WO2004022195A1 - Anlage und verfahren zum durchführen einer diskontinuierlichen rektifikation oder reaktion - Google Patents
Anlage und verfahren zum durchführen einer diskontinuierlichen rektifikation oder reaktion Download PDFInfo
- Publication number
- WO2004022195A1 WO2004022195A1 PCT/EP2003/009605 EP0309605W WO2004022195A1 WO 2004022195 A1 WO2004022195 A1 WO 2004022195A1 EP 0309605 W EP0309605 W EP 0309605W WO 2004022195 A1 WO2004022195 A1 WO 2004022195A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- product
- container
- column
- rectification
- column section
- Prior art date
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/008—Liquid distribution
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4205—Reflux ratio control splitter
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4211—Regulation; Control of columns
- B01D3/4238—Head-, side- and bottom stream
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
- B01J2219/00101—Reflux columns
Definitions
- the invention relates on the one hand to a plant for carrying out a batch rectification in a rectification column or for carrying out a chemical reaction in a batch reactor with a rectification column fitted, the rectification column being able to be operated under total reflux and at least one column section for mass transfer, at least one arranged below the column section Has product container for collecting and temporarily storing the liquid flowing down through the column section and at least one further product container for collecting and temporarily storing the top product.
- the column section for mass transfer can be designed differently depending on the type of rectification column. Bottom and packed columns as well as special constructions such as film and trickle columns and also rectification columns with rotating inserts (spray columns) and other types can be used.
- the invention is not restricted to a specific type of column. However, a packing column with built-in packings is preferred, as will be explained further below.
- the first advantage of this so-called "cyclical operation” is that the best possible theoretical separation performance can be achieved for the system used. This can easily be demonstrated graphically in the well-known McCabe-Thiele diagram for binary mixtures, since in this case the working line coincides with the diagonal, so that the best separation performance is achieved. Therefore, the "multivessel batch distillation” is particularly suitable for the production of high purity products.
- the advantage here is that no strategies are required for the continuous change in the reflux ratio, as is usually the case with conventional batch rectification.
- the second advantage of the cyclical mode of operation is that with "Multivessel Batch Distillation" it is very safe to manufacture defined product qualities.
- With the cyclical mode of operation no product leaves the system balance area for the time being, since there is no forwarding to the product tanks. Pumping into the product tanks only takes place when the product qualities meet the specified quality requirements. This severely limits the possibilities of operating errors during production. This is particularly important when manufacturing products with very high purity requirements.
- In conventional batch rectification if there is an operating error, it is precisely the last quantity of product that is fed into the product tank that can significantly deteriorate the quality of the highly pure product that has accumulated in the tank until then. This disadvantage is avoided with the cyclical driving style by the described procedure.
- a special case of "multivessel batch distillation” is a column with only one upper product container (top / distillate container) and with the bottom area as a further product container.
- top / distillate container top / distillate container
- bottom area as a further product container.
- only two products namely top and bottom product under total
- Return can be established.
- a concentration profile is naturally formed within the known rectification column 1 shown in FIG. 1. At least two components and usually several components are present in the individual column sections. This means that, for example, one or more components from the second product 3 'and third product 4' must always be present in the lower column section with the packs 7, 8. The same applies to all other column sections.
- liquid content within the column, which is composed of the holdup on the packing and packings.
- additional type of liquid content is important, namely the liquid content in the collectors and distributors not shown in FIG. 1.
- the liquid content in the collectors is particularly important.
- the cyclical mode of operation with a multi-vessel structure is characterized in that the individual containers are emptied and the entire liquid content of the product containers is pumped into the production tanks. If this is carried out for all product containers, the bottom region of a rectification column being understood here as a product container, the energy supply in the evaporator system is inevitably interrupted in the course of emptying. As a result of the greatly reduced amount of liquid in the sump area, the circulating flow in forced circulation evaporators, for example in falling film evaporators, or in natural circulation evaporators, breaks off and can no longer be maintained. This extremely disrupts the hydrodynamic conditions within the column.
- the invention is therefore based on the object of providing a facility in a system of the type mentioned at the outset, in operating the system on an industrial production scale, with high certainty to achieve a high degree of purity of the products obtained, with high product yields at the same time.
- This object is achieved according to the invention in the system of the type mentioned at the outset by providing a device for optionally guiding the liquid into the product container arranged below the column section or past this product container.
- the plant can be operated as follows: First of all, the rectification column is operated under total reflux, the device mentioned directing the liquid into the product container, where the liquid is collected and temporarily stored and finally returned to the column. If a stationary operating point of the system has been reached, and the product quality in the product containers meets the specified requirements, the product containers can be completely emptied without the holdup flowing into the product containers from top to bottom and deteriorating the product quality, since the device mentioned now switches over and the liquid flowing back flows past the product containers.
- the column section containing the holdup has at least one built-in packing and / or at least one built-in tray.
- a modern packed column and, if appropriate, a tray column is therefore preferred.
- Said device for optionally guiding the liquid can be designed differently, in particular depending on the type of product container. If the product container arranged below the column section is designed as a sump container or as a batch reactor, it is proposed that a collector is arranged between the lowest column section, for example the bottom packing of the rectification column, and the sump container or the batch reactor, the outlet of which with a Additional container and is connected to the sump container or to the batch reactor, and that the device for optionally guiding the liquid has a first valve arrangement.
