WO2011041337A2 - Systèmes et procédés pour réduire le bruit de fond d'entraînement - Google Patents

Systèmes et procédés pour réduire le bruit de fond d'entraînement Download PDF

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Publication number
WO2011041337A2
WO2011041337A2 PCT/US2010/050611 US2010050611W WO2011041337A2 WO 2011041337 A2 WO2011041337 A2 WO 2011041337A2 US 2010050611 W US2010050611 W US 2010050611W WO 2011041337 A2 WO2011041337 A2 WO 2011041337A2
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WIPO (PCT)
Prior art keywords
headpiece
reactor
vent
vents
center
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PCT/US2010/050611
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English (en)
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WO2011041337A3 (fr
Inventor
Haitham Naeem Saleh Yousef
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Invista Technologies S. A. R. L.
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Priority to CN2010800444873A priority Critical patent/CN102574094A/zh
Publication of WO2011041337A2 publication Critical patent/WO2011041337A2/fr
Publication of WO2011041337A3 publication Critical patent/WO2011041337A3/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • 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
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • B01J8/222—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid in the presence of a rotating device only
    • 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
    • C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
    • C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl 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
    • B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
    • B01J2204/005—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the outlet side being of particular interest

Definitions

  • aromatic carboxylic acids such as terephthalic acid (TA) typically involves the liquid-phase oxidation of an aromatic feedstock compound, such as paraxylene, using molecular oxygen in a solvent, usually in the presence of a catalyst that incorporates a promoter.
  • TA terephthalic acid
  • the solvent, molecular oxygen, feedstock, and catalyst are continuously fed into an oxidation reactor at an elevated temperature and pressure.
  • Feedstock oxidation and other reactions within the reactor produce a high-pressure gaseous stream or "off-gas" that typically comprises nitrogen, unreacted oxygen, carbon dioxide, carbon monoxide and, where bromine is used as a promoter, methyl bromide. Because the oxidation reaction is exothermic, the solvent is often allowed to vaporize to control the reaction temperature. Therefore, the off-gas may further comprise vaporized solvent.
  • the off-gas from the reactor contains a significant amount of energy, which can be recovered to reduce the total energy consumed during production and at least partially offset the cost of obtaining the high temperatures and pressures required by the oxidation reactor.
  • Such recovery often involves passing the off-gas through one or more condensers of an overheads vapor handling system, or "overheads system,” to transfer heat from the off-gas to water that also passes through the condensers to generate steam, or to another heat transfer medium.
  • the residual, non-condensable off-gas can be cleaned to remove toxic, noxious, or flammable components, for example by high-pressure combustion or scrubbing.
  • the off-gas from the reactor often contains various particles, which may include liquid droplets of solvent or water as well as solid particles of the aromatic carboxylic acid. Such particles can reduce the efficiency of the condensers and other components of the overheads system. It is therefore desirable to minimize the entrainment of such particles into the overheads system. Although various impingement devices have been developed for reducing particle entrainment, such devices often become clogged such that their use is disadvantageous.
  • FIG. 1 is a schematic view of an embodiment of a system for producing an aromatic carboxylic acid.
  • FIG. 2 is a partial side view of a first example embodiment of an oxidation reactor that can be used in the system of FIG. 1 , the reactor having a single outlet vent.
  • FIG. 3 is a partial side view of a second example embodiment of an oxidation reactor that can be used in the system of FIG. 1 , the reactor having multiple outlet vents.
  • FIG. 4 is a schematic plan view of an oxidation reactor illustrating a first example vent configuration.
  • FIG. 5 is a schematic plan view of an oxidation reactor illustrating a second example vent configuration.
  • FIG. 6 is a schematic plan view of an oxidation reactor illustrating a third example vent configuration.
