DE3643757C2 - - Google Patents
Info
- Publication number
- DE3643757C2 DE3643757C2 DE19863643757 DE3643757A DE3643757C2 DE 3643757 C2 DE3643757 C2 DE 3643757C2 DE 19863643757 DE19863643757 DE 19863643757 DE 3643757 A DE3643757 A DE 3643757A DE 3643757 C2 DE3643757 C2 DE 3643757C2
- Authority
- DE
- Germany
- Prior art keywords
- inert gas
- molecular sieve
- water
- desorption
- cooler
- 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.)
- Expired - Fee Related
Links
- 239000011261 inert gases Substances 0.000 claims description 22
- 239000002904 solvents Substances 0.000 claims description 17
- 239000011901 water Substances 0.000 claims description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001308 nitrogen Substances 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 239000003960 organic solvents Substances 0.000 description 1
- 239000012071 phases Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
- B01J20/16—Alumino-silicates
- B01J20/18—Synthetic zeolitic molecular sieves
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3408—Regenerating or reactivating of aluminosilicate molecular sieves
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3416—Regenerating or reactivating of sorbents or filter aids comprising free carbon, e.g. activated carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3483—Regenerating or reactivating by thermal treatment not covered by groups B01J20/3441 - B01J20/3475, e.g. by heating or cooling
Description
Die Erfindung bezieht sich auf ein Verfahren zur Rückgewinnung von Lösungsmitteln aus einer Adsorptions anlage, bei dem ein in einem Adsorber mit Aktivkohlefil ter adsorbiertes Wasser-Lösungsmittel-Gemisch durch aufgeheiztes Inertgas desorbiert, über ein Molekular sieb getrocknet, nach der Desorption der Adsorber durch über einen Kühler geführtes Inertgas gekühlt, das Molekularsieb mit noch heißem Inertgas regeneriert und die Aktivkohle wieder befeuchtet wird.The invention relates to a method for Recovery of solvents from an adsorption plant in which an in an adsorber with activated carbon ter adsorbed water-solvent mixture heated inert gas desorbed, via a molecular sieve dried after desorption of the adsorber cooled by inert gas passed through a cooler, the molecular sieve is regenerated with the inert gas still hot and the activated carbon is moistened again.
Derartige Rückgewinnungsverfahren, die überall dort Anwendung finden, wo bei der Verarbeitung von Farben, Klebern o. ä. Stoffen Lösungsmittel frei werden, sind beispielsweise aus der DE-OS 29 42 959 in der Weise bekannt, daß als sogenanntes Trägermedium ein in einem Kreislauf durch eine entsprechende Anlage ge führtes, inertes Gas Verwendung findet. Ein wesentlicher Nachteil dieses Verfahrens besteht deshalb auch darin, daß, bedingt durch das temperaturabhängig unterschied liche Adsorptions- und Desorptionsverhalten der einzelnen Stoffe in der gasförmigen Phase, keine saubere Trennung von Wasser und Lösungsmittel in einem System möglich ist, in welchem bereits eine Trocknung des umlaufenden Inertgasstromes im gasförmi gen Zustand mittels eines Molsiebs stattfindet und erst nach dieser Vortrocknung versucht wird, durch ein Kühlsystem wasserfreies Lösungsmittel zurückzuge winnen. Auch das aus der DE-OS 31 46 553 bekannte Verfahren zur Behandlung wasserhaltiger organischer Lösungsmittel weist einen ähnlich unzulänglichen Weg auf.Such recovery processes that are everywhere Find application where in the processing of colors, Glues or similar substances are free of solvents for example from DE-OS 29 42 959 in the way known that as a so-called carrier medium in a cycle through a corresponding system led, inert gas is used. An essential one The disadvantage of this method is therefore also that that, due to the temperature-dependent difference Liche adsorption and desorption behavior of the individual substances in the gaseous phase, none clean separation of water and solvent in a system is possible in which one Drying the circulating inert gas stream in gaseous form condition takes place using a molecular sieve and only after this predrying is tried through withdraw a cooling system of anhydrous solvent win. Also known from DE-OS 31 46 553 Process for the treatment of water-containing organic Solvent has a similarly inadequate Way on.
