US20120010430A1 - Metering ring - Google Patents

Metering ring Download PDF

Info

Publication number
US20120010430A1
US20120010430A1 US13/256,638 US201013256638A US2012010430A1 US 20120010430 A1 US20120010430 A1 US 20120010430A1 US 201013256638 A US201013256638 A US 201013256638A US 2012010430 A1 US2012010430 A1 US 2012010430A1
Authority
US
United States
Prior art keywords
metering
sites
acetone cyanohydrin
reaction
ring
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
Application number
US13/256,638
Other languages
English (en)
Inventor
Lorenza Sartorelli
Andreas Perl
Udo Gropp
Arndt Selbach
Stefanie Sohnemann
Matthias Groemping
Norbert Mnich
Thomas Mertz
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Evonik Roehm GmbH
Original Assignee
Evonik Roehm GmbH
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 Evonik Roehm GmbH filed Critical Evonik Roehm GmbH
Assigned to EVONIK ROEHM GMBH reassignment EVONIK ROEHM GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MNICH, NORBERT, SARTORELLI, LORENZA, SOHNEMANN, STEFANIE, GROPP, UDO, MERTZ, THOMAS, PERL, ANDREAS, GROEMPING, MATTHIAS, SELBACH, ARNDT
Publication of US20120010430A1 publication Critical patent/US20120010430A1/en
Abandoned legal-status Critical Current

Links

Images

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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C231/00—Preparation of carboxylic acid amides
    • C07C231/06—Preparation of carboxylic acid amides from nitriles by transformation of cyano groups into carboxamide 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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/002—Nozzle-type elements
    • 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
    • B01J4/02—Feed or outlet devices; Feed or outlet control devices for feeding measured, i.e. prescribed quantities of reagents
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C231/00—Preparation of carboxylic acid amides
    • C07C231/10—Preparation of carboxylic acid amides from compounds not provided for in groups C07C231/02 - C07C231/08
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/8158—With indicator, register, recorder, alarm or inspection means

