in a two-stage catalytic oxidation using shell-and-tube heat exchanger type reactor have been described. See, for example, United States Patent Nos.
  • the distributor 60 conveys a feed gas mixture of reactants into the feed plenum or headspace 20.
  • the feed gas mixture expands into and through the feed plenum 20 to the short bed ⁇ f packed material 30.
  • the superficial velocity of the feed gas mixture into the feed plenum can be in the range of 3 to 10 ft/sec.
  • the feed gas mixture can include 7% propylene / 60% air / 30%> steam.
  • the feed gas mixture enters the short bed of packed material 30 adjacent to the reactor tubes inlets 70 of the reactor.
  • Optimum packing material can be determined by the size of the tubular reactor, gas flow combination, flow through the inlet plenum, desired pressure drop and velocity profile in the short bed.
  • a feed gas mixture including n-butane, and air passes via distributor 60 to feed plenum 20.
  • the feed gas mixture is distributed uniformly over the short bed of packing material 30 and passes to the reactor tubes 50.
  • n-butane reacts with oxygen in the air to produce maleic anhydride.
  • a feed gas mixture including isobutylene, and air passes via distributor 60 to feed plenum 20.
  • the feed gas mixture is distributed uniformly over the short bed of packing material 30 and passes to the reactor tubes 50.
  • isobutylene reacts with oxygen in the air to produce methacrylic acid.
  • Still other products, such as vinyl acetate or ethylene oxide may be made in accordance with the present invention.
  • COMPARATIVE EXAMPLE In a process for oxidation of propylene to acrylic acid, a tubular reactor including a plurality of reactor tubes having a cross-sectional area of (ca. 60 ft 2 open tube area; ca.
  • EXAMPLE 1 The reactor of the comparative example above was charged with a short bed of packing material of DENSTONE® l A" spheres. The depth of the short bed of packing material was 1 ft.
  • the reactor conditions were selected such that a temperature of ca. 620°F; 326°C and a pressure of ca. 16 psig; 1.1 bar gauge prevailed in the reactor with a composition of the feed gas mixture being ca. 7% propylene, ca. 60% air and ca. 30% steam.
  • the system was operated such that a circulating volume gas flow of ca. 1200 MSCFH was obtained. Autoignition of the feed was virtually eliminated by placement of the short bed about the reactor tube inlets, while yields and conversions were unchanged.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Furan Compounds (AREA)

Abstract

Selon l'invention, des améliorations sont apportées à un processus d'oxydation qui se déroule dans un réacteur à enveloppe et tubes (10), grâce à la mise en place d'un petit lit de matière de remplissage (30) autour des entrées des tubes (50). Le petit lit de matière de remplissage sert à diriger les substances contaminantes provenant de l'agent d'échange thermique, hors de l'espace vide (20), ce qui permet d'éviter la formation de mélanges gazeux combustibles.
PCT/US2003/023933 2003-07-31 2003-07-31 Procede d'oxydation et reacteur comprenant un systeme d'alimentation modifie WO2005016509A1 (fr)

Priority Applications (7)

Application Number Priority Date Filing Date Title
JP2005507860A JP2007521126A (ja) 2003-07-31 2003-07-31 改良された供給システムを用いる酸化方法及び反応器
US10/565,923 US20060292046A1 (en) 2003-07-31 2003-07-31 Oxidation process and reactor with modified feed system
MXPA06001255A MXPA06001255A (es) 2003-07-31 2003-07-31 Proceso de oxidacion, y reactor con sistema de alimentacion modificado.
PCT/US2003/023933 WO2005016509A1 (fr) 2003-07-31 2003-07-31 Procede d'oxydation et reacteur comprenant un systeme d'alimentation modifie
EP03818197A EP1660225A1 (fr) 2003-07-31 2003-07-31 Procede d'oxydation et reacteur comprenant un systeme d'alimentation modifie
CN03826973.2A CN1819869A (zh) 2003-07-31 2003-07-31 氧化方法和具有改良进料系统的反应器
BRPI0318401-3A BR0318401A (pt) 2003-07-31 2003-07-31 processo e aparelho para a oxidação em alta temperatura de um reagente gasoso e método para fabricar ácido acrìlico em um reator tubular

