EP1414781A1 - Procede de fabrication continue de 2-bromo-2-nitro-1,3-propane diol - Google Patents

Procede de fabrication continue de 2-bromo-2-nitro-1,3-propane diol

Info

Publication number
EP1414781A1
EP1414781A1 EP02754968A EP02754968A EP1414781A1 EP 1414781 A1 EP1414781 A1 EP 1414781A1 EP 02754968 A EP02754968 A EP 02754968A EP 02754968 A EP02754968 A EP 02754968A EP 1414781 A1 EP1414781 A1 EP 1414781A1
Authority
EP
European Patent Office
Prior art keywords
reaction
reaction zone
nitromethane
bromo
nitro
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.)
Withdrawn
Application number
EP02754968A
Other languages
German (de)
English (en)
Inventor
Günter Scherr
Thomas Bogenstätter
Jürgen HUFF
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.)
BASF SE
Original Assignee
BASF SE
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 BASF SE filed Critical BASF SE
Publication of EP1414781A1 publication Critical patent/EP1414781A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C201/00—Preparation of esters of nitric or nitrous acid or of compounds containing nitro or nitroso groups bound to a carbon skeleton
    • C07C201/06—Preparation of nitro compounds
    • C07C201/12—Preparation of nitro compounds by reactions not involving the formation of nitro groups