  • FIG. 7 is a schematic plan view of an oxidation reactor illustrating a fourth example vent configuration.
  • FIG. 8 is a graph that plots particle entrainment as a function of particle diameter for various vent configurations.
  • FIG. 9 is a graph that plots particle entrainment as a function of particle diameter for a single vent configuration at various radial positions.
  • FIG. 10 is a graph that plots particle entrainment as a function of particle diameter for a double vent configuration at various radial positions.
  • FIG. 11 is a graph that plots particle entrainment as a function of particle diameter for a triple vent configuration at various radial positions.
  • FIG. 12 is a graph that plots particle entrainment as a function of particle diameter for a quadruple vent configuration at various radial positions.
  • FIG. 13 is a graph that plots particle entrainment as a function of particle diameter for a double vent configuration at various radial positions for a small reactor.
  • FIG. 14 is a graph that plots entrainment as a function of the number of outlet vents for an equivalent radial position.
  • FIG. 15 is a graph that plots entrainment as a function of radial location for various vent configurations.
  • FIG. 16 is a graph that plots entrainment as a function of vent diameter for single and double vent configurations.
  • FIG. 17 is a graph that plots entrainment as a function of radial location for a double vent configuration and different reactor sizes.
  • entrainment can be reduced by controlling the position and/or number of reactor outlet vents. In some embodiments, entrainment is reduced by positioning a single outlet vent a preferred distance from the center of a reactor headpiece. In other embodiments, entrainment is reduced by providing the headpiece with multiple outlet vents.
  • the system 10 comprises a reaction system that generally includes an oxidation reactor 14 in which the aromatic feedstock can be oxidized to produce the aromatic carboxylic acid. More particularly, an aromatic carboxylic acid can be produced within the reactor 14 through the high pressure, exothermic oxidation of a suitable aromatic feedstock compound in a liquid-phase reaction using an oxidant, an oxidation solvent, a catalyst, and a promoter.
  • the aromatic feedstock compound used can be any aromatic compound that has oxidizable substituents that can be oxidized to a carboxylic acid group.
  • the oxidizable substituent can be an alkyl group such as a methyl, ethyl, or isopropyl group.
  • the substituent can also be a partially-oxidized alkyl group, such as an alcohol group, aldehyde group, or ketone group.
  • the aromatic portion of the aromatic feedstock compound can be a benzene nucleus or it can be bi- or polycyclic, for example a naphthalene nucleus.
  • the number of oxidizable substituents on the aromatic portion of the aromatic feedstock compound can be equal to the number of sites available on the aromatic portion of the aromatic feedstock compound, but is generally fewer, for example approximately 1 to 4 or 2 or 3.
  • suitable aromatic feedstock compounds include toluene, ethylbenzene, orthoxylene, metaxylene, paraxylene, 1-formyI-4-methylbenzene, 1-hydroxymethyl-4-methylbenzene, 1 ,2,4- trimethylbenzene, 1-formyl-2,4-dimethylbenzene, 1 ,2,4,5-tetramethylbenzene, alkyl, hydroxymethyl, formyl, and acyl substituted naphthalene compounds such as 2,6- and 2,7-dimethylnaphthalene, 2-acyl-6-methylnaphthalene, 2-formyl-6- methylnaphthalene, 2-methyl-6-ethylnaphthalene, 2,6-diethylnaphthalene, and
  • oxygen-containing gas fed to the oxidation reactor 14 can comprise an exhaust gas-vapor mixture.
  • the flow rate of oxygen-containing gas fed to the oxidation reactor 14 is controlled to maintain an oxygen concentration in the headpiece in the range from approximately 0.5 to 8 volume percent oxygen (measured on a solvent-free basis).
  • a feed rate of the oxygen-containing gas sufficient to provide oxygen in the amount of from approximately 1.5 to approximately 2.8 moles per methyl group will provide approximately 0.5 to 8 volume percent of oxygen (measured on a solvent-free basis) in the overhead gas-vapor mixture.
  • the oxidation solvent can be a low molecular weight aliphatic monocarboxylic acid having approximately 2 to 6 carbon atoms, or mixtures thereof with water.
  • the solvent comprises acetic acid or a mixture of acetic acid and water.
  • Suitable catalysts include those heavy metals having an atomic number of approximately 21 to 82, such as a mixture of cobalt and manganese, and suitable promoters include bromine compounds such as hydrogen bromide, molecular bromine, and sodium bromide.
