CS217472B1 - Method of and apparatus for preparing aliphatic,cycloaliphatic and aromatic sulphenyl chlorides - Google Patents
Method of and apparatus for preparing aliphatic,cycloaliphatic and aromatic sulphenyl chlorides Download PDFInfo
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- CS217472B1 CS217472B1 CS515179A CS515179A CS217472B1 CS 217472 B1 CS217472 B1 CS 217472B1 CS 515179 A CS515179 A CS 515179A CS 515179 A CS515179 A CS 515179A CS 217472 B1 CS217472 B1 CS 217472B1
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- -1 aromatic sulphenyl chlorides Chemical class 0.000 title claims description 11
- 238000000034 method Methods 0.000 title claims description 9
- 125000001931 aliphatic group Chemical group 0.000 title claims description 8
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 31
- 239000000460 chlorine Substances 0.000 claims description 31
- 229910052801 chlorine Inorganic materials 0.000 claims description 31
- BWGNESOTFCXPMA-UHFFFAOYSA-N Dihydrogen disulfide Chemical compound SS BWGNESOTFCXPMA-UHFFFAOYSA-N 0.000 claims description 28
- 239000011541 reaction mixture Substances 0.000 claims description 21
- 238000006243 chemical reaction Methods 0.000 claims description 20
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims description 8
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 8
- VZGDMQKNWNREIO-UHFFFAOYSA-N tetrachloromethane Chemical compound ClC(Cl)(Cl)Cl VZGDMQKNWNREIO-UHFFFAOYSA-N 0.000 claims description 8
- 125000004432 carbon atom Chemical group C* 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 6
- FWMUJAIKEJWSSY-UHFFFAOYSA-N sulfur dichloride Chemical compound ClSCl FWMUJAIKEJWSSY-UHFFFAOYSA-N 0.000 claims description 6
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 4
- 125000000217 alkyl group Chemical group 0.000 claims description 3
- 125000003118 aryl group Chemical group 0.000 claims description 3
- 125000000753 cycloalkyl group Chemical group 0.000 claims description 3
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 claims description 3
- 125000000449 nitro group Chemical group [O-][N+](*)=O 0.000 claims description 3
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- NTNKNFHIAFDCSJ-UHFFFAOYSA-N (2-nitrophenyl) thiohypochlorite Chemical compound [O-][N+](=O)C1=CC=CC=C1SCl NTNKNFHIAFDCSJ-UHFFFAOYSA-N 0.000 claims description 2
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims description 2
- CYTYCFOTNPOANT-UHFFFAOYSA-N Perchloroethylene Chemical group ClC(Cl)=C(Cl)Cl CYTYCFOTNPOANT-UHFFFAOYSA-N 0.000 claims description 2
- 239000000654 additive Substances 0.000 claims description 2
- 239000003905 agrochemical Substances 0.000 claims description 2
- 239000000975 dye Substances 0.000 claims description 2
- 239000003960 organic solvent Substances 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims description 2
- 230000009257 reactivity Effects 0.000 claims description 2
- 125000001424 substituent group Chemical group 0.000 claims description 2
- 229950011008 tetrachloroethylene Drugs 0.000 claims description 2
- PXJJSXABGXMUSU-UHFFFAOYSA-N disulfur dichloride Chemical class ClSSCl PXJJSXABGXMUSU-UHFFFAOYSA-N 0.000 claims 1
- 239000010687 lubricating oil Substances 0.000 claims 1
- QNXSCOLRVLSJTE-UHFFFAOYSA-N tert-butyl thiohypochlorite Chemical compound CC(C)(C)SCl QNXSCOLRVLSJTE-UHFFFAOYSA-N 0.000 claims 1
- 238000011144 upstream manufacturing Methods 0.000 claims 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 238000001816 cooling Methods 0.000 description 2
- 238000009499 grossing Methods 0.000 description 2
- 238000013021 overheating Methods 0.000 description 2
- ODHAQPXNQDBHSH-UHFFFAOYSA-N Dicyclohexyl disulfide Chemical compound C1CCCCC1SSC1CCCCC1 ODHAQPXNQDBHSH-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
- 239000000314 lubricant Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
