DE1075103B - Process for the continuous production of epichlorohydrin from glycerine - Google Patents
Process for the continuous production of epichlorohydrin from glycerineInfo
- Publication number
- DE1075103B DE1075103B DENDAT1075103D DE1075103DA DE1075103B DE 1075103 B DE1075103 B DE 1075103B DE NDAT1075103 D DENDAT1075103 D DE NDAT1075103D DE 1075103D A DE1075103D A DE 1075103DA DE 1075103 B DE1075103 B DE 1075103B
- Authority
- DE
- Germany
- Prior art keywords
- epichlorohydrin
- hydrogen chloride
- glycerine
- dichlorohydrin
- continuously
- 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.)
- Pending
Links
- BRLQWZUYTZBJKN-UHFFFAOYSA-N epichlorohydrin Chemical compound ClCC1CO1 BRLQWZUYTZBJKN-UHFFFAOYSA-N 0.000 title description 12
- PEDCQBHIVMGVHV-UHFFFAOYSA-N glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 title description 12
- 235000011187 glycerol Nutrition 0.000 title description 10
- 238000000034 method Methods 0.000 title description 8
- 238000010924 continuous production Methods 0.000 title description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N HCl Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 19
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 17
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 17
- 239000007789 gas Substances 0.000 claims description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 4
- DEWLEGDTCGBNGU-UHFFFAOYSA-N 1,3-dichloropropan-2-ol Chemical compound ClCC(O)CCl DEWLEGDTCGBNGU-UHFFFAOYSA-N 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 12
- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 235000011116 calcium hydroxide Nutrition 0.000 description 5
- 239000000920 calcium hydroxide Substances 0.000 description 5
- 238000004821 distillation Methods 0.000 description 4
- 238000007127 saponification reaction Methods 0.000 description 4
- 230000005591 charge neutralization Effects 0.000 description 3
- 230000001264 neutralization Effects 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-N Carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000011541 reaction mixture Substances 0.000 description 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 2
- 238000005292 vacuum distillation Methods 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000015450 Tilia cordata Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 231100000078 corrosive Toxicity 0.000 description 1
- 231100001010 corrosive Toxicity 0.000 description 1
- 238000005755 formation reaction Methods 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 235000002639 sodium chloride Nutrition 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/02—Synthesis of the oxirane ring
- C07D301/24—Synthesis of the oxirane ring by splitting off HAL—Y from compounds containing the radical HAL—C—C—OY
- C07D301/26—Y being hydrogen
Description
Verfahren zur kontinuierlichen Herstellung von Epichlorhydrin aus Glyzerin Die Herstellung von Epichlorhydrin aus Glyzerin läßt sich über die folgenden Reaktionsstufen erreichen: 1. Dichlorhydrindarstellung aus Glyzerin und wasserfreier Salzsäure 2. Verseifung des Dichlorhydrins zum Epichlorhydrin mittels Kalkmilch Die Durchführung der Dichlorhydrindarstellung erfolgt dabei im allgemeinen in der Weise, daß man in Glyzerin, das auf 1000 C erhitzt wird, so lange wasserfreien Chlorwasserstoff einleitet, bis die Gewichtszunahme etwa 25 0/o über dem theoretischen Wert liegt. Den zur Umsetzung benötigten Chlorwasserstoff erhält man entweder durch Einwirkung von konzentrierter Schwefelsäure auf Kochsalz oder aber zweckmäßiger durch Umsetzung von Chlor mit Wasserstoff.Process for the continuous production of epichlorohydrin from glycerine The production of epichlorohydrin from glycerine can be achieved via the following reaction stages: 1. Dichlorohydrin preparation from glycerine and anhydrous hydrochloric acid 2. Saponification of dichlorohydrin to epichlorohydrin using milk of lime The preparation of dichlorohydrin is generally carried out in such a way that anhydrous hydrogen chloride is passed into glycerol, which is heated to 1000 ° C., until the increase in weight is about 25% above the theoretical value. The hydrogen chloride required for the reaction is obtained either by the action of concentrated sulfuric acid on common salt or, more expediently, by reacting chlorine with hydrogen.