Definitions

  • (Meth)acrylic acid and (meth)acrylic esters are important products in the chemical industry, which serve as starting materials for many important products. A maximum yield and a particularly high purity coupled with low preparation costs are therefore essential for the economic success of a preparation process for such an important product. Even relatively small improvements with regard to the yields, the service lives of the plants or similar process features lead to a significant advance with regard to the amount of undesired by-products and the preparation costs.
  • the methacrylamide used to prepare methacrylic acid can preferably be obtained by what is known as the ACH process. Proceeding from hydrogen cyanide and acetone, acetone cyanohydrin is prepared in a first step, and is then converted to methacrylamide. These steps are described, inter alia, in U.S. Pat. No. 7,253,307, EP-A-1 666 451 and PCT/EP2007 059092.
  • Acetone cyanohydrin is prepared by commonly known processes (see, for example, Ullmanns Enzyklopädie der ischen Chemie, 4 th Edition, Volume 7). Frequently, the reactants used are acetone and hydrogen cyanide. The reaction is an exothermic reaction. In order to counteract decomposition of the acetone cyanohydrin formed in this reaction, the heat of reaction is typically removed by a suitable apparatus. The reaction can in principle be conducted as a batchwise process or as a continuous process; when a continuous method is preferred, the reaction is frequently performed in a loop reactor configured correspondingly.
  • the acetone cyanohydrin prepared by different known preparation processes is typically subjected to a distillative workup. This involves freeing the stabilized crude acetone cyanohydrin of low-boiling constituents by means of an appropriate column.
  • a suitable distillation process can, for example, be conducted using only one column.
  • the crude acetone cyanohydrin is generally transferred from the storage to the distillation with a temperature of about 0 to about 15° C., for example a temperature of about 5 to about 10° C.
  • the crude acetone cyanohydrin can be introduced directly into the column.
  • the distillative purification of the acetone cyanohydrin is effected by means of a distillation column having more than 5 and preferably more than 10 trays, or by means of a cascade of two or more correspondingly suitable distillation columns.
  • the column bottom is preferably heated with steam. It has been found to be advantageous when the bottom temperature does not exceed a temperature of 140° C.; it has been possible to achieve good yields and good purification when the bottom temperature is not greater than about 130° C. or not higher than about 110° C.
  • the temperature figures are based on the wall temperature of the column bottom.
  • the crude acetone cyanohydrin is supplied to the column body in the upper third of the column.
  • the distillation is preferably performed under reduced pressure, for example at a pressure of about 50 to about 900 mbar, especially of about 50 to about 250 mbar, and with good results between 50 and about 150 mbar.
  • gaseous impurities especially acetone and hydrogen cyanide
  • a heat exchanger or a cascade of two or more heat exchangers preference is given to using brine cooling with a temperature of about 0 to about 10° C.
  • the first condensation stage can take place, for example, at standard pressure. It is, however, likewise possible, and has in some cases been found to be advantageous, when this first condensation stage is effected under reduced pressure, preferably at the pressure which exists in the distillation.
  • the condensate is passed on into a cooled collecting vessel and collected there at a temperature of about 0 to about 15° C., especially at about 5 to about 10° C.
  • the gaseous compounds which do not condense in the first condensation step are removed from the reduced pressure space by means of a vacuum pump. It is possible in principle to use any vacuum pump. However, it has been found to be advantageous in many cases when a vacuum pump which, owing to its design, does not lead to the introduction of liquid impurities into the gas stream is used. Preference is therefore given here to using, for example, dry-running vacuum pumps.
  • the gas stream which escapes on the pressure side of the pump is conducted through a further heat exchanger which is preferably cooled with brine at a temperature of about 0 to about 15° C.
  • the condensation performed on the pressure side of the vacuum pump can be effected, for example, by means of one heat exchanger, but also with a cascade of two or more heat exchangers arranged in series in parallel. Gaseous substances remaining after this condensation step are removed and sent to any further utilization, for example a thermal utilization.
  • the condensates collected can likewise be utilized further in any way. However, it has been found to be extremely advantageous from an economic point of view to recycle the condensates into the reaction for preparation of acetone cyanohydrin. This is preferably done at one or more points which enable access to the loop reactor.
  • the condensates may in principle have any composition provided that they do not disrupt the preparation of the acetone cyanohydrin. In many cases, the predominant amount of the condensate will, however, consist of acetone and hydrogen cyanide, for example in a molar ratio of about 2:1 to about 1:2, frequently in a ratio of about 1:1.
  • the acetone cyanohydrin obtained from the bottom of the distillation column is first cooled in a first heat exchanger by the cold crude acetone cyanohydrin supplied to a temperature of about 40 to about 80° C. Subsequently, the acetone cyanohydrin is cooled by means of at least one further heat exchanger to a temperature of about 30 to about 35° C. and optionally stored intermediately.
  • acetone cyanohydrin is subjected to a hydrolysis. At various temperature levels, and after a series of reactions, this forms methacrylamide as the product.
  • the conversion is accomplished in a manner known per se to the person skilled in the art by reaction between concentrated sulphuric acid and acetone cyanohydrin.
  • the reaction is exothermic, and so heat of reaction can be removed from the system in an advantageous manner.
  • loop reactors are known in the technical field. These may be configured, for example, in the form of tubular reactors with recycling. The reaction can be effected, for example, in only one loop reactor. However, it may be advantageous when the reaction is performed in a cascade of two or more loop reactors.
  • a suitable loop reactor in the context of the process described has one or more feed sites for acetone cyanohydrin, one or more feed sites for concentrated sulphuric acid, one or more gas separators, one or more heat exchangers and one or more mixers.
  • the loop reactor may comprise further constituents, such as conveying means, pumps, control elements, etc.
  • an apparatus for metering free-flowing media or gases characterized in that one or more metering rings with metering sites [ 11 ] provided in pipelines, tubular reactors or loop reactors are used.
