NO173602B - PROCEDURE AND DEVICE FOR THE PREPARATION OF HIGH-PURE 1,2-DICHLORETHANE WITH CONSUMPTION HEAT RECOVERY - Google Patents
PROCEDURE AND DEVICE FOR THE PREPARATION OF HIGH-PURE 1,2-DICHLORETHANE WITH CONSUMPTION HEAT RECOVERY Download PDFInfo
- Publication number
- NO173602B NO173602B NO91913237A NO913237A NO173602B NO 173602 B NO173602 B NO 173602B NO 91913237 A NO91913237 A NO 91913237A NO 913237 A NO913237 A NO 913237A NO 173602 B NO173602 B NO 173602B
- Authority
- NO
- Norway
- Prior art keywords
- dichloroethane
- pressure relief
- static mixer
- gas
- ethylene
- Prior art date
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- WSLDOOZREJYCGB-UHFFFAOYSA-N 1,2-Dichloroethane Chemical compound ClCCCl WSLDOOZREJYCGB-UHFFFAOYSA-N 0.000 title claims description 37
- 238000000034 method Methods 0.000 title claims description 18
- 238000011084 recovery Methods 0.000 title claims description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 21
- 239000005977 Ethylene Substances 0.000 claims description 21
- 239000007789 gas Substances 0.000 claims description 19
- 230000003068 static effect Effects 0.000 claims description 18
- 238000006243 chemical reaction Methods 0.000 claims description 14
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 9
- 239000000460 chlorine Substances 0.000 claims description 9
- 229910052801 chlorine Inorganic materials 0.000 claims description 9
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 7
- 239000003054 catalyst Substances 0.000 claims description 6
- 239000007791 liquid phase Substances 0.000 claims description 5
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims description 4
- 239000002904 solvent Substances 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 3
- 230000008020 evaporation Effects 0.000 claims description 3
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 claims description 2
- 239000001257 hydrogen Substances 0.000 claims description 2
- 229910052739 hydrogen Inorganic materials 0.000 claims description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims description 2
- 238000011144 upstream manufacturing Methods 0.000 claims description 2
- 238000010438 heat treatment Methods 0.000 claims 1
- UBOXGVDOUJQMTN-UHFFFAOYSA-N 1,1,2-trichloroethane Chemical compound ClCC(Cl)Cl UBOXGVDOUJQMTN-UHFFFAOYSA-N 0.000 description 4
- 238000004821 distillation Methods 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- SCYULBFZEHDVBN-UHFFFAOYSA-N 1,1-Dichloroethane Chemical compound CC(Cl)Cl SCYULBFZEHDVBN-UHFFFAOYSA-N 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000001342 alkaline earth metals Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 238000004581 coalescence Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000010959 steel Substances 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
- C07C19/00—Acyclic saturated compounds containing halogen atoms
- C07C19/01—Acyclic saturated compounds containing halogen atoms containing chlorine
- C07C19/043—Chloroethanes
- C07C19/045—Dichloroethanes
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Description
Foreliggende oppfinnelse angår en fremgangsmåte for fremstilling av høyren 1,2-dikloretan med varmegjenvinning ved omsetning av etylen og klor i flytende 1,2-dikloretan i nærvær av en spesiell katalysator, hvorved uønskede andre klorerte produkter kun oppstår i uvesentlige mengder, slik at det dannede 1,2-EDC ikke må renses ved destillasjon. The present invention relates to a method for the production of high purity 1,2-dichloroethane with heat recovery by reacting ethylene and chlorine in liquid 1,2-dichloroethane in the presence of a special catalyst, whereby unwanted other chlorinated products only occur in insignificant quantities, so that formed 1,2-EDC must not be purified by distillation.
En innretning for gjennomføring av fremgangsmåten beskrives også. A device for carrying out the method is also described.