Definitions

  • the present invention relates to a process for the continuous preparation of 2-bromo-2-nitro-l, 3-propanediol, in which nitromethane is first reacted with formaldehyde and alkali metal hydroxide and then the reaction mixture obtained is reacted with bromine.
  • 2-bromo-2-nitro-l, 3-propanediol, or bronopol for short is an economically very important biocide that is used as a disinfectant and preservative in pharmaceuticals, toiletries, cosmetics and household products.
  • 2-Bromo-2-nitro-1,3-propanediol is usually prepared by bishydroxymethylation of nitromethane with formaldehyde in the presence of a base, giving the corresponding salt of 2-nitropropane-1,3-diol, which is obtained then reacted with bromine to give 2-bromo-2-nitropropane-1,3-diol (see scheme 1).
  • the first reaction step shown in Scheme 1 is usually carried out in an aqueous or an aqueous / alcoholic solvent with an alkali hydroxide or an alkali alcoholate, whereby a solution of the salt of 2-nitropropane-1,3-diol shown in Scheme 1 is obtained, which is obtained then gives a solution of the bromine, such as. B. in Rec. Trav. Chim. Pays Bas by Den Otter in volume 57 from 1938 on pages 13-24.
  • a fundamental problem is that 2-bromo-2-nitropropane-1,3-diol tends to decompose in alkaline.
  • both reaction steps are highly exothermic. Controlled reaction management is therefore important.
  • the methods of the prior art therefore usually only work with dilute solutions.
  • the present invention relates to a process for the continuous production of 2-bromo-2-nitro-1,3-propanediol, which is characterized in that
  • the aqueous reaction mixture obtained in i) is continuously removed from the first reaction zone and is then fed directly thereafter together with bromine with thorough mixing of at least one second cooled reaction zone, and
  • aqueous solutions or aqueous reaction mixtures are understood to mean those solutions / mixtures in which the solvent, water or a mixture of water and water-miscible inert organic solvents, water being the main constituent, ie at least 50 vol. -%, preferably at least 80% by volume and in particular at least 95% by volume.
  • Suitable water-miscible, inert solvents are -CC 4 alcohols such as methanol, ethanol, n-propanol, isopropanol, n-butanol and tert-butanol.
  • water is used as the solvent.
  • the reactants are mixed thoroughly in the cooled reaction zone.
  • Intensive mixing is also important in the second stage ii).
  • Mixing is preferably effected by feeding the liquid reactants to the first and preferably also the second reaction stage via devices which are suitable for the continuous mixing of liquids.
  • mixing of the reactants can also be achieved by metering the liquid reactants into the reactor while swirling the liquid streams, for example via two inlets for the liquid streams which are arranged in close proximity to one another. This procedure has proven particularly useful in laboratory and miniplant systems with reactor volumes (volumes of the respective reaction zone) ⁇ 1000 ml, preferably ⁇ 200 ml.
  • the devices for the continuous mixing of liquids can be jet mixers, static mixers as well as dynamic mixers.
  • Such mixers are known to those skilled in the art, e.g. B. from H.-j. Henzler, "Continuous Mixing of Fluids” in Ullmann's Encyclopedia of Industrial Chemistry, 5th ed. On CD-ROM, WILEY-VCH, 1997, Weinheim.
  • Static mixers are preferably used, as mixers with fixed internals, in particular in the case of tubular reactor geometries.
  • the static mixer can be an arrangement of several deflecting or baffle plates, fabric-like internals, for. B. coax mixers or the Sulzer types SMX, SMV, SMR, SMF or SMXL; or helical internals such as Kenics, Fix Mix, Llightnin or Hellax mixers or combinations of different static mixer types.
  • the geometry of the reaction zone is designed in such a way that it has essentially turbulent flow conditions.
  • the Use of tubular reactors, ie tubular reactors or tube bundle reactors, has proven to be particularly favorable.
  • these reactor shapes allow the high heat of reaction to be dissipated well.
  • the reaction tubes can have both circular and ellipsoidal cross sections.
  • the dimensions of the reactor are generally such that the ratio of the length of the reactor tube to the diameter is in the range from 100: 1 to 1,000,000: 1, preferably in the range from 100: 1 to 10,000: 1 and in particular in the range from 250: 1 to 1000 : 1 lies.
  • the tube diameter is to be understood as the mean value between the major and minor axes.
  • the tubes of the reactor can have a straight geometry. However, they can also have one or more curved tube segments, for example tube segments with a plurality of successive curvatures with an alternating direction of curvature.
  • the latter reactors are e.g. B. from WO 98/08602, to the disclosure of which reference is hereby made.
  • the reaction zones are cooled, i. H. they are equipped with cooling devices.
  • cooling devices Basically, all types of external cooling with cooling liquids are suitable, such as jacket cooling, coils or cooling baths arranged on the walls of the reactors. It is particularly favorable to design the reactors in the form of shell-and-tube heat exchangers. H. in the form of tube bundles which are washed by the liquid cooling medium.
  • all known cooling media in particular cooled brines or liquid ammonia, can be considered as liquid cooling media.
  • the tubular reactors have at least one mixing element in direct spatial proximity to the feeds for the liquid reactants.
  • the tubular reactors can also have other mixers, in particular static mixers, at other points on the reaction tubes.
  • the alkali metal hydroxide and the formaldehyde can be fed to the reaction zone as an aqueous solution which contains both components and as separate aqueous solutions.
  • the nitromethane can be fed to the reaction zone at one point or else at several points.
  • the nitromethane is always supplied via a device suitable for mixing liquids. This ensures intensive mixing of the nitromethane with the aqueous solutions of the other reactants or with the reaction mixture located in the reaction zone.
  • At least a portion of the nitromethane and the other liquid reactants are preferably fed in via two or three feeds arranged in direct proximity to one another and in close proximity to at least one mixing element. In the tubular reactor geometry preferred according to the invention, these are two or three feeds arranged at one end of the reactor tube. At this end there is also at least one device suitable for mixing liquids.