Bei der oben geschilderten Arbeitsweise neutralisiert man das Reaktionsgemisch nach Beendigung der Chlorwasserstoffzugabe bei Raumtemperatur mit Soda, um überschüssigen Chlorwasserstoff zu binden. In the procedure outlined above, the reaction mixture is neutralized after completion of the addition of hydrogen chloride at room temperature with soda to reduce excess To bind hydrogen chloride.
Das gebildete Dichlorhydrin scheidet sich dabei als untere Schicht ab und kann nach Abtrennen und Nachwaschen mit Wasser durch fraktionierte Vakuumdestillation gereinigt werden. Das so erhaltene reine Dichlorhydrin wird mit Kalk oder Lauge zum Epichlorhydrin verseift.The dichlorohydrin formed separates out as a lower layer after separation and washing with water by fractional vacuum distillation getting cleaned. The pure dichlorohydrin thus obtained is treated with lime or lye saponified to epichlorohydrin.
In dieser Weise lassen sich zwar sehr reine End produkte in guter Ausbeute gewinnen. Das Verfahren ist jedoch verhältnismäßig umständlich. In this way, very pure end products can be converted into good Gain yield. However, the process is relatively cumbersome.
Es wurde nun gefunden, daß sich dieses Verfahren wesentlich vereinfachen und kontinuierlich gestalten läßt, wenn man durch auf 100 bis 1300 C erhitztes Glyzerin, das sich in einer unter schwachem Vakuum stehenden Destillationsapparatur befindet, einen lebhaften Strom von trocknem Chlorwasserstoff leitet. It has now been found that this process can be simplified considerably and can be designed continuously, if glycerine heated to 100 to 1300 C, which is located in a distillation apparatus under a weak vacuum, conducts a brisk stream of dry hydrogen chloride.
Hierbei bildet sich in gleicher Weise das gewünschte Dichlorhydrin. Durch das Arbeiten unter schwachem Vakuum destilliert das entstandene Dichlorhydrin sofort nach seiner Bildung fortlaufend als azeotropes Gemisch mit Wasser und überschüssigem Chlorwasserstoff ab. Auf diese Weise wird das Dichlorhydrin daran gehindert, weitere Reaktionen einzugehen, die zu unerwünschten Nebenprodukten führen und die Ausbeute verschlechtern.The desired is formed in the same way Dichlorohydrin. By working under a weak vacuum, the dichlorohydrin formed is distilled immediately after its formation continuously as an azeotropic mixture with water and excess Hydrogen chloride. In this way the dichlorohydrin is prevented from further Enter into reactions that lead to undesirable by-products and the yield worsen.
Es wurde weiterhin gefunden, daß sich das anfallende Azeotrop sehr vorteilhaft ohne Isolierung des reinen Dichlorhydrins zum Epichlorhydrin umsetzen läßt, wenn man das gesamte Destillat mit überschüssiger Kalkmilch verrührt, das Gemisch auf 40 bis 800 C erhitzt und das entstehende Epichlorhydrin im Vakuum laufend durch Destillation entfernt. Hierdurch ist es möglich, die umständliche Neutralisation, bei der erhebliche Mengen an Soda verbraucht werden, zu umgehen. Ein weiterer Vorteil besteht darin, daß die Vakuumdestillation des stark korrodierenden Dichlorhydrins wegfällt. It was also found that the resulting azeotrope is very convert advantageously without isolation of the pure dichlorohydrin to epichlorohydrin if the entire distillate is mixed with excess milk of lime, the Mixture heated to 40 to 800 C and the resulting epichlorohydrin running in vacuo removed by distillation. This makes it possible to eliminate the cumbersome neutralization, in which significant amounts of soda are consumed. Another advantage is that the vacuum distillation of the highly corrosive dichlorohydrin ceases to exist.
Neutralisation und Verseifung lassen sich ebenfalls kontinuierlich durchführen, wenn sie in einem liegenden Reaktionsgefäß in der Weise vorgenommen werden, daß Kalkmilch und rohes Dichlorhydringemisch fortlaufend gemeinsam an dem einen Ende des Rohres zufließen und in dem liegenden Gefäß unter Vakuum auf 40 bis 800 C erhitzt werden. Dabei geht das vorhandene Dichlorhydrin restlos in Epichlorhydrin über und destilliert am anderen Ende des Rohres fortlaufend ab, während die verbrauchte Kalkmilch über einen Siphon ebenfalls kontinuierlich ausgeschleust wird. Neutralization and saponification can also be carried out continuously perform if done in a lying reaction vessel in the manner be that milk of lime and raw dichlorohydrin mixture continuously together on the up one end of the tube and in the lying vessel under vacuum to 40 bis 800 C can be heated. The dichlorohydrin present is completely converted into epichlorohydrin over and continuously distilled at the other end of the tube while the consumed Lime milk is also continuously discharged via a siphon.