  • the catalyst/promoter employed in producing crude terephthalic acid can, for example, comprise cobalt, manganese, and bromine components, and can additionally comprise accelerators.
  • the ratio of cobalt (calculated as elemental cobalt) in the cobalt component of the catalyst-to- paraxylene in the liquid-phase oxidation can be in the range of about approximately 0.2 to 10 milligram atoms (mga) per gram mole of paraxylene.
  • the ratio of manganese (calculated as elemental manganese) in the manganese component of the catalyst-to-cobalt (calculated as elemental cobalt) in the cobalt component of the catalyst in the liquid-phase oxidation is suitably in the range of about approximately 0.2 to 10 mga per mga of cobalt.
  • the weight ratio of bromine (calculated as elemental bromine) in the bromine component of the catalyst-to- total cobalt and manganese (calculated as elemental cobalt and elemental manganese) in the cobalt and manganese components of the catalyst in the liquid-phase oxidation can be in the range of approximately 0.2 to 1.5 mga per mga of total cobalt and manganese.
  • Each of the cobalt and manganese components can be provided in any of its known ionic or combined forms that provide soluble forms of cobalt, manganese, and bromine in the solvent in the oxidation reactor 14.
  • the solvent is an acetic acid medium
  • cobalt and/or manganese carbonate, acetate tetrahydrate, and/or bromide can be employed.
  • bromine-to-total catalyst metals include elemental bromine (Br 2 ), ionic bromine (for example HBr, NaBr, KBr, NhUBr, etc.), or organic bromides that are known to provide bromide ions at the operating temperature of the oxidation (e.g., benzylbromide, mono- and di- bromoacetic acid, bromoacetyl bromide, tetrabromoethane, ethylene-di-bromide, etc.).
  • bromine bromine
  • ionic bromine for example HBr, NaBr, KBr, NhUBr, etc.
  • organic bromides that are known to provide bromide ions at the operating temperature of the oxidation (e.g., benzylbromide, mono- and di- bromoacetic acid, bromoacetyl bromide, tetrabromoethane, ethylene-di-bromide, etc.).
  • the total bromine including molecular bromine, organic bromine, and ionic bromide, is used to determine the elemental bromine-to-total catalyst metals ratio.
  • the bromine ion released from the organic bromides at the oxidation operating conditions can be readily determined by known analytical means.
  • the minimum pressure at which the oxidation reactor 14 is maintained is typically that pressure that will maintain a substantial liquid phase of the paraxylene and the solvent.
  • suitable reaction gauge pressures in the oxidation reactor 14 can be in the range of approximately 0 kg/cm 2 to 35 kg/cm 2 , and typically are in the range of approximately 10 kg/cm 2 to 20 kg/cm 2 .
  • the temperature range within the oxidation reactor can be, for example, approximately 120°C to 250°C.
  • the solvent residence time in the reactor 14 is approximately 20 to 150 minutes, and preferably approximately 30 to 120 minutes.
  • the oxidation reactor 14 typically comprises a vessel that is constructed of or lined with a corrosion-resistant material, such as titanium or glass. Because the oxidation reaction is conducted at an elevated pressure, the reactor 14 is constructed to withstand the high pressures used for the oxidation reaction.
  • the contents of the oxidation reactor 14 are agitated to optimize the oxidation reaction and maintain the solid reaction product in suspension. Agitation comprises specific fluid mixing configurations and the oxidation reactor 14 can be equipped with one or more mechanical agitators (not shown).
  • Crude terephthalic acid which is the solid reaction product produced by the oxidation reaction, leaves the reactor 14 along an outlet line 16 in the form of an oxidation reaction slurry that comprises a mixture of crude terephthalic acid, water, acetic acid, catalyst metals, oxidation reaction intermediates, and reaction byproducts. The slurry is then processed using a variety of procedures and equipment (not shown) to produce purified terephthalic acid.
  • the off-gas is used to raise various pressures of steam that can, for example, be used to drive and/or heat other components of the system 10.
  • the off-gas exits the headpiece of the oxidation reactor 4 through one or more outlet vents 17 and passes into a gas line 18 that delivers the off-gas to a series of condensers 20, 22, and 24, which condense the off-gas and raise steam.
  • the first condenser 20 produces a first pressure of steam (e.g., at approximately 145°C and 4.5 bar)
  • the second condenser 22 produces a second pressure of steam (e.g., at approximately 130°C and 3 bar)
  • the third condenser 24 produces a third pressure of steam (e.g., at approximately 100°C and 1 bar).