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US2003/023933 WO2005016509A1 (fr) 2003-07-31 2003-07-31 Procede d'oxydation et reacteur comprenant un systeme d'alimentation modifie

Publications (1)

Publication Number Publication Date
WO2005016509A1 true WO2005016509A1 (fr) 2005-02-24

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EP (1) EP1660225A1 (fr)
JP (1) JP2007521126A (fr)
CN (1) CN1819869A (fr)
BR (1) BR0318401A (fr)
MX (1) MXPA06001255A (fr)
WO (1) WO2005016509A1 (fr)

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JP2006129450A (ja) * 2004-10-27 2006-05-18 Nec Corp ネットワーク内の移動局との通信を制御する方法
US8926918B2 (en) 2009-10-09 2015-01-06 Dow Global Technologies Llc Isothermal multitube reactors
US8933280B2 (en) 2009-10-09 2015-01-13 Dow Global Technologies Llc Processes for the production of hydrofluoroolefins
US9056808B2 (en) 2011-05-31 2015-06-16 Dow Global Technologies, Llc Process for the production of chlorinated propenes
US9067855B2 (en) 2011-11-21 2015-06-30 Dow Global Technologies Llc Process for the production of chlorinated alkanes
US9169177B2 (en) 2011-12-22 2015-10-27 Blue Cube Ip Llc Process for the production of tetrachloromethane
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
US9284239B2 (en) 2011-12-02 2016-03-15 Blue Cube Ip Llc Process for the production of chlorinated alkanes
US9321707B2 (en) 2012-09-20 2016-04-26 Blue Cube Ip Llc Process for the production of chlorinated propenes
US9334205B2 (en) 2011-12-13 2016-05-10 Blue Cube Ip Llc Process for the production of chlorinated propanes and propenes
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
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
EP2106848A3 (fr) * 2008-03-31 2017-09-13 Rohm and Haas Company Procédé et appareil pour atténuation de pression de déflagration
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

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CN102861538A (zh) * 2012-09-28 2013-01-09 神华集团有限责任公司 列管式固定床反应器

Citations (4)

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JP2006129450A (ja) * 2004-10-27 2006-05-18 Nec Corp ネットワーク内の移動局との通信を制御する方法
EP2106848A3 (fr) * 2008-03-31 2017-09-13 Rohm and Haas Company Procédé et appareil pour atténuation de pression de déflagration
US8926918B2 (en) 2009-10-09 2015-01-06 Dow Global Technologies Llc Isothermal multitube reactors
US8933280B2 (en) 2009-10-09 2015-01-13 Dow Global Technologies Llc Processes for the production of hydrofluoroolefins
US9056808B2 (en) 2011-05-31 2015-06-16 Dow Global Technologies, 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
US9233896B2 (en) 2011-08-07 2016-01-12 Blue Cube Ip Llc Process for the production of chlorinated propenes
US9067855B2 (en) 2011-11-21 2015-06-30 Dow Global Technologies Llc Process for the production of chlorinated alkanes
US9199899B2 (en) 2011-12-02 2015-12-01 Blue Cube Ip Llc Process for the production of chlorinated alkanes
US9284239B2 (en) 2011-12-02 2016-03-15 Blue Cube Ip Llc Process for the production of chlorinated alkanes
US9334205B2 (en) 2011-12-13 2016-05-10 Blue Cube Ip Llc Process for the production of chlorinated propanes and propenes
US9169177B2 (en) 2011-12-22 2015-10-27 Blue Cube Ip Llc Process for the production of tetrachloromethane
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
US9321707B2 (en) 2012-09-20 2016-04-26 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
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

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EP1660225A1 (fr) 2006-05-31
CN1819869A (zh) 2006-08-16
BR0318401A (pt) 2006-08-01
MXPA06001255A (es) 2006-05-15

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