Schließlich wurde gefunden, daß an Stelle von reinem Chlorwasserstoffgas auch bei anderen Reaktionen anfallende Chlorwasserstoff enthaltende Abgase mit Erfolg Verwendung finden können. So läßt sich die Umsetzung beispielsweise ohne Schwierigkeit mit einem bei der Sulfochlorierung anfallenden Abgas, das durchschnittlich 60 bis 70 Volnmprozent Chlorwasserstoff, etwa 10 Volumprozent Schwefel dioxyd und 20 bis 30 Volumprozent Luft enthält, durchführen. Finally it was found that instead of pure hydrogen chloride gas also with other reactions containing accruing hydrogen chloride Exhaust gases can be used with success. So can the implementation for example without difficulty with a waste gas from the sulfochlorination process, which is average 60 to 70 percent by volume of hydrogen chloride, about 10 percent by volume of sulfur dioxide and Contains 20 to 30 percent air by volume.
Das in beiden Stufen kontinuierlich betriebene Verfahren ermöglicht es, in kleinen Reaktionsbehältem große Durchsätze zu erzielen. The process, which is operated continuously in both stages, enables it is possible to achieve high throughputs in small reaction vessels.
Das erfindungsgemäße Verfahren ist nachstehend an Hand der Zeichnung für die Verwendung Chlorwasserstoff enthaltender Abgase beschrieben. The method according to the invention is shown below with reference to the drawing for the use of exhaust gases containing hydrogen chloride.
In ein auf 110 bis 1200 C beheiztes und konstant zu etwa 60 Volumprozent mit Glyzerin gefülltes Reaktionsgefäß 1 wird bei einem Vakuum von 460 bis 560mm Hg laufend das 70 bis 80 Volumprozent Chlorwasserstoff enthaltende Abgas eingeleitet. Bei Einhaltung der Reaktionstemperatur von 110 bis 1200 C destilliert das gebildete Dichlorhydrin unter dem oben angegebenen Vakuum fortlaufend im Gemisch mit Reaktionswasser und überschüssigem Chlorwasserstoff bei etwa 1000 C ab und sammelt sich in der Vorlage 2. In a heated to 110 to 1200 C and constant to about 60 percent by volume Reaction vessel 1 filled with glycerine is operated at a vacuum of 460 to 560 mm Hg continuously introduced the exhaust gas containing 70 to 80 percent by volume of hydrogen chloride. If the reaction temperature of 110 to 1200 C is maintained, what is formed distills Dichlorohydrin continuously mixed with water of reaction under the vacuum indicated above and excess hydrogen chloride at about 1000 C and collects in the template 2.
Das anfallende Destillat hat im Durchschnitt folgende Zusammensetzung: 50 ovo Dichlorhydrin, 35 0/o Wasser, 15 0/o Chlorwasserstoff. The resulting distillate has the following composition on average: 50 ovo dichlorohydrin, 35% water, 15% hydrogen chloride.
In dem Maße wie das Reaktionsgemisch abdestilliert, wird aus dem Vorratsgefäß 3 laufend frisches Glyzerin zugeführt, so daß im Reaktionsgefäß immer die gleiche Fliissigkeitsmenge vorhanden ist. To the extent that the reaction mixture is distilled off, the Supply vessel 3 is continuously supplied with fresh glycerine, so that always in the reaction vessel the same amount of liquid is present.