  • the steam from the condensers 20, 22, and 24 can flow to various other components (not shown) of the system 10 through steam lines 26, 28, and 30.
  • Example components that may receive steam include reboilers, driers, turbines, heat exchangers, and the like.
  • organic materials within the off-gas condense and that condensate can be returned to the oxidation reactor 14 after processing.
  • the remaining off-gas is relatively cold, but is still at relatively high pressure and can also be used for energy recovery purposes.
  • the off-gas exits through a gas line 32 to be delivered to another system component (not shown).
  • a component is an expander.
  • the off-gas can be cleaned to remove toxic, noxious, or flammable components, for example by high-pressure combustion or scrubbing.
  • FIGs. 2 and 3 illustrate two example oxidation reactors that can be used in the system 10 of FIG. 1.
  • a single vent oxidation reactor 40 comprising a vessel 42 that is capped by a headpiece 44. Extending from the headpiece 44 is a single outlet vent 46 that is generally parallel with the vessel but offset from the center of the headpiece.
  • the vent 46 can be coupled to a gas line that leads to the condensers (e.g., gas line 18 in FIG. 1 ) or can form part of such a gas line.
  • Shown in FIG. 3 is a multiple vent oxidation reactor 50, which also comprises a vessel 52 that is capped by a headpiece 54.
  • the reactor 50 comprises two outlet vents 56 and 58 that together join a single line 60 downstream of the reactor. Although only two outlet vents are illustrated in FIG. 3, it will be clear from the disclosure that follows that the reactor 50 could alternatively comprise more than two outlets that join together downstream of the reactor.
  • the two-vent arrangement shown in FIG. 3 is provided to illustrate the concept of a multiple vent reactor.
  • FIGs. 4-7 illustrate in schematic plan view various vent configurations that can be employed for an oxidation reactor.
  • a headpiece 70 comprises a single outlet vent 72.
  • the center of the vent 72 is offset from the center of the headpiece 70 by a center-to-center distance C2C.
  • the C2C distance can be considered to comprise a percentage of the headpiece radius R in which the headpiece center is at 0% R and the outer edge of the headpiece is at 100% R.
  • FIG. 5 illustrates a vent configuration similar to that shown in FIG. 3.
  • a headpiece 80 comprises two outlet vents 82.
  • the center of each vent 82 is offset from the center of the headpiece 80 by a center-to-center distance C2C. Therefore, each vent 82 is equidistant to the headpiece center.
  • the centers of the vents 82 are separated from each other by a vent-to- vent distance V2V.
  • FIG. 6 illustrates a further vent configuration.
  • a headpiece 90 comprises three outlet vents 92 that are arranged in an equilateral triangle configuration.
  • the center of each vent 92 is offset from the center of the headpiece 90 by a center-to-center distance C2C. Therefore, each vent 92 is equidistant to the headpiece center.
  • the centers of the vents 92 are separated from each other by a vent-to-vent distance V2V.
  • FIG. 7 illustrates yet another vent configuration.
  • a headpiece 100 comprises four outlet vents 102 that are arranged in a square configuration.
  • the center of each vent 102 is offset from the center of the headpiece 100 by a center-to-center distance C2C. Therefore, each vent 102 is equidistant to the headpiece center.
  • the centers of the vents 102 are separated from each other by a vent-to-vent distance V2V.
  • vent configurations were evaluated by modeling using computational fluid dynamics. Specifically, computer-based fluid dynamics simulations were performed on various vent configurations. Table 1 identifies some of the variables that were used in the simulations.
  • particle size groups were used to represent entrainment particles, which could be liquid and/or solid particles.
  • particles of 1 , 0.9, 0.8, 0.7, 0.6, 0.5, 0.4, 0.3, 0.2, 0.1 , 0.05, 0.03, 0.01 , and 0.005 millimeters (mm) in diameter were used.
  • 250 particles from each particle size group were assumed to be released from the surface of a liquid within the oxidation reactor.
  • a simulation duration of 120 seconds was used, which resulted in a total of 420,000 particles (14*250*120) being released and tracked.
  • results were post-processed and the number of particles in each size group that exited through the vent or vents (i.e., that entrained) were identified and used to evaluate performance.
  • the results were then presented in two ways: (1 ) the percentage of entrained particles in every size group as a function of the number of vents, the vent radial position, and the reactor size, and (2) the percentage of entrained particles' volume as a function of the number of vents, the percentage of the headpiece radius, and the reactor size.