  • the inventive metering ring may have various embodiments. For instance, many small metering sites may be incorporated into the ring, or few large metering sites ( FIG. 1 ). The metering sites may also project through tubes [ 13 ] into the interior of the tube ( FIG. 2 ), and in particular embodiments also tubes of different lengths.
  • the metering ring may be cooled or heated according to the metering task.
  • a particular embodiment is a metering ring in which the metered addition is effected under elevated pressure.
  • the apparatus may assume any suitable three-dimensional shape, and is preferably constructed in the form of a ring. It is also possible here to use double or multiple rings.
  • the metering ring is particularly suitable for use in continuous processes.
  • the metering ring is preferably used in the continuous preparation of methacrylamide by hydrolysis of acetone cyanohydrin with sulphuric acid.
  • One example of another field of use would be the preparation of acetone cyanohydrin from acetone and hydrogen cyanide.
  • the reaction is effected continuously in a tubular reactor or loop reactor.
  • continuous and tubular reactor are known in the technical field.
  • a continuous reaction is understood to mean especially reactions in which reactants are added to and products are removed from the reaction mixture over a prolonged period.
  • Tubular reactors comprise at least one tubular region in which the reaction can proceed. These reactors typically have a relatively simple construction, and so the capital costs are comparatively low.
  • the reactants can be introduced into the tubular reactor by means of a pump.
  • a pump To prevent maintenance-related operation shutdowns, it is also possible to provide two or more pumps which can be connected in parallel. Viewed in flow direction, the reactants can appropriately be mixed with a metering ring upstream of the pumps, i.e. on the pump suction side, and the system more preferably does not have any further internals for mixing in the region between the pumps and the tubular reactor.
  • the metering ring may, however, also be part of the pump and may be integrated into the pump housing.
  • the components of the plant which come into contact with corrosive substances are built from suitable materials, for example an acid-resistant metal, for example zirconium, tantalum, titanium or stainless steel, or a coated metal which has, for example, an enamel layer or a zirconium layer. It is additionally also possible to use polymers, for example PTFE-coated components, graphitized components or graphite parts, especially in pumps.
  • suitable materials for example an acid-resistant metal, for example zirconium, tantalum, titanium or stainless steel, or a coated metal which has, for example, an enamel layer or a zirconium layer.
  • polymers for example PTFE-coated components, graphitized components or graphite parts, especially in pumps.
  • part of the volume flow of a stream of acetone cyanohydrin is introduced into a first loop reactor.
  • a first loop reactor preferably has one or more heat exchangers, one or more pumps, one or more mixing elements and one or more gas separators.
  • the circulation flows which pass through the first loop reactor are preferably in the range from about 50 to 650 m 3 /h, more preferably in a range from 100 to 500 m 3 /h and additionally preferably in a range from about 150 to 450 m 3 /h.
  • the circulation flows are preferably in a range from about 40 to 650 m 3 /h, more preferably in a range from 50 to 500 m 3 /h and additionally preferably in a range from about 60 to 350 m 3 /h.
  • a preferred temperature difference over the heat exchanger is about 1 to 20° C., particular preference being given to about 2 to 7° C.
  • the supply of the acetone cyanohydrin, according to the invention via a metering ring, can in principle be effected anywhere in the loop reactor. However, it has been found to be advantageous when the supply is effected into a mixing element, for example into a mixer with moving parts or a static mixer, or at a well-mixed site.
  • the sulphuric acid is advantageously supplied upstream of the acetone cyanohydrin addition. Otherwise, however, it is likewise possible to introduce the sulphuric acid into the loop reactor anywhere.
  • the inventive metering ring is used to feed in the medium, for example the sulphuric acid or the acetone cyanohydrin, just upstream of or in a pump.
  • the medium for example the sulphuric acid or the acetone cyanohydrin
  • the highly turbulent flow in the pump housing is utilized to mix the reactants, thus utilizing a conveying machine simultaneously as a mixing machine.
  • the mixing capacity of the pump is therefore exploited in an advantageous manner.
  • the ratio of the reactants in the loop reactor is controlled such that a sulphuric acid excess is present.
  • the excess of sulphuric acid is, based on the molar ratio of the constituents, about 1.8:1 to about 3:1 in the first loop reactor, and about 1.1:1 to about 2:1 in the last loop reactor.
  • the sulphuric acid here may serve, for example, as a solvent and keep the viscosity of the reaction mixture low, which can ensure more rapid removal of heat of reaction and a lower temperature of the reaction mixture. This can bring significant yield advantages.
  • the temperature in the reaction mixture is about 85 to about 150° C.
  • the removal of heat is ensured by one or more heat exchangers in the loop reactor. It has been found to be advantageous when the heat exchangers possess a suitable sensor system for adjusting the cooling output, in order to prevent excessive cooling of the reaction mixture for the reasons mentioned above. For example, it may be advantageous to measure the heat transfer at certain points or continuously in the heat exchanger or in the heat exchangers, and adjust the cooling output of the heat exchangers thereto. This can be done, for example, via the coolant itself. It is also equally possible to achieve corresponding heating of the reaction mixture through corresponding variation in the addition of the reactants and through the generation of more heat of reaction. A combination of both possibilities is also conceivable.
  • the loop reactor preferably additionally possesses at least one gas separator.
  • the gas separator can be used firstly to withdraw product formed continuously from the loop reactor. Secondly, gases formed in the course of the reaction can thus be withdrawn from the reaction space. The gas formed is principally carbon monoxide.
  • the product withdrawn from the loop reactor is preferably transferred into a second loop reactor. In this second loop reactor, the reaction mixture comprising sulphuric acid and methacrylamide as obtained by the reaction in the first loop reactor is reacted with the remaining substream of acetone cyanohydrin. In the course of this, the excess of sulphuric acid from the first loop reactor, or at least a portion of the excess sulphuric acid, reacts with the acetone cyanohydrin to form further sulphoxyisobutyramide (SIBA).