Den katalytiske anleiring av klor på etylen i 1,2-dikloretan som oppløsningsmiddel skjer i 3 trinn: The catalytic attachment of chlorine to ethylene in 1,2-dichloroethane as solvent takes place in 3 steps:
1. oppløsning av det gassformige klor i 1,2-dikloretan 1. dissolution of the gaseous chlorine in 1,2-dichloroethane
2. oppløsning av det gassformige etylen i 1,2-dikloretan 2. dissolution of the gaseous ethylene in 1,2-dichloroethane
3. omsetning av de oppløste reaktanter til 1,2-dikloretan. 3. reaction of the dissolved reactants to 1,2-dichloroethane.
Mens trinnene 1 og 3 forløper hurtig, forløper trinn 2, sannsynligvis på grunn av den kun lave oppløselighet av etylen i 1,2-dikloretan, langsomt, og er derfor det hastig-hetsbestemmende reaskjonstrinn. Av denne grunn har i den kjente teknikk 1,2-dikloretan fremstillingen vært gjennomført i reaktorer som består av en hovedreaktor med tilstrekkelig oppholdstid og en efterreaktor for fullstendig omsetning av etylen. While steps 1 and 3 proceed rapidly, step 2, probably due to the only low solubility of ethylene in 1,2-dichloroethane, proceeds slowly, and is therefore the rate-determining reaction step. For this reason, in the known technique, 1,2-dichloroethane production has been carried out in reactors consisting of a main reactor with sufficient residence time and an after-reactor for complete conversion of ethylene.
I henhold til det som er foreslått i EP-0 080 098 Bl (CÅ-1 221 708) blir klor og etylen gassformig omsatt i 1,2-dikloretan som oppløsningsmiddel i en dobbelsløyfereaktor med efterreaktor. I hovedreaktoren er det anordnet en med fyllegemer fylt blandesone for finfordeling av reaksjons-gassene. Reaksjonstiden angis med 1 til 15 timer. Rensingen av 1,2-dikloretan skjer i efterkoblede destillasjonskolloner. According to what is proposed in EP-0 080 098 B1 (CÅ-1 221 708), chlorine and ethylene are reacted in gaseous form in 1,2-dichloroethane as solvent in a double-loop reactor with an after-reactor. In the main reactor, there is a mixing zone filled with filler cells for fine distribution of the reaction gases. The reaction time is indicated by 1 to 15 hours. The purification of 1,2-dichloroethane takes place in downstream distillation columns.
For 1,2-dikloretan fremstilling foreslås det i EP-0 111 203 Al (TJS-A-4.774.373) en spesiell katalysator ved hvis anvendelse det kun oppstår lave korrosjonsangrep på stål-overflåtene i de angjeldende deler av innretningen. Denne spesielle katalysator består av vannfri tetraklorferrat (1-) hvis kation er et alkali- eller jordalkalimetall- eller et ammoniumion. For 1,2-dichloroethane production, a special catalyst is proposed in EP-0 111 203 Al (TJS-A-4,774,373) by the use of which only low corrosion attacks occur on the steel surfaces in the relevant parts of the device. This particular catalyst consists of anhydrous tetrachloroferrate (1-) whose cation is an alkali or alkaline earth metal or an ammonium ion.
Det forelå som følge av dette en oppgave i det å forandre de kjente arbeidsmetoder og innretninger på en slik måte at mengden av dannelsen av de totale klorerte biprodukter i 1,2-dikloretan ligger under en verdi på 500 ppm og der installasjoner både i forbindelse med en stor hoved- og en sidereaktor og også en destillativ biproduktseparering faller bort, og der reaksjonsentalpien kan stilles til disposisjon på variabel måte for andre prosesser. As a result, there was a task in changing the known working methods and devices in such a way that the amount of the formation of the total chlorinated by-products in 1,2-dichloroethane is below a value of 500 ppm and where installations both in connection with a large main and a side reactor and also a distillative by-product separation are omitted, and where the reaction enthalpy can be made available in a variable way for other processes.