  • the feed provided for the nitromethane and the feed provided for the formaldehyde and alkali metal hydroxide form a nozzle with a central outlet and a second outlet arranged concentrically around this central outlet.
  • the shape of these outlets is of minor importance and can have circular or annular cross sections as well as ellipsoid cross sections.
  • the outlet openings of this nozzle are preferably dimensioned such that the ratio of their cross-sectional areas approximately corresponds to the material flows to be supplied through them.
  • the nitromethane will preferably be fed through the central outlet opening and the aqueous solution containing formaldehyde and alkali metal hydroxide via the outlet opening concentrically arranged about the mixing element of the reaction zone. This arrangement is particularly preferred in the case of the tubular reactor geometry preferred according to the invention.
  • FIG. 1 A particularly preferred embodiment of this special arrangement is shown in FIG. 1 for a tubular reaction space.
  • Alkali metal hydroxides suitable for the process according to the invention are in particular sodium hydroxide and potassium hydroxide.
  • Sodium hydroxide is particularly preferably used.
  • the concentration of alkali hydroxide and of formaldehyde in these aqueous solutions is preferably in the range from 10 to 50% by weight and in particular in the range from 15 to 30% by weight, based in each case the total weight of the solution. If it is supplied via a common solution, the total concentration of formaldehyde and alkali metal hydroxide is preferably 10 to 50% by weight and in particular 15 to 30% by weight, based on the total weight of the solution. Nitromethane is preferably fed as such to the first reaction zone.
  • the concentrations of formaldehyde and alkali hydroxide are preferably selected such that the concentration of nitromethane or its reaction product in the reaction mixture of the first reaction stage is in the range from 1 to 10 mol / 1, in particular in the range from, to the molar ratio of nitromethane, formaldehyde and alkali hydroxide 1.2 mol / 1 to 5 mol / 1 and particularly preferably in the range from 1.5 mol / 1 to 4 mol / 1.
  • the proportion of nitromethane in the total amount of the streams fed in is preferably about 60 g / 1 to 600 g / 1, in particular 7.5 g / 1 to 300 g / 1 and particularly preferably 90 g / 1 to 250 g / 1 or 5 , 3 vol% to 53 vol%, in particular 6.6 vol% to 26.5 vol% and particularly preferably 8.0 vol% to 22.1 vol%, based on the total volume of the material flow.
  • the reactants are added to the first reaction stage in approximately the amount required in accordance with the stoichiometry shown at the outset, an up to 10% excess of alkali metal hydroxide and formaldehyde, based on nitromethane, being possible, as well as a small difference in these components
  • Information on the stoichiometry of the reactants here and in the following should always be understood as molar information.
  • formaldehyde and alkali metal hydroxide are preferably used in at least an equimolar amount, based on nitromethane and preferably in a slight excess of preferably 0.5 to 10 mol% and in particular 2 to 7.5 mol%.
  • the molar ratio of formaldehyde to nitromethane is preferably in the range from 2.01: 1 to 2.2: 1 and in particular in the range from 2.05: 1 to 2.15: 1 and the molar ratio of alkali hydroxide to nitromethane in the range from 1 , 01: 1 to 1.1: 1 and in particular in the range from 1.02: 1 to 1.07: 1.
  • the reaction temperature in the first reaction zone is preferably kept below 40 ° C. by cooling the reaction zone.
  • the reaction in the first reaction zone takes place at temperatures in the range from 10 to 40 ° C. and particularly preferably in the range from 15 to 30 ° C. and especially in the range from 20 to 25 ° C.
  • the residence time of the reactants in the first reaction zone is very short and preferably not more than 3 minutes, e.g. B. 5 seconds to 3 minutes, in particular 10 seconds 1 minute, particularly preferably 10 seconds to .45 seconds and very particularly preferably 10 seconds to 30 seconds.
  • the solution of the alkali metal salt of 2-nitropropane-1,3-diol obtained in the first reaction zone is then fed directly to the second reaction stage, ie without intermediate storage.
  • the supply is preferably carried out together with bromine via at least one device suitable for mixing liquids. Static mixers are also preferred here.
  • the aqueous reaction mixture containing 2-bromo-2-nitropropane-1,3-diol is continuously taken from the second or, in the case of several reaction zones, the last reaction zone, and the product of value is isolated therefrom.
  • the second reaction zone preferably also has a tubular geometry. Accordingly, the second reaction zone is also preferably configured as a tube reactor or as a tube bundle reactor.
  • the aqueous reaction mixture and bromine obtained in reaction stage i) are preferably added via two introduction points located in spatial proximity, which in turn are located in direct spatial proximity to the mixing element.
  • An arrangement is also preferably selected here in which bromine and the aqueous reaction solution of stage i) via a nozzle with a first central outlet and a second outlet arranged concentrically around the central outlet via a device of the reaction zone, preferably the, which is suitable for mixing liquids Reactor tube is fed.
  • an arrangement is also used here, as explained for the supply of the reactants in stage i) and is shown, for example, in FIGS. 1 and 1a.
  • the bromine is preferably added via the central outlet and the aqueous reaction solution is added via the second outlet arranged in a ring around the central outlet.
  • the amount of bromine which is fed in in the second stage corresponds essentially to the required stoichiometry, with bromine also being able to be used here in a slight excess or small excess, which as a rule does not exceed 20 mol%.
  • the amount of nitromethane used is used as the basis for stoichiometry. It has proven to be advantageous if bromine is used at most in an equimolar amount, based on the nitromethane used, but in particular in a small deficit.
  • the molar ratio of bromine to the nitromethane used in the first stage is therefore preferably 1.8: 1 to 1.99: 1 and in particular 1.9: 1 to 1.95: 1.
  • the temperature of the reaction mixture in the second reaction zone is preferably below 40 ° C, z. B. in the range from 5 to 40 ° C, in particular in the range from 10 to 30 ° C and particularly preferably in the range from 15 to 25 ° C.