Diesen Nachteil der bekannten Systeme zu beseitigen und eine saubere Trennung von Lösemittel und Träger medium auf einfache und sichere Weise zu erzielen, ist daher Aufgabe der vorliegenden Erfindung.To eliminate this disadvantage of the known systems and a clean separation of solvent and carrier medium in a simple and safe way, is therefore an object of the present invention.
Gelöst wird diese Aufgabe dabei durch die im Patent anspruch 1 angegebenen verfahrenstechnischen Maßnahmen. Der einzige Unteranspruch stellt zudem eine bei gewissen Einsatzfällen sinnvolle Ergänzung des Verfahrensablaufs nach dem Hauptanspruch dar. This task is solved by the patent Claim 1 specified procedural measures. The only subclaim also applies to certain A practical addition to the process flow according to the main claim.
Die Zeichnungsfiguren 1 und 2 zeigen hierbei erläuternd je ein Verfahrensschema zu den beiden Patentansprüchen.The drawing figures 1 and 2 show explanatory a procedural scheme for each of the two claims.
Zur Trocknung des wiedergewonnenen Lösemittels aus einer Adsorptionsanlage ist im Verfahrens schema ein Verfahren dargestellt, in dem das Lösemittel in flüssiger Form durch ein Molsieb getrocknet wird. Hierdurch ist die Einhaltung eines Restwassergehalts von kleiner 0,1% sicherer möglich als in einem Ver fahren mit einer Trocknung des umlaufenden Inertgases. Der vorgesehne Verfahrensablauf gemäß Fig. 1 ist dabei folgender:To dry the recovered solvent from an adsorption system, a process is shown in the process scheme in which the solvent is dried in liquid form through a molecular sieve. This makes it easier to maintain a residual water content of less than 0.1% than in a process involving drying of the circulating inert gas. . One of the tendon process sequence shown in Figure 1 is as follows:
Das in der Anfangsphase der Desorption überwiegend aus Wasser bestehende Desorbat wird in dem Kühler 1 kondensiert und in einen Pufferbehälter 2 einge leitet. Nach dem Erreichen einer Inertgastemperatur von 70 bis 90° am Adsorberaustritt 5 b wird wasserarmes Kondensat in einen weiteren Pufferbehälter 4 geleitet und daran anschließend dieses Kondensat in flüssiger Form durch ein nachgeschaltetes Molekularsieb 6 ge trocknet und das Lösungsmittel auf diese Weise rück gewonnen.The desorbate consisting predominantly of water in the initial phase of the desorption is condensed in the cooler 1 and passed into a buffer container 2 . After reaching an inert gas temperature of 70 to 90 ° at the adsorber outlet 5 b , low-water condensate is passed into a further buffer tank 4 and then this condensate in liquid form is dried by a downstream molecular sieve 6 and the solvent is recovered in this way.
Zum Abschluß der Desorption wird zudem ein Teilstrom des noch heißen Inertgases am Kühler 1 vorbeigeführt und zur Regeneration durch das Molekularsieb 6 geleitet und danach der aus dem Molekularsieb 6 austretende, mittlerweile gekühlte, wasserenthaltende Inertgasteil strom T 2 über einen Befeuchter 7 geleitet, der mit dem zu Beginn der Desorption im Pufferbehälter 2 gesammelten Wasser-Lösungsmittel-Gemisch gespeist und in den Adsorber 5 zur Befeuchtung der Aktivkohle 5 a geleitet wird, wobei im Befeuchter vorrangig die Restlösemittel ausgetrieben werden und eine zusätz liche Wasserverdunstung stattfindet.At the end of the desorption, a partial stream of the still hot inert gas is also led past the cooler 1 and passed through the molecular sieve 6 for regeneration and then the now cooled, water-containing inert gas part T 2 emerging from the molecular sieve 6 is passed via a humidifier 7 , which with the fed at the beginning of the desorption in the buffer tank 2 collected water-solvent mixture and passed into the adsorber 5 for moistening the activated carbon 5 a , the residual solvent being primarily driven off in the humidifier and an additional water evaporation taking place.
Sobald die erforderliche Wassermenge aus dem Kreis lauf abgezogen und auf die Kohle 5 a gebracht ist, gilt der Desorptionsvorgang als beendet.As soon as the required amount of water is withdrawn from the circuit and brought to the coal 5 a , the desorption process is considered to be complete.