Vynález sia týká spósobu výroby alifatických, cykloalifatických a aromatických sulfenylchloridov obecného· vzorca IThe invention relates to a process for the preparation of aliphatic, cycloaliphatic and aromatic sulfenyl chlorides of the formula I
R-S-Cl (I) kde R je ,alkyl s priamym alebo rozvětveným refazcom s 3 až 12 atómiami uhlíka, cykloalkyl s 5 až 8 atómami uhlíka alebo fenyl, substituovaný v icxrlto-, meta- alebo para- poiohe elefctroakoeptórnym alebo elektr-odonórnym substituentom, například nitronskupinou al-eIbo metylovou skupinou, ako aj zariadenia pre uskutočnenie tohto spósobu. Dává možnost zabezpečit homogénne rozpustenie chlóru v reakčnej zmesi -ako aj udržovat jej optimálinu je-akčnú teplotu v priebehu reakcie, čo sa priatenifvo prejavuje predovšetkým v podstatnOm zvýšení výťažnosti procesu.RS-Cl (I) wherein R is, straight or branched chain alkyl of 3 to 12 carbon atoms, cycloalkyl of 5 to 8 carbon atoms, or phenyl, substituted with an ω-nitro-, meta-, or para-aromatic substituent with an electron-o-acceptor or an electron-donor substituent , for example, nitro or methyl, as well as devices for carrying out this method. It provides the possibility of ensuring a homogeneous dissolution of the chlorine in the reaction mixture - as well as maintaining its optimal temperature at the reaction temperature during the reaction, which in particular results in a substantial increase in the process yield.
-Dopoisial’ isa alifatické, cykloalifiati-cké a aromatické sulfenylohloridy technicky pripravujú tak, že sa chlóráciia příslušného diteulfi-du rozpuštěného v nepolárnom alif atickom, cykloalifatitekom, aromatiekom ,alebo -chlór-ovanom organidkom rozpúšťadle, ako například v n-hexáne, cyklohexáne, benzíne, perchlóretyléne -al-ebo v chloride uhliěitom suchým plynným dhlórom uskutečňuje tak, že sa -chlór zavádza d-o celého objemu reakčnej zmesi, miešanej obvyklým spósobom konvenčnýna typom naiešadla.Dopoisial isa aliphatic, cycloaliphatic and aromatic sulfenyl chlorides are technically prepared by chlorinating the appropriate di-sulfide dissolved in a nonpolar aliphatic, cycloaliphatic, aromatic, or chlorinated organic solvent such as n-hexane, cyclohexane The reaction is effected by the introduction of chlorine into the entire volume of the reaction mixture, stirred in a conventional manner by a conventional type of reagent.
Koncentrácáa dilsulfidu je 1 až 40 % hrnotnostných, množstvo chlóru k množstvu disulfidu je v molárnona pomere 1,0 až 1,3 :1. Optimáln-a re-akčná teplota sa pohybuje v m-edziach —15 °C až 40 °C. V priebehu reakcie sa reákčná zmes chladí v celom svojdm objeme naraz.The concentration of dilsulfide is 1 to 40% by weight, the amount of chlorine to the amount of disulfide is in a molar ratio of 1.0 to 1.3: 1. The optimum and reaction temperature is between -15 ° C and 40 ° C. During the reaction, the reaction mixture is cooled in all its volume at once.
Výroba Sa dosial’ Uskutečňuje v běžných násadových kotloch, vybavených dhladiacim plástem a lopatkovým miešadlom.Sa dosial ´ production takes place in conventional hatch boilers, equipped with a smoothing jacket and a paddle stirrer.
Nevýhodou doterajšej výroby je predovšetkým to, že sa plynný chlór -zavá-dza do celého objemu roztoku disulfiidu, resp. reakčnej zmesi, pričom vzniká vplyvem nedostatečného premiešania z hliadiska chlóru koncentračně nehomogenný roztok a vplyvem nevhodného spóisObu čhladeniia doohádza k lokálnym prehriatiam reakčnej zmesi.The disadvantage of the prior art is that chlorine gas is introduced into the entire volume of the disulfide solution and the disulfide solution. of the reaction mixture, whereby due to insufficient mixing from the chlorine point of view, a concentration-inhomogeneous solution is formed and due to an unsuitable method of smoothing, local overheating of the reaction mixture occurs.