  • SIBA sulphoxyisobutyramide
  • the performance of the reaction in two or more loop reactors has the advantage that, owing to the sulphuric acid excess in the first loop reactor, the pumpability of the reaction mixture and hence the heat transfer and ultimately the yield are improved.
  • at least one mixing element, at least one heat exchanger and at least one gas separator are arranged within the second loop reactor.
  • the reaction temperature in the second loop reactor is likewise about 90 to about 120° C.
  • the second loop reactor too advantageously possesses a heat exchanger, the cooling output of which can be regulated by means of a corresponding sensor system.
  • the acetone cyanohydrin is supplied in a suitable mixing element, preferably in a static mixer or the inventive metering ring.
  • the product can be withdrawn from the gas separator of the second loop reactor, and it can be heated to a temperature of about 130 to about 180° C. to complete the conversion and to form the methacrylamide.
  • the heating is preferably performed in such a way that the maximum temperature is attained only for a very short period, for example for a period of about one minute to about 30 minutes, especially for a period of about two to about eight minutes or about three to about five minutes.
  • This can in principle be effected in any desired apparatus for achieving such a temperature for such a short period.
  • the energy can be supplied in a conventional way by means of electrical energy or by means of steam.
  • the heating step is effected in a heat exchanger with a two-stage or multistage arrangement of tube coils which may preferably be present in an at least double, opposing arrangement.
  • the reaction mixture is heated rapidly to a temperature of about 130 to 180° C.
  • the amide solution thus obtainable generally has a temperature of more than 100° C., typically a temperature of about 130 to 180° C. Cooling to temperatures less than 130° C. is likewise possible.
  • the metering ring can also be used in overland pipelines for mineral oil transport.
  • Flow improvers have to be added to the crude oil at regular intervals. At these feed sites, the flow improver is usually added through a nozzle. The large volume flow forces the medium metered in primarily to the inside of the tube, and the conversion proceeds poorly and only over a long distance.
  • inventive metering ring it is possible to ensure that the flow improver is added to the crude oil over the entire tube cross section.
  • the invention further provides for the use of the inventive metering device in chemical processes, preferably in processes in which rapid mixing and fine distribution of a medium are required.
  • the medium supplied is reacted or mixed completely with the medium flowing past.
  • metered addition for example, of one drop of liquid, until fine mixing with the other medium, a minimum distance should be covered to the mixing point.
  • the inventive metering ring enables almost ideal mixing or conversion in the case of supply or free-flowing media or gases at one feed site.
  • the inner wall of the metering ring is permeated by any number of injection channels. Preferably 2 to 20 and more preferably 16 injection channels arranged homogeneously over the circumference are used. These may, individually or in common, be tilted with respect to the inner wall of the pipeline at an angle of 1° to 179°, preferably of 20° to 120°, more preferably of 60°.
  • the metering ring is positioned directly upstream of the suction stub of the circulation pump. It is thus possible to utilize the turbulences in the pump for mixing.
  • the supply of a gas can generate turbulence in the medium which flows through the tube. It is thus possible to prevent sedimentation of a suspension by laminar flow within the tube.
  • a broad and homogeneous distribution over the entire cross section of a tube can be achieved by virtue of the metering sites or tubes of the metering ring being of different lengths. It is thus possible to meter the reactant into the tube interior in a controlled manner.
  • the inventive metering apparatus has a broad spectrum of application, wherever rapid and/or homogeneous metered addition of free-flowing media or gases is required. It is possible to meter in liquids with low or high viscosity, but also suspensions, emulsions, gases, etc. It is used in chemical systems such as pipelines or tubular reactors.
  • the metering ring serves as a metering apparatus and/or mixer.
  • the metering ring is used in the hydrolysis of acetone cyanohydrin with sulphuric acid to give methacrylamide.
  • FIG. 1 A first figure.
  • the inventive metering ring 4 is mounted by means of clamping means 5 shown schematically in a pipeline 1 through which a medium M flows, between two tube flanges 2 and two seals 3 .
  • the metering ring 4 has a peripheral distributor chamber 6 which is supplied with the fluid F to be metered by two feed stubs 7 and 8 .
  • the inner wall 10 of the metering ring 4 is permeated by preferably sixteen injection channels 11 distributed homogeneously over the circumference. These are, again preferably, inclined at an angle ⁇ of 60° with respect to the inner wall 12 of the pipeline 1 .
  • the solution according to FIG. 2 envisages inserting into the injection channels 11 tubes 13 which have a radial projection Y with respect to the inner wall 12 of the pipeline 1 .
  • the end of the tube 13 which thus extends somewhat into the flow of the medium M, constitutes the metering point 16 .
  • a stop collar 14 is provided, which is formed by the diameter difference between the diameter d of the injection channel 11 and the outer diameter D of the tube 13 .
  • This construction feature results in rational mounting of the metering tubes 13 , while simultaneously ensuring the predetermined position of the radial distance Y of the metering point 16 from the inner wall 12 of the pipeline 1 .
  • the yield was determined in a process regime with metering ring and a downstream pump as a dynamic mixer, compared to the static mixer used conventionally.
  • the pump is arranged immediately after (connected downstream of) the metering ring in the flow direction.
  • the metering ring is flanged (mounted) directly onto the suction nozzle of the pump, in order to ensure a very short path of the ACH before mixing and thus to achieve very rapid mixing.
  • the pump, in the process regime with the inventive metering ring is a circulation pump, which is used in a loop reactor typically for circulation of the amide mixture.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Accessories For Mixers (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
  • Pipeline Systems (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Sampling And Sample Adjustment (AREA)
US13/256,638 2009-04-23 2010-03-26 Metering ring Abandoned US20120010430A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE200910002592 DE102009002592A1 (de) 2009-04-23 2009-04-23 Dosierring
DE102009002592.8 2009-04-23
PCT/EP2010/053962 WO2010121882A1 (de) 2009-04-23 2010-03-26 Dosierring