Das erhaltene Destillat wird nun ohne Neutralisation und Destillation gemeinsam mit 10- bis 20ff/oiger Kalkmilch aus dem Vorratsbehälter4 bei 600 C und unter einem Vakuum von etwa 100 mm Hg kontinuierlich an einem Ende eines liegenden, mit Dampf beheizten Eisenrohres 5 eingeleitet. Das bei der Verseifung entstehende Epichlorhydrin destilliert dann bei 50 bis 600 C mit Wasser als konstant siedendes Gemisch am oberen Teil des anderen Rohrendes ab. Dieses Gemisch trennt sich in den Vorlagen 6. Die verbrauchte Kalkmilch fließt am gleichen Rohrende an der unteren Seite des Rohres in die Vorlagen 7 ab. The distillate obtained is now without neutralization and distillation together with 10- to 20ff / o lime milk from the storage container4 at 600 C and under a vacuum of about 100 mm Hg continuously at one end of a lying, steam-heated iron pipe 5 initiated. The resulting from the saponification Epichlorohydrin then distills at 50 to 600 C with water as a constant boiling point Mixture from the upper part of the other end of the pipe. This mixture separates into the Templates 6. The used milk of lime flows at the same end of the pipe at the lower one Side of the tube into the templates 7.
Das anfallende rohe Epichlorhydrin ist verhältnismäßig rein. In der Kolonne 8 wird es durch fraktionierte Destillation bei einem Vakuum von etwa 100 mm Hg gereinigt.The resulting crude epichlorohydrin is relatively pure. In the Column 8 is made there by fractional distillation at a vacuum of about 100 mm Hg purified.
PATENTANSPRtSCHE 1. Verfahren zur kontinuierlichen Herstellung von Epichlorhydrin aus Glyzerin durch Umsatz mit Chlorwasserstoff zum Dichlorhydrin und anschließende alkalische Verseifung, dadurch gekennzeichnet, daß man in auf 100 bis 1300 C erhitztes Glyzerin unter schwachem Vakuum fortlaufend Chlorwasserstoffgas einleitet, das dabei entstehende Dichlorhydrin als Azeotrop mit dem Re aktionswasser und dem nicht umgesetzten Chlorwasserstoff fortlaufend durch Destillation entfernt und das Destillat unmittelbar in einem Arbeitsgang mit Kalkmilch kontinuierlich neutralisiert und zum Epichlorhydrin verseift. PATENT CLAIMS 1. Process for the continuous production of Epichlorohydrin from glycerine by reaction with hydrogen chloride to dichlorohydrin and subsequent alkaline saponification, characterized in that in on Glycerine heated to 100 to 1300 C under a weak vacuum, continuously hydrogen chloride gas initiates the resulting dichlorohydrin as an azeotrope with the water of reaction and the unreacted hydrogen chloride is continuously removed by distillation and the distillate immediately in one operation with milk of lime continuously neutralized and saponified to epichlorohydrin.
Claims (1)
Publications (1)
Publication Number | Publication Date |
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DE1075103B true DE1075103B (en) | 1960-02-11 |
Family
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Family Applications (1)
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DENDAT1075103D Pending DE1075103B (en) | Process for the continuous production of epichlorohydrin from glycerine |
Country Status (1)
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DE (1) | DE1075103B (en) |
Cited By (30)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1285993B (en) * | 1966-03-08 | 1969-01-02 | Leuna Werke Veb | Process for the continuous production of epichlorohydrin |
WO2005021476A1 (en) | 2003-09-01 | 2005-03-10 | Spolek Pro Chemickou A Hutni Vyrobu, Akciova Spolecnost | Method of preparing dichloropropanols from glycerine |
WO2006020234A1 (en) * | 2004-07-21 | 2006-02-23 | Dow Global Technologies Inc. | Conversion of a multihydroxylated-aliphatic hydrocarbon or ester thereof to a chlorohydrin |
JP2007284447A (en) * | 2003-11-20 | 2007-11-01 | Solvay (Sa) | Method for producing dichloropropanol from glycerol which is finally formed by conversion of animal fat in producing biodiesel |