DcfeledkOm toho je vytvánanie priaznivých pOdmien-ok pre vznik paralelných reakcií a nežiadúcieh vedJajších produfctov. Tým sa -podstatné znižujú výtažky žia-daného produktu.As a result, favorable conditions are created for parallel reactions and unwanted byproducts. Thus, the yields of the desired product are substantially reduced.
Tieto nevýhody odstraňuje podlá vynálezu spóteiob výroby alifatických, cykloalifatických a ar-omátických sulfenylchloridov Obecného vzorca IAccording to the invention, these disadvantages are overcome by methods of producing aliphatic, cycloaliphatic and aromatic sulfenyl chlorides of the general formula I
R - S - Cl (I) kde R je alkyl s priamym alebo rozvětveným reťazcom s 3 až 12 atomami uhlíka, cykloalkyl s 5 až 8 atómami uhlíka alebo fenyl, substituovaný v orto-, meta- alebo .para- polohe elektroakceptórnym alebo elektrodonorným sublstituentom, například nitro- skupinou alebo metylovou skupinou, chloráoiou diisulfiídov obecného vzorca IIR-S-Cl (I) wherein R is a straight or branched chain alkyl of 3 to 12 carbon atoms, cycloalkyl of 5 to 8 carbon atoms or phenyl, substituted in the ortho, meta- or para-position by an electroacceptory or electrodonorous sublstituent , for example, nitro or methyl, by chloroalysis of the diisulfides of the formula II
R _ s - S - R (II) kde R má horeuvedený výzrnam. Dilsulfidy sú rozpuštěné v nepolámam alifatickom, cykloalifátickom, aromatickom alebo chlórovanom arganiíckom razpúšfaidle, ako například v n-lhexáne, cýkloihexáne,. benzíne, percihlóretyléne, s výhodou v chloride uhiičiltam, o koncentrácii disulfidu 1 až 40 % hmotnostných. Ohlorácia sa uskutečňuje suchým plynným dhlórom poúžitom v molámom pomere k disulfidu 1,0 až 1,3 ku 1 pri teplote —15 °C až 40 °C. Celkové množstvo chlóru Sa zavádza postupné plynulým prúdom do chliadenej, cíirkulujúoej reakčnej zmesi, pričom sa drkulačný poměr reakčnej zmesi na jednotkové množstvo chlóru upraví nastavením rychlosti cirkulácie reakičnej zmesi a prúdenia plynného chlóru nia hodnotu, pri ktorej sa v priebehu reakcie teplota reakičnej zmesi pohybuje ešte v rozmédzí —15 °C až 40 °C.R_ s-S-R (II) where R has the above-mentioned meaning. The dilsulfides are dissolved in a non-polar aliphatic, cycloaliphatic, aromatic or chlorinated arganic razor, such as in n-hexane, cycloihexane. benzene, perchlorethylene, preferably in carbon tetrachloride, at a disulfide concentration of 1 to 40% by weight. The chlorination is carried out with a dry gaseous gas used in a molar ratio to the disulfide of 1.0 to 1.3 to 1 at a temperature of -15 ° C to 40 ° C. The total amount of chlorine is introduced in a continuous stream into the cooled, circulating reaction mixture, whereby the ratio of the reaction mixture to the unit amount of chlorine is adjusted by adjusting the circulation rate of the reaction mixture and the chlorine gas flow to a value at which range from -15 ° C to 40 ° C.