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2010/053962 A-371-Of-International WO2010121882A1 (de) 2009-04-23 2010-03-26 Dosierring

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US13/838,525 Division US9169194B2 (en) 2009-04-23 2013-03-15 Metering ring

Publications (1)

Publication Number Publication Date
US20120010430A1 true US20120010430A1 (en) 2012-01-12

Family

ID=42139987

Family Applications (2)

Application Number Title Priority Date Filing Date
US13/256,638 Abandoned US20120010430A1 (en) 2009-04-23 2010-03-26 Metering ring
US13/838,525 Active 2030-05-06 US9169194B2 (en) 2009-04-23 2013-03-15 Metering ring

Family Applications After (1)

Application Number Title Priority Date Filing Date
US13/838,525 Active 2030-05-06 US9169194B2 (en) 2009-04-23 2013-03-15 Metering ring

Country Status (14)

Country Link
US (2) US20120010430A1 (ja)
EP (1) EP2421637B1 (ja)
JP (2) JP2012524650A (ja)
KR (1) KR20120003460A (ja)
CN (1) CN102395422B (ja)
BR (1) BRPI1014260B1 (ja)
DE (1) DE102009002592A1 (ja)
ES (1) ES2424494T3 (ja)
HK (1) HK1167360A1 (ja)
RU (1) RU2538260C2 (ja)
SA (1) SA110310293B1 (ja)
SG (1) SG175776A1 (ja)
TW (1) TWI498164B (ja)
WO (1) WO2010121882A1 (ja)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2015516379A (ja) * 2012-03-30 2015-06-11 エボニック レーム ゲゼルシャフト ミット ベシュレンクテル ハフツングＥｖｏｎｉｋ Ｒｏｅｈｍ ＧｍｂＨ アセトンシアンヒドリンの加水分解方法