Gjenstand for oppfinnelsen er i henhold til dette en fremgangsmåte for fremstilling av høyren 1,2-dikloretan med varmegjenvinning fra ekvimolare mengder av etylen og klor i 1,2-dikloretan som oppløsningsmiddel i nærvær av en tetraklorferrat (1-)-katalysator ved en temperatur på 75 til 200°C og et trykk på 1 til 15 bar i en reaksjonssone og der fremgangsmåten karakteriseres ved at man oppløser klorgassen i en forkoblet blandingssone i sirkulerende 1,2-dikloretan, omsetter med etylengassen i den efterkoblede reaksjonssone hvor etylgassen er i f indispergsf lytende fase med en boblediamter på maksimalt 2,0 mm, lar denne findispergsflytende fase gjennomstrømme reaksjonssonen med en hastigheten på 0,3 til 1 meter pr. sekund ved en oppholdstid på 2,5 til 25 sekunder, beregnet på den flytende fase, og derefter trekker av det dannede høyrene 1,2-dikloretan som gass via en trykkavlastningsfordamping. According to this, the subject of the invention is a method for producing high purity 1,2-dichloroethane with heat recovery from equimolar amounts of ethylene and chlorine in 1,2-dichloroethane as solvent in the presence of a tetrachloroferrate (1-) catalyst at a temperature of 75 to 200°C and a pressure of 1 to 15 bar in a reaction zone and where the method is characterized by dissolving the chlorine gas in an upstream mixing zone in circulating 1,2-dichloroethane, reacting with the ethylene gas in the downstream reaction zone where the ethyl gas is in f indispergsf solid phase with a bubble diameter of a maximum of 2.0 mm, allows this finely dispersed liquid phase to flow through the reaction zone at a rate of 0.3 to 1 meter per second. second at a residence time of 2.5 to 25 seconds, calculated on the liquid phase, and then withdraws the formed hydrogen 1,2-dichloroethane as gas via a pressure relief evaporation.
Fortrinnsvis holdes boblediameteren for etylengassen mindre enn 1,5 mm. Preferably, the bubble diameter for the ethylene gas is kept smaller than 1.5 mm.
Med oppfinnelsens fremgangsmåte angis det nu en meget enkel fremgangsmåte for fremstilling av høyren 1,2-dikloretan. Efter en trykkavlastningsfordamping blir den gassformige 1,2-dikloretan kondensert og oppnås i en renhet på mer enn 99,95 vekt-$. Som vesentlig biprodukt oppstår 1,1,2-trikloretan. Den ved kondensasjonen frisatte varme kan for eksempel utnyttes for destillasjon av 1,2-dikloretan som oppnås ved oksikloreringsmetoden. De ellers ved 1,2-dikloretan fremstilling i henhold til direkte kloreringsmetoden nødvendige destillasjonskolonner for separering av lettere kokende og høyere kokende bestanddeler, faller fullstendig bort ved oppfinnelsens fremgangsmåte. Derved spares både de til-svarende investeringsomkostninger og også driftsom-kostningene. Utbyttene av 1,2-dikloretan utgjør 99, 7%, beregnet på C2H4, og 99, 1%, beregnet på Cl2- With the method of the invention, a very simple method for the production of high-purine 1,2-dichloroethane is now specified. After a pressure relief evaporation, the gaseous 1,2-dichloroethane is condensed and obtained in a purity of more than 99.95% by weight. 1,1,2-trichloroethane occurs as a significant by-product. The heat released by the condensation can, for example, be used for the distillation of 1,2-dichloroethane, which is obtained by the oxychlorination method. The distillation columns otherwise required for 1,2-dichloroethane production according to the direct chlorination method for separating lower boiling and higher boiling components are completely eliminated by the method of the invention. This saves both the corresponding investment costs and also the operating costs. The yields of 1,2-dichloroethane amount to 99.7%, calculated on C2H4, and 99.1%, calculated on Cl2-
For oppfinnelsens fremgangsmåte er finfordelingen av etylengassen av avgjørende betydning. Det er ikke tilstrekkelig å dosere inn etylengassen i finfordelt form i 1,2-dikloretan da etylengassboblene hurtig vokser sammen til større bobler og reaksjonshastigheten derved synker i vesentlig grad. Derfor må man sørge for at man forhindrer sammenvoksingen til større etylengassbobler. Denne finfordeling av etylengassen oppnås i såkalte "statiske blandere" slik de er beskrevet i "Chemie-Ingenieur-Technik" 52 (1980), nr.4, side 285 til 291. For the method of the invention, the fine distribution of the ethylene gas is of decisive importance. It is not sufficient to dose the ethylene gas in finely divided form into 1,2-dichloroethane, as the ethylene gas bubbles quickly grow together into larger bubbles and the reaction rate thereby drops significantly. Therefore, care must be taken to prevent the coalescence of larger ethylene gas bubbles. This fine distribution of the ethylene gas is achieved in so-called "static mixers" as described in "Chemie-Ingenieur-Technik" 52 (1980), no. 4, pages 285 to 291.