  • plotted is particle entrainment as a function of particle diameter for each of the single, double, triple, and quadruple vent configurations.
  • the percentage of particles that were entrained decreased as the number of vents increased. For example, approximately 37% of the 0.01 mm diameter particles were entrained in the single vent configuration, while less than 5% of those particles were entrained in the quadruple vent configuration.
  • FIG. 9 illustrated is a graph that plots particle entrainment as a function of particle diameter for the single vent configuration at various vent positions.
  • the percentage of particles that were entrained decreased as the radial position (i.e., distance of the vent center from the headpiece center) decreased.
  • the radial position i.e., distance of the vent center from the headpiece center
  • nearly 40% of the 0.01 mm diameter particles were entrained when the vent center was separated from the headpiece center by approximately 81% of the headpiece radius, while approximately 27% of those particles were entrained when the vent center was separated from the headpiece center by approximately 18% of the headpiece radius.
  • FIG. 10 plots particle entrainment as a function of particle diameter for the double vent configuration with the vents being positioned at various radial distances from the headpiece center. As indicated in FIG. 10, the lowest percentage of particle entrainment occurred when the vent centers were separated from the headpiece center by approximately 40% of the headpiece radius (one of four positions evaluated). More generally, the results indicate that the optimal position for the vents in the double vent configuration is at some position between the 20% and 58% of headpiece radius range, whether it be at, below, or above the 40% position. With reference to FIG. 11 , plotted is particle entrainment as a function of particle diameter for a triple vent configuration at various vent positions.
  • FIG. 12 plots particle entrainment as a function of particle diameter for a quadruple vent configuration at various vent positions.
  • the lowest percentage of particle entrainment occurred when the vent centers were separated from the headpiece center by approximately 58% of the headpiece radius (one of four positions evaluated). More generally, the results indicate that the optimal position for the vents in the quadruple vent configuration is at some position between the 29% and 71% of headpiece radius range.
  • FIG. 13 plotted is particle entrainment as a function of particle diameter for a double vent configuration at various vent positions for a small reactor (8.05 meters (m) in diameter).
  • FIG. 14 plots volume entrainment as a function of the number of outlet vents. As can be appreciated from FIG.
  • FIG. 14 plotted is volume entrainment as a function of vent location radius for each of the single, double, triple, and quadruple vent configurations. As can be appreciated from that figure, a clear optimal vent location (identified by the minimum point of each curve) exists for multiple vent configurations.
  • FIG. 16 compares the volume entrainment as a function of vent radius for single and double vent configurations. As indicated in FIG.
  • FIG. 17 plots entrainment as a function of vent location for a double vent configuration and different reactor sizes, i.e., an original reactor (9.92 m in diameter) and a smaller reactor (8.05 m in diameter). As can be seen from FIG. 17, there is little difference between entrainment levels between the two reactor sizes, which suggests that the relationships identified above are universally applicable.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne un appareil destiné à réduire l'entraînement des particules pendant une réaction, ledit appareil étant un réacteur d'oxydation configuré pour oxyder une charge aromatique afin de produire un acide carboxylique aromatique, ledit réacteur comprenant au moins un orifice d'évacuation par lequel les gaz d'échappement peuvent s'échapper du réacteur. L'invention divulgue également un système pour produire un acide carboxylique aromatique, le système comprenant un réacteur d'oxydation comportant au moins un orifice d'évacuation par lequel les gaz d'échappement peuvent s'échapper du réacteur; et un système en hauteur comprenant au moins un condenseur dans lequel au moins une partie des gaz d'échappement peut être condensée et de l'eau peut circuler pour générer de la vapeur.
PCT/US2010/050611 2009-10-02 2010-09-29 Systèmes et procédés pour réduire le bruit de fond d'entraînement WO2011041337A2 (fr)