  • T he V erweilzeit of the reactants in the second reaction zone will preferably not exceed 3 minutes and preferably 10 seconds to 3 minutes, especially 10 seconds to 2 minutes and most preferably 15 seconds to 1 minute.
  • the second reaction zone resulting aqueous reaction mixture is generally as an aqueous solution of 2-B rom-2-nitro-l, 3-propanediol, and alkali metal bromide before.
  • the reaction mixture obtained is preferably cooled to temperatures below 5 ° C., in particular below 0 ° C., the lower temperature limit being limited by the solidification of the aqueous reaction mixture. It is preferably cooled to a temperature in the range from -10 to -2 ° C.
  • the 2-bromo-2-nitro-1,3-propanediol contained in the reaction solution crystallizes almost completely and can be filtered by customary methods.
  • the 2-bromo-2-nitro-1,3-propanediol will preferably be washed with small amounts of water and organic solvents. Subsequent drying then provides the 2-bromo-2-nitro-1,3-propanediol in a form which is sufficiently pure for most applications.
  • a further purification of the 2- B rom-2-nitro-l, 3-propanediol can be carried out by recrystallization, e.g. B. from water, alcohols, e.g. B.
  • C -C 4 alcohols such as methanol, E THANOL, n- and iso-propanol, ethers such as diethyl ether, diisopropyl carried pylether, methyl tert-butyl ether, chlorinated solvents and the like.
  • Additional 2-bromo-2-nitro-l, 3-propanediol can be concentrated by concentrating the reaction solution and performing the crystallization again and / or by salting out, preferably with alkali metal bromide or chloride, for.
  • B. NaBr or NaCl can be obtained.
  • the process according to the invention provides 2-bromo-2-nitro-l, 3-propanediol in a significantly higher yield based on nitromethane used as the discontinuous V of the article out of the art.
  • the selectivity, based on the nitromethane used is usually above 90% and in particular in the range from 95 to 99%.
  • the yield of 2-bromo-2-nitro-1,3-propanediol, based on the nitromethane used is generally above 80% of the theoretical yield and is often at least 85%. Accordingly, the formation of by-products is less.
  • the invention V is experienced economic, discontinuous because unlike the procedures do not have to be worked in a very dilute solution.
  • the space-time yield in the process according to the invention is very much higher, generally at least by a factor of 100, in particular at least 200, than in the batch processes of the prior art, so that quantities of product of value are produced with much smaller reactor volumes can be used for which much larger reactor volumes are required in the batch process. This increases the economic efficiency, since less material is required to build the plants.
  • the method according to the invention can be controlled very precisely. The use of organic solvents, as is required according to the literature in the prior art processes, is not necessary in the process according to the invention.
  • Figure 1 Representation of a preferred arrangement of a feed for reactants in a reaction tube
  • Figure la Schematic representation of one of several interconnected arrangements according to Figure 1
  • Figure 2 Flow chart of the continuous production of 2-bromo-2-nitro-l, 3-propanediol
  • FIG. 1 shows the cross section of a section of a tube bundle reactor with a reaction tube (1), into the end of which projects a second tube (2) with an outlet opening (3), the cross-sectional area of which is smaller than that of the reaction tube.
  • the outer wall of the tube (2) forms a second outlet opening (4) with the inner wall of the tube (1).
  • a static mixing element (7) for example an SMX Sulzer pack.
  • the tubes (1) and (2) are connected to chambers (5) and (6), not shown.
  • Arrow (A) symbolizes the inflow of aqueous formaldehyde and sodium hydroxide solution
  • arrow (B) the inflow of nitromethane.
  • Figure la shows a schematic representation of a section of a tube bundle arrangement which has several of the arrangements explained in Figure 1.
  • Several reaction tubes (1) with mixing elements (7) extend from a base (8).
  • Several tubes (2) extend from a base (9) and protrude into the tubes (1).
  • Base (9) forms with base (8) a chamber (5) which has feed lines for the supply of a reactant solution or a reactant.
  • Bottom (9) in turn forms a chamber (6) with hood (10) which has lines for a reactant or a reactant solution.
  • FIG. 2 shows a flow diagram of the production of 2-bromo-2-nitro-1,3-propanediol according to the invention.
  • a nitromethane stream (11) is fed via a chamber (6) into a tube bundle reactor R1.
  • the tube bundle reactor R1 has a plurality of reaction tubes with the arrangement explained in FIG. 1 or FIG.
  • An aqueous solution of sodium hydroxide (stream 12) and an aqueous formaldehyde solution (stream 13) are combined via a mixer (14) and fed into the reactor R1 via a chamber (5).
  • the reactor discharge (15) is moved directly into the reactor R2 via a chamber (5).
  • Reactor R2 has a reactor geometry comparable to reactor R1 with several of the arrangements explained in FIG.
  • Bromine (16) is fed into the reactor R2 via a chamber (6 ').
  • the discharge (17) from reactor R2 is then fed to the crystallization, not shown.
  • Both the reactor R1 and the reactor R2 are connected to a cooling system, not shown.
  • the first reaction tube had a length of 5000 mm and an inside diameter of 2 mm, corresponding to a reactor volume of approximately 15.7 ml.
  • the second reaction tube had a length of 3000 mm and an inside diameter of also 2 mm, corresponding to a reactor volume of 9.4 ml.
  • the first reaction tube had three liquid supply lines at one end. At its other end, it was connected to the beginning of the second reaction tube via a connection piece which had a feed line for a liquid. The free end of the second reaction tube led into a cooled receiver. Both the reaction tube (1) and the reaction tube (2) were cooled by means of cooling baths, so that a maximum reactor temperature of +30 ° C.
  • the template was cooled to -5 ° C.
  • the first reactor was fed 3.43 ml / min of a 20% strength by weight aqueous formaldehyde solution, 0.54 ml / min of nitromethane and 1. 8 ml / min of a 20% by weight sodium hydroxide solution. After a preliminary amount of about 50 ml, 0.51 ml / min of bromine were added by means of a Metrohm posimate via the feed line in the connecting piece of the two reactors.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