WO2008128011A2 (en) * | 2007-04-12 | 2008-10-23 | Dow Global Technologies Inc. | Conversion of a multihydroxylated-aliphatic hydrocarbon or ester thereof to a chlorohydrin |
JP2008540608A (en) * | 2005-05-20 | 2008-11-20 | ソルヴェイ(ソシエテ アノニム) | Epoxide production method |
DE102008007622A1 (en) | 2008-02-04 | 2009-08-06 | Biopetrol Industries Ag | Process for the preparation of epichlorohydrin from glycerol |
WO2010106085A1 (en) | 2009-03-20 | 2010-09-23 | Akzo Nobel N.V. | Process for the catalytic halogenation of a diol |
US7851558B2 (en) | 2005-11-12 | 2010-12-14 | Dow Global Technologies Inc. | Brominated butadiene/vinyl aromatic copolymers, blends of such copolymers with a vinyl aromatic polymer and polymeric foams formed from such blends |
US7930651B2 (en) | 2007-01-18 | 2011-04-19 | Research In Motion Limited | Agenda display in an electronic device |
US7939696B2 (en) | 2005-11-08 | 2011-05-10 | Solvay Societe Anonyme | Process for the manufacture of dichloropropanol by chlorination of glycerol |
US8067645B2 (en) | 2005-05-20 | 2011-11-29 | Solvay (Societe Anonyme) | Process for producing a chlorhydrin from a multihydroxylated aliphatic hydrocarbon and/or ester thereof in the presence of metal salts |
CN101654444B (en) * | 2004-07-21 | 2011-12-07 | 陶氏环球技术有限责任公司 | Conversion of multihydroxylated-aliphatic hydrocarbon or ester thereof to chlorohydrin |
US8124814B2 (en) | 2006-06-14 | 2012-02-28 | Solvay (Societe Anonyme) | Crude glycerol-based product, process for its purification and its use in the manufacture of dichloropropanol |
US8197665B2 (en) | 2007-06-12 | 2012-06-12 | Solvay (Societe Anonyme) | Aqueous composition containing a salt, manufacturing process and use |
CN101921175B (en) * | 2003-11-20 | 2012-07-25 | 索尔维公司 | Process for producing an organic compound |
US8236975B2 (en) | 2004-07-21 | 2012-08-07 | Dow Global Technologies Llc | Process for the conversion of a crude glycerol, crude mixtures of naturally derived multicomponent aliphatic hydrocarbons or esters thereof to a chlorohydrin |
US8258350B2 (en) | 2007-03-07 | 2012-09-04 | Solvay (Societe Anonyme) | Process for the manufacture of dichloropropanol |
US8273923B2 (en) | 2007-06-01 | 2012-09-25 | Solvay (Societe Anonyme) | Process for manufacturing a chlorohydrin |
US8304563B2 (en) | 2004-07-21 | 2012-11-06 | Dow Global Technologies Llc | Batch, semi-continuous or continuous hydrochlorination of glycerin with reduced volatile chlorinated hydrocarbon by-products and chloroacetone levels |
US8314205B2 (en) | 2007-12-17 | 2012-11-20 | Solvay (Societe Anonyme) | Glycerol-based product, process for obtaining same and use thereof in the manufacturing of dichloropropanol |
US8378130B2 (en) | 2007-06-12 | 2013-02-19 | Solvay (Societe Anonyme) | Product containing epichlorohydrin, its preparation and its use in various applications |
WO2013034612A1 (en) | 2011-09-09 | 2013-03-14 | Akzo Nobel Chemicals International B.V. | Process for the chlorination of a hydroxylated organic compound |
US8471074B2 (en) | 2007-03-14 | 2013-06-25 | Solvay (Societe Anonyme) | Process for the manufacture of dichloropropanol |
US8507643B2 (en) | 2008-04-03 | 2013-08-13 | Solvay S.A. | Composition comprising glycerol, process for obtaining same and use thereof in the manufacture of dichloropropanol |
US8536381B2 (en) | 2008-09-12 | 2013-09-17 | Solvay Sa | Process for purifying hydrogen chloride |
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0
- DE DENDAT1075103D patent/DE1075103B/en active Pending
Cited By (62)
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DE1285993B (en) * | 1966-03-08 | 1969-01-02 | Leuna Werke Veb | Process for the continuous production of epichlorohydrin |
WO2005021476A1 (en) | 2003-09-01 | 2005-03-10 | Spolek Pro Chemickou A Hutni Vyrobu, Akciova Spolecnost | Method of preparing dichloropropanols from glycerine |