Der Einsatz von Kühler 1 und Lösemitteltrockner, also Molsieb 6 in der angegebenen Form, gewährleistet eine optimale Anpassung des Systems der Desorption an geänderte Betriebsverhältnisse, wie z. B. stärkere Feuchtigkeit bei gleichzeitig geringerem Restwasser gehalt des Lösemittels, o. dgl. Da es hierbei auch Einsatzfälle geben kann, bei denen Druck- und Tempe raturabfall im Adsorber so hoch sind, daß vor allem das Temperaturniveau für eine einwandfreie Regeneration des Molsiebs 6 nicht mehr ausreicht, ist gemäß der Alternativlösung in Fig. 2 vorgesehen, daß zum Abschluß der Desorption der vom Adsorber 5 austretende, erwärmte Inertgasteilstrom T 1 zur besseren Regeneration des Molekularsiebs 6 nacherhitzt wird, wobei ein Gasteil strom T 3 bereits vor dem Nacherhitzer 10 am Moleku larsieb 6 vorbei direkt zum Vorkühler 1 a geht, und daß der aus dem Molekularsieb 6 austretende Inertgas teilstrom T 4 zusammen mit dem Teilstrom T 3 über den Kühler 1 a, 1 b zum Befeuchter 7 geleitet wird.The use of cooler 1 and solvent dryer, i.e. molecular sieve 6 in the specified form, ensures an optimal adaptation of the desorption system to changed operating conditions, such as. B. stronger moisture with lower residual water content of the solvent, o. The like. Since there may also be cases in which pressure and temperature drop in temperature in the adsorber are so high that especially the temperature level for proper regeneration of the molecular sieve 6 is not 2 is sufficient that, according to the alternative solution in FIG. 2, the heated inert partial stream T 1 emerging from the adsorber 5 is reheated for better regeneration of the molecular sieve 6 , with a partial gas stream T 3 already before the reheater 10 at the molecule larsieb 6 passes directly to the pre-cooler 1 a, and that the emerging from the molecular sieve inert gas partial flow 6 T 4 together with the partial stream T 3 through the cooler 1 a, 1 b to the humidifier 7 is passed.
Aus den beiden Verfahrensskizzen weiterhin noch er sichtliche Kurz-Bezeichnungen und Positionsangaben, die in Ansprüchen und der Beschreibung nicht gesondert erwähnt sind, weil sie zum Stand der Technik eines solchen Anlagenaufbaus gehören, sind im ebenfalls zur Anmeldung gehörenden Bezugsziffernverzeichnis definiert. From the two procedural sketches, he still continues visible short names and position information, not separately in the claims and the description are mentioned because they are part of the state of the art belong to such plant construction are also reference number register for registration Are defined.
BezugsziffernverzeichnisList of reference numbers
1 a Vorkühler
1 b Kondensator
2 Pufferbehälter für Wasser mit Lösungsmittelanteil
3 Inertgaskreislauf mit Erhitzer
4 Pufferbehälter für Lösungsmittel mit Restwasseranteil
5 Adsorber
5 a Kohlefilter
5 b Adsorberaustritt
6 Molsieb
7 Befeuchter
7 a Raschig-Ringe-Schüttung
8 Drosselklappe
9 Ventilator
9 a Ventilator
10 Zusatzerhitzer
11 Rückschlagklappe
12 Absperrventil 1 a precooler
1 b capacitor
2 buffer tanks for water with solvent content
3 Inert gas circuit with heater
4 buffer tanks for solvents with residual water
5 adsorbers
5 a carbon filter
5 b Adsorber outlet
6 molecular sieves
7 humidifiers
7 a Raschig rings fill
8 throttle valve
9 fan
9 a fan
10 additional heaters
11 check valve
12 shut-off valve
LM Lösemittel
N Stickstoff
REG Reingas
ROG Rohgas
W Wasser
T 1 Inertgasteilstrom (heiß)
T 2 Inertgasteilstrom (gekühlt)
T 3 Inertgasteilstrom (erwärmt)
T 4 Inertgasstrom (gekühlt) LM solvent
N nitrogen
REG clean gas
ROG raw gas
W water
T 1 inert gas partial flow (hot)
T 2 inert gas partial flow (cooled)