L'invention concerne un procédé de fabrication continue de 2-bromo-2-nitro-1,3-propane diol consistant I) à alimenter en continu dans une zone de réaction refroidie un mélange de nitrométhane et d'une ou deux solutions aqueuses contenant du formaldéhyde et de l'hydroxyde alcalin, avec des rapports molaires formaldéhyde sur nitrométhane de 1,9 : 1 à 2,2 : 1, et hydroxyde alcalin sur nitrométhane de 0,95 : 1 à 1,1 : 1 ; II) à prélever en continu le mélange réactif aqueux obtenu en I) dans la première zone de réaction et, immédiatement après, à alimenter celui-ci en continu avec du brome dans au moins une deuxième zone de réaction refroidie ; et, III) à isoler du 2-bromo-2-nitro-1,3-propane diol à partir du mélange réactif aqueux obtenu en II).
EP02754968A 2001-08-02 2002-08-01 Procede de fabrication continue de 2-bromo-2-nitro-1,3-propane diol Withdrawn EP1414781A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE10137829A DE10137829A1 (de) 2001-08-02 2001-08-02 Verfahren zur kontinuierlichen Herstellung von 2-Brom-2-nitro-1,3-propandiol
DE10137829 2001-08-02
PCT/EP2002/008595 WO2003011811A1 (fr) 2001-08-02 2002-08-01 Procede de fabrication continue de 2-bromo-2-nitro-1,3-propane diol