JP2007504101A (en) | 2003-09-01 | 2007-03-01 | スポレク プロ ケミコー ア フツニ ビロブ アクシオバ スポレクノスト | Method for preparing dichloropropanol from glycerin |
JP2012025769A (en) * | 2003-11-20 | 2012-02-09 | Solvay (Sa) | Method for producing dichloropropanol from glycerol, the glycerol coming eventually from the conversion of animal fat in the manufacture of biodiesel |
US9663427B2 (en) | 2003-11-20 | 2017-05-30 | Solvay (Société Anonyme) | Process for producing epichlorohydrin |
JP2007284447A (en) * | 2003-11-20 | 2007-11-01 | Solvay (Sa) | Method for producing dichloropropanol from glycerol which is finally formed by conversion of animal fat in producing biodiesel |
US8415509B2 (en) | 2003-11-20 | 2013-04-09 | Solvay (Societe Anonyme) | Process for producing dichloropropanol from glycerol, the glycerol coming eventually from the conversion of animal fats in the manufacture of biodiesel |
CN101921175B (en) * | 2003-11-20 | 2012-07-25 | 索尔维公司 | Process for producing an organic compound |
JP2009007349A (en) * | 2003-11-20 | 2009-01-15 | Solvay (Sa) | Method for producing dichloropropanol from glycerol wherein the glycerol comes eventually from conversion of animal fat in biodiesel production |
JP2012051914A (en) * | 2003-11-20 | 2012-03-15 | Solvay (Sa) | Process for producing dichloropropanol from glycerol, the glycerol coming eventually from the conversion of animal fats in the manufacture of biodiesel |
US8404905B2 (en) | 2004-07-21 | 2013-03-26 | Dow Global Technologies Llc | Batch, semi-continuous or continuous hydrochlorination of glycerin with reduced volatile chlorinated hydrocarbon by-products and chloroacetone levels |
CN101654444B (en) * | 2004-07-21 | 2011-12-07 | 陶氏环球技术有限责任公司 | Conversion of multihydroxylated-aliphatic hydrocarbon or ester thereof to chlorohydrin |
WO2006020234A1 (en) * | 2004-07-21 | 2006-02-23 | Dow Global Technologies Inc. | Conversion of a multihydroxylated-aliphatic hydrocarbon or ester thereof to a chlorohydrin |
US8304563B2 (en) | 2004-07-21 | 2012-11-06 | Dow Global Technologies Llc | Batch, semi-continuous or continuous hydrochlorination of glycerin with reduced volatile chlorinated hydrocarbon by-products and chloroacetone levels |
EP2174925A1 (en) | 2004-07-21 | 2010-04-14 | Dow Global Technologies Inc. | Conversion of a multihydroxylated-aliphatic hydrocarbon or ester thereof to a chlorohydrin |
EP2181979A1 (en) | 2004-07-21 | 2010-05-05 | Dow Global Technologies Inc. | Conversion of a multihydroxylated aliphatic hydrocarbon or ester thereof to a chlorohydrin |
US8236975B2 (en) | 2004-07-21 | 2012-08-07 | Dow Global Technologies Llc | Process for the conversion of a crude glycerol, crude mixtures of naturally derived multicomponent aliphatic hydrocarbons or esters thereof to a chlorohydrin |
CN101654396B (en) * | 2004-07-21 | 2014-09-24 | 陶氏环球技术有限责任公司 | Conversion of a multihydroxylated-aliphatic hydrocarbon or ester thereof to a chlorohydrin |
JP2008545643A (en) | 2005-05-20 | 2008-12-18 | ソルヴェイ(ソシエテ アノニム) | Process for the preparation of chlorohydrin by reaction of polyhydroxylated aliphatic hydrocarbons with chlorinating agents. |
US8519198B2 (en) | 2005-05-20 | 2013-08-27 | Solvay (Societe Anonyme) | Method for making an epoxide |
US7906692B2 (en) | 2005-05-20 | 2011-03-15 | Solvay (Societe Anonyme) | Method for making a chlorohydrin by chlorinating a polyhydroxylated aliphatic hydrocarbon |
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WO2008128011A3 (en) * | 2007-04-12 | 2009-01-29 | Dow Global Technologies Inc | Conversion of a multihydroxylated-aliphatic hydrocarbon or ester thereof to a chlorohydrin |
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DE102008007622A1 (en) | 2008-02-04 | 2009-08-06 | Biopetrol Industries Ag | Process for the preparation of epichlorohydrin from glycerol |
EP2093221A1 (en) | 2008-02-04 | 2009-08-26 | Biopetrol Industries AG | Method for manufacturing epichlorohydrin from glycerine |
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