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CN2010800444873A CN102574094A (zh) 2009-10-02 2010-09-29 减少夹带的系统和方法

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US24817309P 2009-10-02 2009-10-02
US61/248,173 2009-10-02

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Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5087741A (en) * 1990-11-29 1992-02-11 Eastman Kodak Company Continuous production of aromatic carboxylic acids
US5211924A (en) * 1988-02-29 1993-05-18 Amoco Corporation Method and apparatus for increasing conversion efficiency and reducing power costs for oxidation of an aromatic alkyl to an aromatic carboxylic acid
US5510521A (en) * 1995-03-27 1996-04-23 Eastman Chemical Company Process for the production of aromatic carboxylic acids
US5596129A (en) * 1994-03-22 1997-01-21 Mitsui Petrochemical Industries, Ltd. Process and apparatus for producing aromatic carboxylic acid
US5612007A (en) * 1994-10-14 1997-03-18 Amoco Corporation Apparatus for preparing aromatic carboxylic acids with efficient energy recovery
US20020183546A1 (en) * 2001-06-04 2002-12-05 Sheppard Ronald Buford Two stage oxidation process for the production of aromatic dicarboxylic acids
US20020193629A1 (en) * 2001-06-04 2002-12-19 Miller Harold David Process for production of aromatic carboxylic acids with improved water removal technique
US20080194865A1 (en) * 2005-03-21 2008-08-14 Bp Corporation North America Inc. Recovery of Energy During the Production of Aromatic Carboxylic Acids

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5443806A (en) * 1994-03-22 1995-08-22 A. Ahlstrom Corporation Treating exhaust gas from a pressurized fluidized bed reaction system
CN1232341C (zh) * 2003-12-12 2005-12-21 华东理工大学 一种催化重整和催化脱氢固定床径向反应器

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5211924A (en) * 1988-02-29 1993-05-18 Amoco Corporation Method and apparatus for increasing conversion efficiency and reducing power costs for oxidation of an aromatic alkyl to an aromatic carboxylic acid
US5087741A (en) * 1990-11-29 1992-02-11 Eastman Kodak Company Continuous production of aromatic carboxylic acids
US5596129A (en) * 1994-03-22 1997-01-21 Mitsui Petrochemical Industries, Ltd. Process and apparatus for producing aromatic carboxylic acid
US5612007A (en) * 1994-10-14 1997-03-18 Amoco Corporation Apparatus for preparing aromatic carboxylic acids with efficient energy recovery
US5510521A (en) * 1995-03-27 1996-04-23 Eastman Chemical Company Process for the production of aromatic carboxylic acids
US20020183546A1 (en) * 2001-06-04 2002-12-05 Sheppard Ronald Buford Two stage oxidation process for the production of aromatic dicarboxylic acids
US20020193629A1 (en) * 2001-06-04 2002-12-19 Miller Harold David Process for production of aromatic carboxylic acids with improved water removal technique
US20080194865A1 (en) * 2005-03-21 2008-08-14 Bp Corporation North America Inc. Recovery of Energy During the Production of Aromatic Carboxylic Acids

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WO2011041337A3 (fr) 2011-09-29
SA110310733B1 (ar) 2014-08-25

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