Publications (1)

Publication Number Publication Date
EP1414781A1 true EP1414781A1 (fr) 2004-05-06

Family

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Application Number Title Priority Date Filing Date
EP02754968A Withdrawn EP1414781A1 (fr) 2001-08-02 2002-08-01 Procede de fabrication continue de 2-bromo-2-nitro-1,3-propane diol

Country Status (7)

Country Link
US (1) US6867336B2 (fr)
EP (1) EP1414781A1 (fr)
JP (1) JP2004536151A (fr)
KR (1) KR20040029390A (fr)
CN (1) CN1237047C (fr)
DE (1) DE10137829A1 (fr)
WO (1) WO2003011811A1 (fr)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1295963C (zh) * 2004-12-29 2007-01-24 广州泰成生化科技有限公司 一种消毒剂
WO2009107133A1 (fr) * 2008-02-28 2009-09-03 Bromine Compounds Ltd. Procédé de préparation de bronopol
CN102627566A (zh) * 2012-03-21 2012-08-08 山东润鑫精细化工有限公司 一种固体碱催化制备溴硝醇的方法
CN108794307B (zh) * 2018-07-18 2022-11-11 山东道可化学有限公司 一种溶剂法合成4-溴-3-甲基苯甲醚的微反应系统和方法
CN113801024A (zh) * 2021-10-18 2021-12-17 天津长芦海晶集团有限公司 以氯化溴合成溴硝醇的方法

Family Cites Families (6)

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Publication number Priority date Publication date Assignee Title
US3534112A (en) 1967-11-13 1970-10-13 Commercial Solvents Corp Nitroalkanols from nitroalkanes and formaldehyde
NL170411C (nl) 1968-07-19 1982-11-01 Henkel Kgaa Werkwijze voor het bereiden van broomnitroalcoholen.
FR96391E (fr) * 1968-10-19 1972-06-16
BE757999A (fr) * 1969-10-28 1971-04-26 Henkel & Cie Gmbh Procede de preparation de bromonitro-alcools.
DE3814772A1 (de) * 1988-04-30 1989-11-09 Henkel Kgaa Aldolkondensation von nitroparaffinen
DE3814773A1 (de) * 1988-04-30 1989-11-09 Henkel Kgaa Verfahren zur bromierung von nitroalkoholen

Non-Patent Citations (1)

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Title
See references of WO03011811A1 *

Also Published As

Publication number Publication date
CN1538949A (zh) 2004-10-20
US20040186326A1 (en) 2004-09-23
DE10137829A1 (de) 2003-02-13
WO2003011811A1 (fr) 2003-02-13
KR20040029390A (ko) 2004-04-06
JP2004536151A (ja) 2004-12-02
CN1237047C (zh) 2006-01-18
US6867336B2 (en) 2005-03-15

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