Zariadenie k uskutečňovaniu spósobu výroby je vytvořené tak, že reaktor, cirkulačně čerpadlo a výmenník tepla, spojené vzájemné cirkulačnýlm potrubím vytvárajú cirkulačný obvod, kterému je predrádený zásobník disulfidu, spojený svojím výstupným potrubím s reaktorem, ako i zásobník chlóru, 'ktorý je svojím výstupným potrubím napojený nia saciu stranu cirkulačného čerpadla. Výstupné potrubie z cirkulačného obvodu je napojené na cirkulačně potrubie za cirkulačným čerpadlem.The apparatus for carrying out the production method is designed such that the reactor, the circulation pump and the heat exchanger connected to each other through the circulation piping form a circulation circuit to which the disulfide reservoir is connected by its outlet pipeline to the reactor and chlorine reservoir which is its outlet pipeline. connected to the suction side of the circulation pump. The outlet pipe from the circulation circuit is connected to the circulation pipe downstream of the circulation pump.
SpótsOb aj zariádenie podlá vynálezu majú proti došila! známým technickým sposobom výroby sulfenylchloridov mnohé výhody. Tým, že sa chlór zavádza do reakčnej zmesi, jestvujiúcej v relativné tenkej cirkiulujúcej vrstvě, je zabezpečené, že sa zabráni vzniku jeho nehomogénneho roztoku a tiež lokálnym prehriatiam reakčnej zmesi. Přesnou kontrolou hodnot cirkulačného poměru reakčnej zmesi na jednotkové množstvo chlóru je tiež zabezpečené, že sla nepřekročí stanovený molárny poměr reagujúcich látek. To všétko prispievia k tomu, že v priebehu reakcie nedochádza k nežiádúcim paralelným reakciám a v dósledku toho sa podstatné zvyšuje výtažnosť technologického procesu.Both the device and the device according to the invention have anti-sewn! the known technical process for the production of sulfenyl chlorides has many advantages. By introducing chlorine into the reaction mixture existing in the relatively thin circulating layer, it is ensured that its inhomogeneous solution is prevented, as well as local overheating of the reaction mixture. By strictly controlling the circulating ratio values of the reaction mixture per unit amount of chlorine, it is also ensured that the salt does not exceed the determined molar ratio of the reactants. This all contributes to avoiding undesired parallel reactions during the reaction and consequently increases the yield of the process substantially.
Výhodou zariadenia podlá vynálezu je jeho jednoduchost, univerzálnost pokia! ide o výrobu roznych derivátov sulfenylchloridu a fakt, že je bez požiadaviek nia atypické aparáty. Podstatnou výhodou je tiež to, že dává možnost 1’ahkej kontroly priébéhu reakcie příslušnými meracími systémami, s pomocou ktorých sa dá, za aplikácie vhodných spatných vazieb, eventuálně automaticky udržovat optimálny reakčný režim.The advantage of the device according to the invention is its simplicity, versatility as far as possible. it is the production of various sulfenyl chloride derivatives and the fact that there are no atypical apparatuses without requirements. An important advantage is also that it gives the possibility to easily control the progress of the reaction by means of appropriate measuring systems, by means of which it is possible, where appropriate, to maintain an optimal reaction mode by applying suitable bad links.
Schématicky je zariadenie znázorněné na pripojenom výkrese.The device is schematically shown in the attached drawing.
Pri vlastnej prevádzke sa postupuje tak, že zo zásobníka 1 disulfidu potrubím 3 sa do reaktora 8 předloží roztok disulfidu vo vhodnom organiidkom rozpúštadle a spuistí sa cirkulačně čerpadlo 5. Roztok disulfidu obieha v cirkulačnom obvode cirkulačným potrubím 6, pričom s'a ochladzuje vo výmenníku 7 tepla. Po ochladení na žiadanú teplotu sia zavádza na saciu stranu cirkulačného čerpadla 5, potrubím 4 zo zásobníka 2 chlóru, cirfculujúcej reakčnej zmesi chlór. Doba privádzania chlóru je závislá od nastavenej hodnoty cirkulačného poměru reakčnej zmesi na jednotkové množstvo chlóru a na žiadanom mdárnoim pomere chlóru k disulfidu, Rýchlostou jého zavádzania sa nastavuje potřebný cirkulačný poměr reakčnej zmesi na jednotkové množstvo chlóru. Nakolko od tóhto poměru je závislá teplota drkulujúcej reakčnej zmesi, je nutné nastavit ho na hodnotu, pri ktorej je ešte možné odóberať použitým výmemníkom 7 tepla vznikajúce reafečné teplo v takám množstve, aby sa v priebehu reakcie nepřekročila optimálna reakčná teplota Po doreagovaní všetkého předloženého disulfidu sa zatvorí přívod chlóru a reakčný produkt sa vypúšfia z cirkulačného Obvodu potrubím 9 k ďaíišiemu spracovaniu.In the actual operation, a disulfide solution in a suitable organics solvent is introduced from the disulfide container 1 via line 3 into a reactor 8 and a circulating pump 5 is started into the reactor 8 and the disulfide solution is circulated through the circulation line 6 while cooling in the exchanger 7. heat. After cooling to the desired temperature, the chlorine is fed to the suction side of the circulation pump 5 via line 4 from the chlorine reservoir 2 of the circulating reaction mixture. The chlorine supply time depends on the set value of the circulation ratio of the reaction mixture per unit amount of chlorine and the desired standard ratio of chlorine to disulfide. The rate of introduction of the reaction mixture to the unit amount of chlorine is set at the rate of introduction. Since this ratio is dependent on the temperature of the crushing reaction mixture, it must be set to a value at which the heat exchanger 7 generated by the heat exchanger 7 can still be removed in such an amount that the optimum reaction temperature is not exceeded during the reaction. closes the chlorine feed and discharges the reaction product from the circulation circuit via line 9 for further processing.
Takto připravený sulfenylchlorid sa móže buď spotřebovat, alébo sa móže použit ku kontinuálnej výrobě ďalšiého isulfenyldhloridu, a to tak, že po doreagovaní disulfidu přívod chlóru sa nezatvorí, ale ďalej sa kontinuálně přidává do oirkulujúcej reakčnej zmesi roiztok disulfidu a kontinuálně sa zavádza suChý plynný Chlór, pričom sa na výťlačnej straně cirkulačného čerpadla nepřetržíte odoberá ekvivalentně -množstvo sulfenylohloridu.The sulphenyl chloride thus prepared can either be consumed or used for the continuous production of further isulfenyl chloride, so that, after the disulfide has reacted, the chlorine feed is not closed, but the disulfide solution is continuously added to the circulating reaction mixture and dry chlorine gas is continuously introduced. whereby an equivalent amount of sulfenyl chloride is withdrawn at the pressure side of the circulation pump.
K tomu účelu sa zariadenie doplní potřebnými konvenčnými meracími a regulačnými členmi.To this end, the equipment is supplemented with the necessary conventional measuring and control elements.
Příklad 1Example 1
Do reaktora 8 sa předložilo 330 kg 9,7 %něho roztoku dicyklohexyldisulflidu v chloride uhličitom a spuistilo sa čerpadlo 5 v drkulačnom obvode, pričom prietok cirkulujúcého roztoku disulfidu bol nastavený nia 2 m3/hód. Po ochladení roztoku dicyklobexyldiisulfidu n;a 5 °C začal sa na saciu stranu cirkulačného čerpadla privádzať suchý plynný chlór rýchlostou 2,208 m3/hod, čím bol vytvořený cirkulačný poměr 1 liter roztoku dicylklohexyldisulfidu ku 1,104 litea plynného Chlóru. Takto sa zavádzal plynný chlór póčasReactor 8 was charged with 330 kg of a 9.7% dicyclohexyldisulphide solution in carbon tetrachloride and the pump 5 in the crushing circuit was started, the flow rate of the circulating disulphide solution being set at 2 m 3 / h. After the dicyclobexyldisulphide solution was cooled to 5 ° C, dry chlorine gas was fed to the suction side of the circulation pump at a rate of 2.208 m 3 / h, creating a circulation ratio of 1 liter of dicylclohexyldisulfide solution to 1.104 liters of chlorine gas. Chlorine gas was introduced in this way
1,5 hod, čím sa celkove priviedio do reakičnej zmesi 10,5 kg chlóru, čo je 1,06 molámy pre•bytok na vložený diicyklohexyldisulfid. Teplota póčas oxidácie sa pohybovala v rozmédzí 0 °C až 5 °C. Analýzou výslednej reakčnej •zmesi sa zifetila 94 %-ná kanverzia dicyldohexyldisulfidu na cyklohexylsulifenylchlorid. Příklad 21.5 hours, thereby introducing a total of 10.5 kg of chlorine, which is 1.06 molar, into the reaction mixture into the loaded diicyclohexyldisulfide. The oxidation half-life temperature was in the range of 0 ° C to 5 ° C. Analysis of the resulting reaction mixture revealed a 94% conversion of dicyldohexyldisulfide to cyclohexylsuliphenyl chloride. Example 2
Do reaktora 8 sa .předložilo 225 kg 40 %ného roztoku biis-/o-niteofenyl/-idísu!fidu v Chloride uhličitom pri 40 °C. Na sadu stranu cirkulačného čerpadla 5 sa privádzaloReactor 8 was charged with 225 kg of a 40% solution of biis- (o-nitrophenyl) disulfide in carbon tetrachloride at 40 ° C. The side of the circulation pump 5 was fed to the set
5,07 1 roztdku disulfidu na 1 liter chlóru, oo je 1,3 molámy preíbytok chlóru na vložený disulfid. Výsledná reakčná teplota bola 36 °C. Analýzou získaného roztoku o-nitro-fenylsulfenylchloridu sa zistila 68 %-má konverzia disulfidu na sulďenylclhloríd.5.07 l of disulfide solution per liter of chlorine, i.e. 1.3 molar excess of chlorine per disulfide loaded. The resulting reaction temperature was 36 ° C. Analysis of the obtained o-nitro-phenylsulfenyl chloride solution showed a 68% conversion of disulfide to sulfenyl chloride.
Příklad 3Example 3
Do reaktora 8 sa předložilo 220 kg 8 %nebo roztoku diterebutýldisulfidu v n-hexáne pri —15 °C. Do roztoku sa zavádzalo 8 kg chlóru pri cirkulačnom pomere 1 liter roztoku disulfidu na 1,32 litr a chlóru, čo je 1,15 moiáimy prébyltok chlóru na vložený disulfid. Teplota sa pohybovala v rozanedzí —15 °C až —10°C. Konverzia diterebutýldisulfidu na tercbutylsulfenýlehlorid bola 76,5 %.Reactor 8 was charged with 220 kg of 8% or a solution of diterebutyl disulfide in n-hexane at -15 ° C. 8 kg of chlorine were introduced into the solution at a circulation ratio of 1 liter of disulfide solution to 1.32 liters and chlorine, which is 1.15 molar excess chlorine per disulfide loaded. The temperature was in the range of -15 ° C to -10 ° C. The conversion of diterebutyl disulfide to tert-butylsulfene chloride was 76.5%.
Vyseká reaktivita sulfenylchloridov icih vraďuje medzi dóležité medziprodukty pri výrobě > gumárenských chemikálií, farbív, agrochemikálií, přísad do mazacích olejov a pod. látek.The high reactivity of sulfenyl chlorides ranks among important intermediates in the manufacture of> rubber chemicals, dyes, agrochemicals, lubricant oil additives and the like. substances.
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Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CS515179A CS217472B1 (en) | 1979-07-24 | 1979-07-24 | Method of and apparatus for preparing aliphatic,cycloaliphatic and aromatic sulphenyl chlorides |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CS515179A CS217472B1 (en) | 1979-07-24 | 1979-07-24 | Method of and apparatus for preparing aliphatic,cycloaliphatic and aromatic sulphenyl chlorides |
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| Publication Number | Publication Date |
|---|---|
| CS217472B1 true CS217472B1 (en) | 1983-01-28 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CS515179A CS217472B1 (en) | 1979-07-24 | 1979-07-24 | Method of and apparatus for preparing aliphatic,cycloaliphatic and aromatic sulphenyl chlorides |
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| Country | Link |
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| CS (1) | CS217472B1 (en) |
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1979
- 1979-07-24 CS CS515179A patent/CS217472B1/en unknown
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