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR102135558B1 (ko) * 2012-10-10 2020-07-21 쉘 인터내셔날 리써취 마트샤피지 비.브이. 혼합 디바이스를 포함하는 다층 하향류 반응기, 상기 반응기의 용도, 및 혼합 방법
DE102013222634B4 (de) 2013-11-07 2019-05-16 Volkswagen Aktiengesellschaft Verfahren zur Prognostizierung eines Fahrbahn-Reibungsbeiwerts sowie Verfahren zum Betrieb eines Kraftfahrzeugs
DE102013022582B4 (de) 2013-11-07 2024-10-02 Volkswagen Aktiengesellschaft Verfahren zum Betrieb eines Kraftfahrzeugs
WO2019187039A1 (ja) * 2018-03-30 2019-10-03 三菱ケミカルエンジニアリング株式会社 微細気泡発生用ノズル、該微細気泡発生用ノズルを用いて液体に微細気泡を含む気泡を混合させる方法、該微細気泡発生用ノズルを備えた生物反応装置、および該微細気泡発生用ノズルを複数本備えた微細気泡発生用ノズル装置
CN108786505B (zh) * 2018-06-08 2020-06-12 诸暨市烈火工业设计工作室 一种水溶性颗粒混合搅拌机械设备

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3540853A (en) * 1967-06-03 1970-11-17 Titan Gmbh Means for producing titanium dioxide pigment
US5935490A (en) * 1996-07-26 1999-08-10 Boc Gases Australia Limited Oxygen dissolver for pipelines or pipe outlets
JP2000213681A (ja) * 1999-01-27 2000-08-02 Toshiba Corp 流体混合継手
US6969490B2 (en) * 2003-06-26 2005-11-29 3M Innovative Properties Company Device for the continuous process for the production of controlled architecture materials

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2548759A (en) * 1943-07-06 1951-04-10 Phillips Petroleum Co Fluid mixer-reactor
JPS6323734A (ja) * 1986-07-16 1988-02-01 Agency Of Ind Science & Technol 微粒子の製造方法とその装置
US5461932A (en) 1991-07-15 1995-10-31 Texas A & M University System Slotted orifice flowmeter
US5295397A (en) 1991-07-15 1994-03-22 The Texas A & M University System Slotted orifice flowmeter
FR2750780B1 (fr) 1996-07-05 1998-10-30 Valois Compteur de doses
JP4648548B2 (ja) 2001-01-18 2011-03-09 因幡電機産業株式会社 長尺体カバーの接続部
DE10144681A1 (de) * 2001-09-11 2003-03-27 Volkswagen Ag Strömungsreaktor und Verfahren zur Reaktionsstromführung in einem Strömungsreaktor
WO2003033097A2 (en) * 2001-10-17 2003-04-24 E.I. Du Pont De Nemours And Company Rotor-stator apparatus and process for the formation of particles
ZA200303241B (en) 2002-05-01 2003-11-04 Rohm & Haas Improved process for methacrylic acid and methcrylic acid ester production.
DE102004055425B4 (de) * 2004-11-17 2007-06-14 Forschungszentrum Jülich GmbH Mischkammer für einen Reformer sowie Verfahren zum Betreiben derselben
US7582790B2 (en) 2004-11-24 2009-09-01 Rohm And Haas Company Process for chemical reactions involving cyanohydrins
WO2006113883A2 (en) 2005-04-19 2006-10-26 Daniel Industries, Inc. Orifice flow meters
DE102006058250A1 (de) * 2006-12-08 2008-06-12 Evonik Röhm Gmbh Integriertes Verfahren und Vorrichtung zur Herstellung von Methacrylsäureestern aus Aceton und Blausäure
DE102006059511A1 (de) 2006-12-14 2008-06-19 Evonik Röhm Gmbh Verfahren zur Herstellung von Acetoncyanhydrin und dessen Folgeprodukten durch gezielte Kühlung