T 3 inert gas partial flow (heated)
T 4 inert gas stream (cooled)
Claims (2)
- a) das in der Anfangsphase der Desorption überwie gend aus Wasser bestehende Desorbat in dem Kühler (1) kondensiert und in einen Pufferbe hälter (2) eingeleitet wird,
- b) ab Erreichen einer Inertgastemperatur von 70 bis 90° am Adsorberaustritt (5 b) wasserarmes Kondensat in einen weiteren Pufferbehälter (4) geleitet wird und anschließend dieses Kondensat in flüssiger Form durch ein nachge schaltetes Molekularsieb (6) getrocknet und das Lösungsmittel rückgewonnen wird,
- c) zum Abschluß der Desorption ein Teilstrom (T 1) des noch heißen Inertgases am Kühler (1) vorbeigeführt und zur Regeneration durch das Molekularsieb (6) geleitet wird, und dann der aus dem Molekularsieb (6) austretende, mittlerweile gekühlte, wasserenthaltende Inertgasteilstrom (T 2) über einen Befeuchter (7), der mit dem zu Beginn der Desorption im Pufferbehälter (2) gesammelten Wasser- Lösungsmittel-Gemisch gespeist wird, in den Adsorber (5) zur Befeuchtung der Aktivkohle (5 a) geleitet wird, wobei im Befeuchter vor rangig die Restlösemittel ausgetrieben werden und zusätzlich Wasser verdunstet wird.
- a) the desorbate predominantly consisting of water is condensed in the cooler ( 1 ) in the initial phase of the desorption and is introduced into a buffer tank ( 2 ),
- b) when an inert gas temperature of 70 to 90 ° is reached at the adsorber outlet ( 5 b), low-water condensate is passed into a further buffer tank ( 4 ) and then this condensate is dried in liquid form through a downstream molecular sieve ( 6 ) and the solvent is recovered,
- c) at the end of the desorption, a partial stream (T 1 ) of the still hot inert gas is led past the cooler ( 1 ) and passed through the molecular sieve ( 6 ) for regeneration, and then the now cooled, water-containing inert gas partial stream emerging from the molecular sieve ( 6 ) (T 2 ) via a humidifier ( 7 ), which is fed with the water / solvent mixture collected at the beginning of the desorption in the buffer container ( 2 ), is passed into the adsorber ( 5 ) for moistening the activated carbon ( 5 a) , wherein in the humidifier the residual solvents are primarily driven out and water is also evaporated.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE3545613 | 1985-12-21 | ||
| DE19863643757 DE3643757C2 (en) | 1985-12-21 | 1986-12-20 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19863643757 DE3643757C2 (en) | 1985-12-21 | 1986-12-20 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| DE3643757A1 DE3643757A1 (en) | 1987-06-25 |
| DE3643757C2 true DE3643757C2 (en) | 1990-10-18 |
Family
ID=25839229
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| DE19863643757 Expired - Fee Related DE3643757C2 (en) | 1985-12-21 | 1986-12-20 |
Country Status (1)
| Country | Link |
|---|---|
| DE (1) | DE3643757C2 (en) |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU540231B2 (en) * | 1978-11-02 | 1984-11-08 | Mitsubishi Kasei Corporation | Adsorption separation method and apparatus |
| DE2942959C2 (en) * | 1979-10-24 | 1986-07-17 | Rekuperator Kg Dr.-Ing. Schack & Co, 4000 Duesseldorf, De | |
| DE3146553A1 (en) * | 1980-11-28 | 1982-09-09 | Coal Industry Patents Ltd | "METHOD FOR TREATING WATER-BASED ORGANIC SOLVENTS" |
| DE3316062A1 (en) * | 1983-05-03 | 1984-11-08 | Schott Glaswerke | Process for eliminating solvents from waste waters |
| DE3533313C2 (en) * | 1984-09-27 | 1988-03-24 | Otto Oeko-Tech Gmbh & Co Kg, 5000 Koeln, De |
-
1986
- 1986-12-20 DE DE19863643757 patent/DE3643757C2/de not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| DE3643757A1 (en) | 1987-06-25 |
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