Det angis videre en innretning for gjennomføring av den ovenfor beskrevne fremgangsmåte og denne karakteriseres ved at den består av en blander 1 med klortilførsel 11, en "statisk blander" 2 med etylentilførsel 5, en trykkavlastningsbeholder 3, en sirkulasjonspumpe 6 og en varmeveksler 7, hvorved blanderen 1, den "statiske blander" 2, trykkavlastningsbeholderen 3, sirkulasjonspumpen 6 og varmeveksleren 7 strømningsmessig er forbundet med hverandre og trykkavlastningsventilen 3 er forbundet med en kondensator via en struper 4 og der det fra kondensatoren 8 fører en produktledning 9 samt en avgassledning 10. A device for carrying out the method described above is also specified and this is characterized by the fact that it consists of a mixer 1 with chlorine supply 11, a "static mixer" 2 with ethylene supply 5, a pressure relief container 3, a circulation pump 6 and a heat exchanger 7, whereby the mixer 1, the "static mixer" 2, the pressure relief container 3, the circulation pump 6 and the heat exchanger 7 are flow-wise connected to each other and the pressure relief valve 3 is connected to a condenser via a throttle 4 and where from the condenser 8 a product line 9 and an exhaust gas line 10 lead.
Innretningen kan også karakteriseres ved at The device can also be characterized by
a) det anvendes en "statisk blander" 2 med skrå stegom-strømning, b) platene i den "statiske blander" 2 er hullet, slisset, takket og/eller bølget, c) platene danner meanderkanaler eller kanaler som krysser hverandre, d) det mellom den "statiske blander" 2 og trykkavlastningsbeholderen 3 er anordnet en trykkholder 12, e) trykkavlastningsbeholderen 3 er anordnet 8 til 12 meter over den "statiske blander" 2 i stedet for trykkholderen 12 . a) a "static mixer" 2 with inclined step flow is used, b) the plates in the "static mixer" 2 are perforated, slotted, notched and/or corrugated, c) the plates form meander channels or channels that cross each other, d) a pressure holder 12 is arranged between the "static mixer" 2 and the pressure relief container 3, e) the pressure relief container 3 is arranged 8 to 12 meters above the "static mixer" 2 instead of the pressure holder 12.
Det på denne måte i den "statiske blander" 2 forhøyede trykk forhindrer en koking av 1,2-dikloretan i reaksjonssonen da dette vil medføre en reduksjon av reaksjonshastigheten. In this way, the elevated pressure in the "static mixer" 2 prevents a boiling of 1,2-dichloroethane in the reaction zone, as this will result in a reduction of the reaction rate.
Fremgangsmåten og innretningen for fremstilling av høyren 1,2-dikloretan skal illustreres nærmere nedenfor under henvisning til den ledsagende tegning. The procedure and device for the production of the right 1,2-dichloroethane shall be illustrated in more detail below with reference to the accompanying drawing.
Trykkavlastningsbeholderen 3, varmeveksleren 7, blandesonen 1 samt den "statiske blander" 2 fylles med 1,2-dikloretan og innstilles ved hjelp av sirkulasjonspumpen 6 på en 1,2-dikloretanstrøm på 200 m<3> pr. time. Gjennom ledningen 11 doseres 2867 kg pr. time klorgass til blandingssonen 1. Blandingssonen 1 er tildannet som en blandedyse. Den med klorfylte 1,2-dikloretan inneholder 0,2 vekt-# NaFeCl4 som katalysator og strømmer til den "statiske blander" 2 til hvilken det doseres 1134 kg pr. time etylengass via ledningen 5. Som "statisk blander" 2 anvendes en 3 meter lang SMV-blander fra firma Sulzer, Winterthur/Schweiz, med bølgede plater som dannes åpne kanaler som krysser hverandre. The pressure relief container 3, the heat exchanger 7, the mixing zone 1 and the "static mixer" 2 are filled with 1,2-dichloroethane and set with the help of the circulation pump 6 to a 1,2-dichloroethane flow of 200 m<3> per hour. Through line 11, 2867 kg per hour chlorine gas to the mixing zone 1. The mixing zone 1 is designed as a mixing nozzle. The one with chlorine-filled 1,2-dichloroethane contains 0.2 wt-# NaFeCl4 as catalyst and flows to the "static mixer" 2 to which 1134 kg per hour ethylene gas via line 5. As "static mixer" 2, a 3 meter long SMV mixer from the company Sulzer, Winterthur/Switzerland, with corrugated plates that form open channels that cross each other is used.
Etylengassboblediameteren er 1,0 til 1,5 mm, 1,2-dikloretan gjennomstrømmer den "statiske blander" 2 med en hastighet på 0,4 meter pr. sekund. The ethylene gas bubble diameter is 1.0 to 1.5 mm, 1,2-dichloroethane flows through the "static mixer" 2 at a speed of 0.4 meters per minute. second.
Efter innstilling av de stasjonære tilstander i kondensatoren 8 oppvarmes 7,5 m<3> pr. time vann til 60°C, i varmeveksleren 7 oppvarmes ytterligere 20 m<3> pr.time vann til 96°C. 1,2-dikloretan kretsløpet drives ved 125°C under et trykk på 4 bar. Fra trykkavlastningsbeholderen 3 blir det dannede 1,2-dikloretan via en standard regulering gassformig ført til kondensatoren 8 via struperen 4. Pr. time trekkes det av 3997 kg 1,2-dikloretan gjennom ledningen 9. Via avgassledningen 10 fjernes ikke-kondenserbare gasser for forbrenning. After setting the stationary conditions in the condenser 8, 7.5 m<3> is heated per hour of water to 60°C, in the heat exchanger 7 a further 20 m<3> per hour of water is heated to 96°C. The 1,2-dichloroethane circuit is operated at 125°C under a pressure of 4 bar. From the pressure relief vessel 3, the formed 1,2-dichloroethane is fed via a standard regulation in gaseous form to the condenser 8 via the throttle 4. Per hour, 3997 kg of 1,2-dichloroethane is drawn off through the line 9. Via the exhaust line 10, non-condensable gases are removed for combustion.
Det produserte 1,2-dikloretan inneholder som klorerte forurensninger i tillegg The 1,2-dichloroethane produced also contains chlorinated pollutants
400 ppm 1,1,2-trikloretan 400 ppm 1,1,2-trichloroethane
50 ppm 1,1-dikloretan 50 ppm 1,1-dichloroethane
5 ppm 1,2-dikloretylen-trans 5 ppm 1,2-dichloroethylene-trans
Utbyttet var 99, 7% beregnet på C2H4The yield was 99.7% calculated on C2H4
99, 7% beregnet på Cl2. 99.7% calculated for Cl2.
Claims (9)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE4026282A DE4026282A1 (en) | 1990-08-20 | 1990-08-20 | METHOD AND DEVICE FOR THE PRODUCTION OF HIGH PURITY 1,2-DICHLORETHANE WITH HEAT RECOVERY |
Publications (4)
| Publication Number | Publication Date |
|---|---|
| NO913237D0 NO913237D0 (en) | 1991-08-19 |
| NO913237L NO913237L (en) | 1992-02-21 |
| NO173602B true NO173602B (en) | 1993-09-27 |
| NO173602C NO173602C (en) | 1994-01-05 |
Family
ID=6412550
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO913237A NO173602C (en) | 1990-08-20 | 1991-08-19 | Method and apparatus for producing highly pure 1,2-dichloroethane with simultaneous heat recovery |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0471987B1 (en) |
| JP (1) | JPH04261125A (en) |
| KR (1) | KR920004322A (en) |
| DE (2) | DE4026282A1 (en) |
| HU (1) | HU212465B (en) |
| MX (1) | MX9100732A (en) |
| NO (1) | NO173602C (en) |
| RU (1) | RU2015955C1 (en) |
| ZA (1) | ZA916491B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TW442449B (en) * | 1996-07-04 | 2001-06-23 | Hoechst Ag | Process for preparing 1,2-dichloroethane by direct chlorination |
| DE19910964A1 (en) * | 1999-03-12 | 2000-09-21 | Krupp Uhde Gmbh | Process for the production of ethylene dichloride (EDC) |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3146246A1 (en) * | 1981-11-21 | 1983-05-26 | Hoechst Ag, 6230 Frankfurt | METHOD FOR PRODUCING 1,2-DICHLORETHANE |
| DE3245366A1 (en) * | 1982-12-08 | 1984-06-14 | Hoechst Ag, 6230 Frankfurt | METHOD FOR PRODUCING 1,2-DICHLORETHANE |
| DE3445896C1 (en) * | 1984-12-15 | 1986-04-10 | Dynamit Nobel Ag, 5210 Troisdorf | Process for the continuous production of 1,2-dichloroethane |
-
1990
- 1990-08-20 DE DE4026282A patent/DE4026282A1/en not_active Withdrawn
-
1991
- 1991-07-20 DE DE91112153T patent/DE59100802D1/en not_active Expired - Lifetime
- 1991-07-20 EP EP91112153A patent/EP0471987B1/en not_active Expired - Lifetime
- 1991-08-16 ZA ZA916491A patent/ZA916491B/en unknown
- 1991-08-17 KR KR1019910014180A patent/KR920004322A/en not_active Application Discontinuation
- 1991-08-17 HU HU912749A patent/HU212465B/en not_active IP Right Cessation
- 1991-08-19 JP JP3206866A patent/JPH04261125A/en active Pending
- 1991-08-19 RU SU5001303/04A patent/RU2015955C1/en not_active IP Right Cessation
- 1991-08-19 NO NO913237A patent/NO173602C/en unknown
- 1991-08-19 MX MX9100732A patent/MX9100732A/en not_active IP Right Cessation
Also Published As
| Publication number | Publication date |
|---|---|
| DE4026282A1 (en) | 1992-02-27 |
| HU212465B (en) | 1996-07-29 |
| KR920004322A (en) | 1992-03-27 |
| RU2015955C1 (en) | 1994-07-15 |
| MX9100732A (en) | 1992-04-01 |
| NO913237D0 (en) | 1991-08-19 |
| HU912749D0 (en) | 1992-01-28 |
| ZA916491B (en) | 1992-05-27 |
| HUT58675A (en) | 1992-03-30 |
| DE59100802D1 (en) | 1994-02-17 |
| EP0471987B1 (en) | 1994-01-05 |
| JPH04261125A (en) | 1992-09-17 |
| NO913237L (en) | 1992-02-21 |
| EP0471987A1 (en) | 1992-02-26 |
| NO173602C (en) | 1994-01-05 |
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