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3540853A (en) * 1967-06-03 1970-11-17 Titan Gmbh Means for producing titanium dioxide pigment
US5935490A (en) * 1996-07-26 1999-08-10 Boc Gases Australia Limited Oxygen dissolver for pipelines or pipe outlets
JP2000213681A (ja) * 1999-01-27 2000-08-02 Toshiba Corp 流体混合継手
US6969490B2 (en) * 2003-06-26 2005-11-29 3M Innovative Properties Company Device for the continuous process for the production of controlled architecture materials

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2015516379A (ja) * 2012-03-30 2015-06-11 エボニック レーム ゲゼルシャフト ミット ベシュレンクテル ハフツングＥｖｏｎｉｋ Ｒｏｅｈｍ ＧｍｂＨ アセトンシアンヒドリンの加水分解方法
RU2622428C2 (ru) * 2012-03-30 2017-06-15 Эвоник Рем ГмбХ Способ гидролиза ацетонциангидрина

Also Published As

Publication number Publication date
BRPI1014260B1 (pt) 2018-07-03
EP2421637A1 (de) 2012-02-29
HK1167360A1 (en) 2012-11-30
WO2010121882A1 (de) 2010-10-28
ES2424494T3 (es) 2013-10-02
US9169194B2 (en) 2015-10-27
US20130211140A1 (en) 2013-08-15
DE102009002592A1 (de) 2010-10-28
RU2538260C2 (ru) 2015-01-10
CN102395422A (zh) 2012-03-28
TWI498164B (zh) 2015-09-01
SA110310293B1 (ar) 2014-06-08
JP2016222679A (ja) 2016-12-28
JP2012524650A (ja) 2012-10-18
CN102395422B (zh) 2015-03-18
TW201111042A (en) 2011-04-01
EP2421637B1 (de) 2013-05-08
BRPI1014260A2 (pt) 2016-04-12
KR20120003460A (ko) 2012-01-10
RU2011147120A (ru) 2013-05-27
SG175776A1 (en) 2011-12-29

Similar Documents

Publication Publication Date Title
US9169194B2 (en) Metering ring
ES2470567T3 (es) Un tratamiento por destilación de cianhidrina de acetona y unos procedimientos para la preparación de ésteres de ácido metacr�lico y de productos subsiguientes
US8334399B2 (en) Method for producing acetone cyanohydrin and the subsequent products thereof by specific cooling
CN109225114B (zh) 一种带高效混合器的自循环列管反应装置及采用其的反应方法
US10273199B2 (en) Hydrolysis vessel used in a process for amidification of acetone cyanohydrin
US8586779B2 (en) Method for producing methacrylic alkyl esters by way of azeotropic distillation
MX2014011644A (es) Proceso para la hidrolisis de cianohidrina de acetona.
RU2567619C2 (ru) Однокамерный испаритель и его применение при химическом синтезе
AU2007327789B2 (en) Process for preparing cyanohydrins and their use in the preparation of alkyl esters of methacrylic acid
CN115814717A (zh) 一种连续酸解循环反应器及制备乙烯利的方法
US7850939B2 (en) Method for producing prussic acid
CN209576694U (zh) 一种带高效混合器的自循环列管反应装置
US20240269634A1 (en) Method for producing phosgene
KR101337202B1 (ko) 다발관 강하막 반응기 및 이를 이용한 젖산 고분자 제조방법
RU2568113C1 (ru) Способ производства метанола и установка для его осуществления
CN117342979A (zh) 一种α-羟基腈的生产方法及生产系统
JP2023550265A (ja) 転化時の逆混合の低減によるメチルメタクリレートおよび／またはメタクリル酸の改良された製造方法
WO2008100170A1 (fr) Procédé de fabrication de méthanol et installation correspondante
US20120004460A9 (en) Method for producing methacrylic acid

Legal Events

Date Code Title Description
AS Assignment

Owner name: EVONIK ROEHM GMBH, GERMANY

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:SARTORELLI, LORENZA;PERL, ANDREAS;GROPP, UDO;AND OTHERS;SIGNING DATES FROM 20110407 TO 20110419;REEL/FRAME:026940/0649

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION