NO157450B - PROCEDURE FOR THE PREPARATION OF 1,2-DICHLORETHANE. - Google Patents
PROCEDURE FOR THE PREPARATION OF 1,2-DICHLORETHANE. Download PDFInfo
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- NO157450B NO157450B NO834801A NO834801A NO157450B NO 157450 B NO157450 B NO 157450B NO 834801 A NO834801 A NO 834801A NO 834801 A NO834801 A NO 834801A NO 157450 B NO157450 B NO 157450B
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- Prior art keywords
- catalyst
- dichloroethane
- mixture
- separated
- chlorination
- Prior art date
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- WSLDOOZREJYCGB-UHFFFAOYSA-N 1,2-Dichloroethane Chemical compound ClCCCl WSLDOOZREJYCGB-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 17
- 238000002360 preparation method Methods 0.000 title abstract description 3
- 239000003054 catalyst Substances 0.000 claims abstract description 36
- 239000000203 mixture Substances 0.000 claims abstract description 29
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 20
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000005977 Ethylene Substances 0.000 claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims abstract description 14
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000000460 chlorine Substances 0.000 claims abstract description 12
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 12
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 10
- 239000000047 product Substances 0.000 claims abstract description 9
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims abstract description 7
- 239000002904 solvent Substances 0.000 claims abstract description 7
- 238000004821 distillation Methods 0.000 claims abstract description 6
- 150000003839 salts Chemical class 0.000 claims abstract description 6
- 238000009835 boiling Methods 0.000 claims abstract description 4
- 239000007788 liquid Substances 0.000 claims abstract description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 12
- 229910052742 iron Inorganic materials 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 230000015572 biosynthetic process Effects 0.000 claims description 4
- 239000006227 byproduct Substances 0.000 claims description 4
- 239000003112 inhibitor Substances 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 239000000706 filtrate Substances 0.000 abstract description 2
- 239000003463 adsorbent Substances 0.000 abstract 3
- 239000002585 base Substances 0.000 description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 10
- SCYULBFZEHDVBN-UHFFFAOYSA-N 1,1-Dichloroethane Chemical class CC(Cl)Cl SCYULBFZEHDVBN-UHFFFAOYSA-N 0.000 description 6
- 238000007792 addition Methods 0.000 description 6
- 239000011541 reaction mixture Substances 0.000 description 6
- 229910021529 ammonia Inorganic materials 0.000 description 5
- UBOXGVDOUJQMTN-UHFFFAOYSA-N 1,1,2-trichloroethane Chemical compound ClCC(Cl)Cl UBOXGVDOUJQMTN-UHFFFAOYSA-N 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 3
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 3
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 3
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 2
- -1 alicyclic amine Chemical group 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 2
- 239000012429 reaction media Substances 0.000 description 2
- UOCLXMDMGBRAIB-UHFFFAOYSA-N 1,1,1-trichloroethane Chemical compound CC(Cl)(Cl)Cl UOCLXMDMGBRAIB-UHFFFAOYSA-N 0.000 description 1
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 125000003710 aryl alkyl group Chemical group 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- HRYZWHHZPQKTII-UHFFFAOYSA-N chloroethane Chemical compound CCCl HRYZWHHZPQKTII-UHFFFAOYSA-N 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 229960003750 ethyl chloride Drugs 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 229920000768 polyamine Chemical group 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/013—Preparation of halogenated hydrocarbons by addition of halogens
- C07C17/02—Preparation of halogenated hydrocarbons by addition of halogens to unsaturated hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
- C07C17/383—Separation; Purification; Stabilisation; Use of additives by distillation
Abstract
Fremgangsmåte til fremstilling av 1,2-dikloretan ved reaksjon av etylen med klor i et opplSsningsmiddel i nærvær av en katalysatorblanding bestående av vannfritt jern-III-klorid og en nitrogenbase, resp. et salt av denne base ved en temperatur under kokepunktet for 1,2-dikloretan og adskilles av 1,2-dikloretan, fra kloreringsblandingen hvor. a) kloreringsblandingen haes i en destilla-sonskolonne,fra blandingen avdestilleres 1,2-dikloretan inntil utskillelse av katalysatoren fra det flytende sump-produkt, fra sump-produktet adskilles den utskilte katalysator og sistnevnte anvendes på nytt til omsetning av etylen med klor eller b) kloreringsblandingen føres over et adsorb-sjonsmiddel, den i blandingen inneholdte katalysator adsorberes på adsorpsjonsmiddelet fra det dannede filtra^adskilles 1,2-dikloretan ved destillering, og katalysatoren gjenvinnes ved adsorbsjonsmiddelet eller c) det gåes frem tilsvarende a), imidlertid ved små katalysatorinn hold kasseres det. katalysatorholdige sump-produkt.Process for the preparation of 1,2-dichloroethane by reaction of ethylene with chlorine in a solvent in the presence of a catalyst mixture consisting of anhydrous iron-III chloride and a nitrogen base, resp. a salt of this base at a temperature below the boiling point of 1,2-dichloroethane and separated from 1,2-dichloroethane, from the chlorination mixture where. a) the chlorination mixture is carried out in a distillation column, 1,2-dichloroethane is distilled from the mixture until the catalyst is separated from the liquid swamp product, the separated catalyst is separated from the swamp product and the latter is used again to react ethylene with chlorine or b ) the chlorination mixture is passed over an adsorbent, the catalyst contained in the mixture is adsorbed on the adsorbent from the filtrate formed, 1,2-dichloroethane is separated by distillation and the catalyst is recovered by the adsorbent or c) it is carried out corresponding to a) team discarded it. catalyst-containing swamp product.
Description
Fremstillingen av 1,2-dikloretan ved omsetning av etylen med klor i 1,2-dikloretan som oppløsningsmiddel og reaksjonsmedium er kjent. Til aksellerering av kloraddisjonen anvender man som katalysator ved siden av kloridene fra elementene i det periodiske systems IV til VI-gruppe fremfor alt vannfritt jern-III-klorid eventuelt i nærvær av oksygen, da jern-III-kloridet er lett tilgjengelig og prisgunstig. Som hoved-saklig biprodukt fremkommer ved denne reaksjon 1,1,2-trikloretan ved substitusjon av dikloretan. The production of 1,2-dichloroethane by reacting ethylene with chlorine in 1,2-dichloroethane as solvent and reaction medium is known. To accelerate the chlorine addition, in addition to the chlorides from the elements in the IV to VI groups of the periodic system, anhydrous iron III chloride is used as a catalyst, possibly in the presence of oxygen, as iron III chloride is readily available and inexpensive. The main by-product produced by this reaction is 1,1,2-trichloroethane by substitution of dichloroethane.
Kloraddisjonen til etylen gjennomføres i teknikken, såvel ved reaksjonstemperaturer rundt 9 0°C, idet reaksjonsproduktet avdestilleres fra reaksjonsblandingen under utnyttelse av den frigjorte reaksjonsvarme som også ved lavere temperaturer på 30-60°C, som omtalt i Ullmann Encyklopadie der technischen Chemie, bind 9, 4. opplag, 1975, side 427. Reaksjonsvarme kan i sistnevnte tilfelle ikke anvendes for rektifikasjon av rådikloretan, men må som eksempelvis anført i DE-OS 19 05 517 bortføres ved ompumping av reaksjonsmediet over varmeutveksler. The chlorine addition to ethylene is carried out in the technique, both at reaction temperatures around 90°C, as the reaction product is distilled off from the reaction mixture using the released heat of reaction, as well as at lower temperatures of 30-60°C, as discussed in Ullmann Encyklopadie der technischen Chemie, volume 9 , 4th edition, 1975, page 427. In the latter case, reaction heat cannot be used for the rectification of crude dichloroethane, but must, as stated for example in DE-OS 19 05 517, be removed by re-pumping the reaction medium over a heat exchanger.
Det ved lavere temperaturer fremstilte rå katalysatorholdig dikloretan ble tidligere vanligvis fjernet fra reaksjonskaret og for fjerning av katalysatoren og det i råproduktet inneholdte hy^drogenklorid vasket med vann resp. vandige alkali-oppløsninger i kloretanet adskilles fra det vandige sjikt, The crude catalyst-containing dichloroethane produced at lower temperatures was previously usually removed from the reaction vessel and, to remove the catalyst and the hydrogen chloride contained in the crude product, washed with water or aqueous alkali solutions in the chloroethane are separated from the aqueous layer,
og opparbeides deretter på kjent måte destillativt. and is then worked up in a known manner by distillation.
Anvendelse av FeCl^ som katalysator ved addisjonskloreringen av etylen, er forbundet med visse ulemper. Således virker FeCl^ korrosivt i nærvær av vann overfor de metalliske materialer av reaktorer, kolonner eller varmeutvekslere, såvidt disse kommer i berøring med katalysatoren. Det til klorering normalt anvendte klor med teknisk renhetsgrad innholder alltid spor av fuktighet, dessuten oppstår alltid hydrogenklorid av uønskede bireaksjoner. The use of FeCl^ as a catalyst in the addition chlorination of ethylene is associated with certain disadvantages. Thus, FeCl^ acts corrosively in the presence of water towards the metallic materials of reactors, columns or heat exchangers, insofar as these come into contact with the catalyst. The technically pure chlorine normally used for chlorination always contains traces of moisture, and hydrogen chloride always results from unwanted side reactions.
Ifølge fremgangsmåten i DE-OS 31 48 450 kan den på grunn av FeCl-j som katalysator ved fremstilling av 1,2-dikloretan for-årsakede korrosjon nedsettes betraktelig i ikke-korrosjons-faste reaktorer, når man påfører FeCl3 katalysatorer bestemte tilsetninger. Dessuten ble det fastslått at disse tilsetninger også virker fordelaktig på biproduktdannelsen som derved nedsettes . According to the method in DE-OS 31 48 450, the corrosion caused by FeCl-j as a catalyst in the production of 1,2-dichloroethane can be considerably reduced in non-corrosion-resistant reactors, when certain additions are applied to FeCl3 catalysts. Furthermore, it was established that these additions also have a beneficial effect on by-product formation, which is thereby reduced.
Gjenstanden for DE-OS 31 48 450 er en katalysatorblanding, bestående av vannfritt jern-III-klorid samt en ytterligere blandingskomponent til fremstilling av 1,2-dikloretan ved reaksjon av etylen med klor i et oppløsningsmiddel ved normal- eller overtrykk, idet denne blanding er karakterisert ved at en ytterligere blandingskomponent er en med hensyn til jern-III-kloridmengden omtrent ekvivalent mengde av en nitrogenbase eller et salt av denne base. The subject of DE-OS 31 48 450 is a catalyst mixture, consisting of anhydrous ferric chloride and a further mixture component for the production of 1,2-dichloroethane by reaction of ethylene with chlorine in a solvent at normal or overpressure, this mixture is characterized in that a further mixture component is an approximately equivalent amount of a nitrogen base or a salt of this base with respect to the amount of iron III chloride.
Nitrogenbasen kan være NH^, et primært, sekundært eller tertiært alkyl-, aralkyl-, aryl- eller alicyklisk amin eller et polyamin. Saltet av nitrogenbasen er fortrinnsvis et halogensalt, eksempelvis ammoniumklorid. The nitrogenous base may be NH 3 , a primary, secondary or tertiary alkyl, aralkyl, aryl or alicyclic amine or a polyamine. The salt of the nitrogen base is preferably a halogen salt, for example ammonium chloride.
Den i DE-OS 31 48 450 omtalte katalysatorblanding egner seg spesielt for gjennomføring av kloreringen av etylen med forhøyet temperatur, idet etylenkloreringens reaksjonsvarme kan utnyttes således at den dannede del av 1,2-dikloretan avdrives dampformet fra reaksjonsblandingen. Katalysatoren forblir derved i reaksjonsblandingen således at det i alle tilfelle fra tid til annen må utligne små katalysatortap. The catalyst mixture mentioned in DE-OS 31 48 450 is particularly suitable for carrying out the chlorination of ethylene at an elevated temperature, as the reaction heat of the ethylene chlorination can be utilized so that the formed part of 1,2-dichloroethane is driven off in the form of steam from the reaction mixture. The catalyst thereby remains in the reaction mixture so that in all cases small catalyst losses must be compensated for from time to time.
I motsetning hertil utvaskes det kloreringsfremgangsmåter In contrast, chlorination processes are leaching
som drives under kokeområdet for 1,2-dikloretan, katalysatoren fra det dannede rå dikloretan eksempelvis med vann, which is operated below the boiling range for 1,2-dichloroethane, the catalyst from the crude dichloroethane formed, for example with water,
idet katalysatoren er oppløst i vaskevannet, således at det herved inntredende katalysatortap må utlignes ved tilset- as the catalyst is dissolved in the wash water, so that the resulting catalyst loss must be offset by adding
ning av frisk katalysator. ning of fresh catalyst.
Da de ved fremgangsmåte ifølge DE-OS 31 48 450 anvendte kata-lysatordannede komponenter i form av vanrifritt FeCl^ og en nitrogenbase reagerer i kloreringsblandingen til en også i små mengder høyvirksom katalysator, har det vist seg fordelaktig å tilbakevinne denne katalysator ved opparbeidelsen av kloreringsblandingen i avhengighet av dens konsentrasjon i kloreringsblandingen for å kunne anvende den igjen for reaksjon av etylen med klor. Egnede måter til opparbeidelse av over-nevnte katalysatorholdige kloreringsblanding formidles ved fremgangsmåten ifølge oppfinnelsen. As the catalyst-forming components used in the process according to DE-OS 31 48 450 in the form of anhydrous FeCl 2 and a nitrogen base react in the chlorination mixture to form a highly effective catalyst, also in small quantities, it has proven advantageous to recover this catalyst during the processing of the chlorination mixture depending on its concentration in the chlorination mixture to be able to use it again for the reaction of ethylene with chlorine. Suitable methods for preparing the above-mentioned catalyst-containing chlorination mixture are provided by the method according to the invention.
Oppfinnelsens gjenstand er en fremgangsmåte til fremstilling av 1,2-dikloretan ved reaksjon av etylen med klor i et opp-løsningsmiddel i nærvær av en katalysatorblanding bestående av vannfritt jern-III-klorid og en nitrogenbase resp. et salt av denne base samt eventuelt en inhibitor for å hindre biproduktdannelse ved en temperatur under kokepunktet av 1,2-dikloretan på 20-100°C og normal- eller overtrykk og adskillelse av 1,2-dikloretanet fra kloreringsblandingen, idet fremgangsmåten er karakterisert ved at man befordrer kloreringsblandingen i en destillasjonskolonne, avdestillerer fra blandingen 1,2-dikloretanet inntil utskillelse av katalysatoren fra det flytende sumpprodukt, adskiller fra sumppro-duktet den utskilte katalysator og anvender sistnevnte igjen til omsetning av etylen med klor. The object of the invention is a method for producing 1,2-dichloroethane by reacting ethylene with chlorine in a solvent in the presence of a catalyst mixture consisting of anhydrous iron III chloride and a nitrogen base or a salt of this base and possibly an inhibitor to prevent by-product formation at a temperature below the boiling point of 1,2-dichloroethane of 20-100°C and normal or positive pressure and separation of the 1,2-dichloroethane from the chlorination mixture, the method being characterized by advancing the chlorination mixture in a distillation column, distilling off the 1,2-dichloroethane from the mixture until the catalyst is separated from the liquid sump product, separating the separated catalyst from the sump product and using the latter again to react ethylene with chlorine.
I utøvelse av fremgangsmåten ifølge oppfinnelsen ble det fastslått at konsentrasjonen av FeCl^ i reaksjonsblandingen er å dimensjonere til 0,001 til ca. 0,5 vekt-%, spesielt 0,002 til 0,1 vekt-%, referert til oppløsningsmiddelmengden, mens mengden av nitrogenbase resp. dets salt skal være ekvivalent til FeCl^-mengden. In carrying out the method according to the invention, it was determined that the concentration of FeCl^ in the reaction mixture is to be dimensioned to 0.001 to approx. 0.5% by weight, in particular 0.002 to 0.1% by weight, referred to the amount of solvent, while the amount of nitrogen base resp. its salt should be equivalent to the amount of FeCl^.
Som oppløsningsmiddel har det som ved de tilsvarende kjente fremgangsmåter til fremstilling av 1,2-dikloretan vist seg egnet også i foreliggende tilfelle selve 1,2-dikloretan. As a solvent, 1,2-dichloroethane itself has also proved suitable in the present case, as in the corresponding known methods for the production of 1,2-dichloroethane.
Den ved fremgangsmåten ifølge oppfinnelsen anvendte katalysator er å betegne som teknisk fremskritt da ved hjelp av den pro-duktdannelsen uttrykkes resp. unngås sterkt med unntak av mindre mengder av 1,1,2-trikloretan og en tilsvarende liten mengde klorhydrogen. Dessuten forblir også ved lengere reak-sjonsvarighet reaksjonsoppløsningen lys, når den til kloreringsblandingen satte nitrogenbase eksempelvis er ammoniakk. En i løpet av reaksjonen eventuelt mørkfarget reaksjonsblanding lysner i graden for ammoniakktilsetning etter kort tid igjen. Endelig er det å fastslå at ved fremgangsmåten ifølge oppfinnelsen er omsetningen omtrent kvantitativ ved høyt rom/tids-utbytte. Dette resultat oppnås også ved katalysatorkonsentra-sjon på mindre enn 0,003 vekt-%, referert til FeCl-^. The catalyst used in the method according to the invention is to be described as technical progress, since by means of the product formation, resp. strongly avoided with the exception of smaller amounts of 1,1,2-trichloroethane and a correspondingly small amount of hydrogen chloride. Moreover, even with a longer reaction duration, the reaction solution remains light, when the nitrogen base added to the chlorination mixture is, for example, ammonia. A reaction mixture that may have been dark in the course of the reaction brightens after a short time again due to the addition of ammonia. Finally, it must be established that with the method according to the invention, the turnover is roughly quantitative with a high space/time yield. This result is also achieved with a catalyst concentration of less than 0.003% by weight, referred to FeCl-^.
Den ifølge oppfinnelsen meddelte tekniske lære til opparbeidelse av kloreringsblandingen var ikke nærliggende da det foran det måtte gå den erkjennelse at den til opparbeidelse bestemte kloreringsblanding ikke mer inneholder de angitte katalysatorkomponenter i form av FeCl^ og nitrogenbase, men at det katalytisk virksomme stoff er reaksjonsproduktet av FeCl^ og nitrogenbasen med hensyn til den katalytiske akti-vitet langt overskrider FeCl^. Forsåvidt viser det seg hensiktsmessig å tilbakevinne denne katalysatoren i motsetning til FeCl^ ved de vanlige fremgangsmåter. The technical teaching disclosed according to the invention for preparing the chlorination mixture was not obvious as it had to be preceded by the recognition that the chlorination mixture intended for preparation no longer contains the specified catalyst components in the form of FeCl^ and nitrogen base, but that the catalytically active substance is the reaction product of FeCl^ and the nitrogen base with regard to the catalytic activity far exceed FeCl^. It therefore proves appropriate to recover this catalyst in contrast to FeCl^ by the usual methods.
Fremgangsmåten ifølge oppfinnelsen kan eksempelvis gjennom-føres i den i DE-OS 24 27 045 omtalte slyngreaktor eller også enhver annen egnet reaktor. The method according to the invention can, for example, be carried out in the loop reactor mentioned in DE-OS 24 27 045 or any other suitable reactor.
Eksempel_l Example_l
En sylindrisk reaktor, hvis volum utgjorde ca. 25 m 3 ble A cylindrical reactor, whose volume was approx. 25 m 3 was
fylt med 20 000 liter 1,2-dikloretan, reaktorfyllingen blandet med 170 mg jern-III-klorid/kg 1,2-dikloretan. Dess-ble det til denne oppløsning satt ca. 600 liter ammoniakk. filled with 20,000 liters of 1,2-dichloroethane, the reactor filling mixed with 170 mg iron-III-chloride/kg 1,2-dichloroethane. Then, approx. 600 liters of ammonia.
Ved et trykk ved toppen av reaktoren på ca. 1,3 bar ble At a pressure at the top of the reactor of approx. 1.3 bar was
det i reaktoren pr. time innført 1,008 kg etylen og 2,540 kg klorgass som i tillegg inneholdt ca. 4 volum-% inerte gasser, that in the reactor per hour introduced 1,008 kg of ethylene and 2,540 kg of chlorine gas which additionally contained approx. 4 volume-% inert gases,
samt 8 m 3 luft. I tillegg ble kloreringsblandingen blandet med ca. 80 liter ammoniakk og 170 mg FeCl^ pr. time. as well as 8 m 3 of air. In addition, the chlorination mixture was mixed with approx. 80 liters of ammonia and 170 mg FeCl^ per hour.
Fra reaktoren ble det fjernet ca. 3,542 kg pr. time rå dikloretan tilført sumpen av en destillasjonskolonne. Det tilførte råprodukt hadde følgende sammensetning: From the reactor, approx. 3.542 kg per hour crude dichloroethane fed to the sump of a distillation column. The added raw product had the following composition:
(EDC = dikloretan, ETC = trikloretan). (EDC = dichloroethane, ETC = trichloroethane).
Kolonnen ble drevet med et svakt undertrykk (ca. 0,7 bar abs.) ved kolonnens topp. Fra reaksjonsblandingen ble det avdestillert 95% av det ønskede reaksjonsprodukt, idet det rensede 1,2-dikloretan har følgende sammensetning: The column was operated with a slight negative pressure (approx. 0.7 bar abs.) at the top of the column. 95% of the desired reaction product was distilled from the reaction mixture, the purified 1,2-dichloroethane having the following composition:
Kolonnens sump ble etter avkjøling ført gjennom et filter og filtrert. Filtratet ble for ytterligere opparbeidelse After cooling, the sump of the column was passed through a filter and filtered. The filtrate was for further processing
tilført en vakuum-kolonne. Den adskilte katalysator ble ut-tatt fra filteret under utelukkelse av luftfuktighet og til-ført en oppløsningsbeholder som var fylt med 1,2-dikloretan. I det ytterligere forløp av kloreringsprosessen ble den for reaksjonen nødvendige katalysatormengde tilsatt fra den gjenvunnede del, mens jern-III-klorid- og ammoniakk-tilfør-selen kunne stoppes. added to a vacuum column. The separated catalyst was removed from the filter under the exclusion of atmospheric moisture and added to a solution container which was filled with 1,2-dichloroethane. In the further course of the chlorination process, the amount of catalyst required for the reaction was added from the recovered part, while the iron III chloride and ammonia supply could be stopped.
Claims (1)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19823247988 DE3247988A1 (en) | 1982-12-24 | 1982-12-24 | METHOD FOR PRODUCING 1,2-DICHLORETHANE |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| NO834801L NO834801L (en) | 1984-06-25 |
| NO157450B true NO157450B (en) | 1987-12-14 |
| NO157450C NO157450C (en) | 1988-03-23 |
Family
ID=6181740
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO834801A NO157450C (en) | 1982-12-24 | 1983-12-23 | PROCEDURE FOR THE PREPARATION OF 1,2-DICHLORETHANE. |
Country Status (14)
| Country | Link |
|---|---|
| EP (1) | EP0112544A1 (en) |
| JP (1) | JPS59118725A (en) |
| AU (1) | AU560130B2 (en) |
| BR (1) | BR8307098A (en) |
| CA (1) | CA1227496A (en) |
| CS (1) | CS240987B2 (en) |
| DD (1) | DD215527A5 (en) |
| DE (1) | DE3247988A1 (en) |
| ES (1) | ES528324A0 (en) |
| HU (1) | HU195175B (en) |
| IN (1) | IN161724B (en) |
| NO (1) | NO157450C (en) |
| SU (1) | SU1299496A3 (en) |
| ZA (1) | ZA839523B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3347153A1 (en) * | 1983-12-27 | 1985-07-04 | Hoechst Ag, 6230 Frankfurt | METHOD FOR PRODUCING 1,2-DICHLORETHANE |
| DE4012529A1 (en) * | 1990-04-19 | 1991-10-24 | Wacker Chemie Gmbh | CATALYST SYSTEM AND METHOD FOR PRODUCING 1,2-DICHLORETHANE BY CHLORINATION OF ETHYLENES USING THIS CATALYST SYSTEM |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1768367B1 (en) * | 1968-05-06 | 1972-03-09 | Wacker Chemie Gmbh | Process for the production of 1,2-dichloroethane |
| BE736638A (en) * | 1968-08-05 | 1969-12-31 | ||
| US3691239A (en) * | 1969-05-05 | 1972-09-12 | Continental Oil Co | Process for purification of ethylene dichloride |
| DE3148450A1 (en) * | 1981-12-08 | 1983-06-16 | Hoechst Ag, 6230 Frankfurt | CATALYST MIXTURE AND METHOD FOR PRODUCING 1,2-DICHLORETHANE |
-
1982
- 1982-12-24 DE DE19823247988 patent/DE3247988A1/en not_active Withdrawn
-
1983
- 1983-12-05 IN IN1491/CAL/83A patent/IN161724B/en unknown
- 1983-12-08 CA CA000442868A patent/CA1227496A/en not_active Expired
- 1983-12-13 JP JP58233795A patent/JPS59118725A/en active Pending
- 1983-12-17 EP EP83112745A patent/EP0112544A1/en not_active Ceased
- 1983-12-22 CS CS839804A patent/CS240987B2/en unknown
- 1983-12-22 ZA ZA839523A patent/ZA839523B/en unknown
- 1983-12-22 DD DD83258474A patent/DD215527A5/en unknown
- 1983-12-22 ES ES528324A patent/ES528324A0/en active Granted
- 1983-12-22 SU SU833679916A patent/SU1299496A3/en active
- 1983-12-23 AU AU22894/83A patent/AU560130B2/en not_active Ceased
- 1983-12-23 NO NO834801A patent/NO157450C/en unknown
- 1983-12-23 HU HU834459A patent/HU195175B/en unknown
- 1983-12-23 BR BR8307098A patent/BR8307098A/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| ES8406991A1 (en) | 1984-09-16 |
| HU195175B (en) | 1988-04-28 |
| SU1299496A3 (en) | 1987-03-23 |
| CS240987B2 (en) | 1986-03-13 |
| EP0112544A1 (en) | 1984-07-04 |
| JPS59118725A (en) | 1984-07-09 |
| BR8307098A (en) | 1984-07-31 |
| NO157450C (en) | 1988-03-23 |
| AU560130B2 (en) | 1987-04-02 |
| DD215527A5 (en) | 1984-11-14 |
| IN161724B (en) | 1988-01-23 |
| AU2289483A (en) | 1984-06-28 |
| DE3247988A1 (en) | 1984-06-28 |
| CA1227496A (en) | 1987-09-29 |
| NO834801L (en) | 1984-06-25 |
| ES528324A0 (en) | 1984-09-16 |
| ZA839523B (en) | 1984-09-26 |
| CS980483A2 (en) | 1985-06-13 |
| HUT36766A (en) | 1985-10-28 |
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