- the first valve arrangement is actuated in such a way that the holdup from the lowest mass transfer area no longer into the sump container or into the batch reactor, but into the additional container flows and thus does not impair the high quality, in particular the high purity, of the bottom product.
- the downward-flowing liquid it is fundamentally possible for the downward-flowing liquid to flow completely through the said additional container and out of this into the sump, even during operation of the column with total reflux.
- a valve being arranged here at the outlet of the collector arranged below the lowest pack. To end the process, this valve is closed and another valve is opened, which directs the liquid into the additional container via a secondary line.
- the collector is connected via the first valve arrangement on the one hand to the additional container and on the other hand to the sump container or to the batch reactor.
- the first valve arrangement can consist of an arrangement of several valves or of a single multi-way valve.
- the plant according to the invention can be used not only for the physical separation of mixtures of substances, but also for carrying out chemical reactions, in particular also as a batch reactor with a rectification column attached.
- the sump container corresponds to a discontinuous boiler reactor, for example a stirred tank reactor.
- a plant with a stirred tank reactor and an attached rectification column according to the prior art is described for example in EP 0 464 045 B1 (Henkel KGaA).
- the rectification column here is not designed to carry out the "multivessel batch distillation".
- the liquid flowing downwards in the central column section via a second valve arrangement into a second product container, the outlet of which is connected to the lower-lying column section, or into a bypass line bypassing the second product container is steerable.
- the additionally provided container does not serve as a collection container for the holdup, but rather as a product container, which is connected to the column via corresponding valves, i.e. on the one hand to the outlet of the overhead collector and on the other hand to the inlet of the distributor below is.
- bypass line that bypasses the second product container, through which the holdup flows when the method is ended, in order not to contaminate the content that has already accumulated in the second product container.
- several product containers of this type can be arranged along the column, but at different heights, that is, below different middle column sections, the contents of the product containers being protected in the same way from the holdup flowing down when the method is ended.
- the product container for the top product namely the distillate container
- the product container for the top product is connected to the top of the column via an inflow line, in particular with a condenser, and a backflow line.
- the invention also includes a method for performing a rectification and / or a reaction in a plant of the type according to the invention.
- the method is first operated under total reflux and the liquid is directed into the product containers for intermediate storage and then, that is, when the specified or desired specification, in particular the desired purity, has been reached, steers past the product containers and empties the product containers.
- FIG. 1 is a schematic representation of a system for "multivessel batch distillation" according to the prior art
- FIG. 2 is a perspective view of the central area of a modern packing column with a packing from Sulzer according to the prior art
- FIG. 3 shows a schematic illustration of a system for "multivessel batch distillation" according to the invention in a first exemplary embodiment
- FIG. 3a shows the lower part of the system according to FIG. 3 according to another variant according to the invention
- Fig. 4 is a schematic representation of a plant according to the invention in a further embodiment with a reactor with an attached rectification column.
- the same reference symbols have the same meaning and are therefore only explained once, if appropriate.
- FIG. 1 An example of a system for "multivessel batch distillation" according to the prior art is shown schematically in FIG. 1.
- a plurality of product containers 2, 3 are arranged along an ordinary batch rectification column 1.
- the bottom area of the column is regarded as product container 4 for the bottom product.
- the liquid flowing down within the column 1 through the packs 5, 6, 7, 8 is removed from the column and passed into a corresponding product container 2, 3, 4.
- the products themselves are designated in the figures with the reference numerals 2 'for the top product, 3' for the product temporarily stored in the middle container 3 and 4 'for the bottom product.
- Several product containers can also be arranged in the central region of the column. After collecting a defined amount of liquid in the containers 2,
- the second phase of the method is initiated, in which the valves 12, 13, 14 are opened and the products 2 ', 3', 4 'from the individual product containers 2, 3, 4 removed and passed into the product tanks 15, 16, 17.
- FIG. 1 Also shown in FIG. 1 are a condenser 18, known per se, at the top of column 1 and the sump heater 19, known per se, which can be designed, for example, as a forced circulation evaporator or as a natural circulation evaporator.
- FIG. 2 shows a section of a conventional rectification column. The return flow from the condenser 18 is passed via the line 9 to a distributor 20 and from there flows down uniformly via the packing 21.
- the quantities of liquid emerging from the underside of the pack 21 are collected by inclined sheet metal lamellae, namely from the collector 22, and fed via a ring channel 23 to a further distributor 24, which distributes the liquid evenly onto the top of the pack 25 arranged below it.
- the lamella collector 22 can be, for example, a SLR type collector from Sulzer.
- a further line 26 is provided in the central area of the column, which opens into the ring channel 23.
- FIG. 3 shows a rectification column 1 for separating a liquid mixture.
- an additional line 27 is installed in the area of the product container 3 parallel to the product line 11 and can be shut off with a valve 28. With another valve 29, the product container 3 can be secured against the liquid flowing down in column 1.
- An additional valve 37 is also arranged between the outlet of the product container 3 and the distributor 24. At the stationary operating point of the system when the specified product quality in the product container 3 has been reached, the valves 29 and 37 are closed and the valve 28 is opened so that the liquid flows from the collector 22 directly to the distributor 24 and not into the product container 3 arrives. After opening the valve 13, the product container 3 is then emptied into the product tank 16.
- the entire liquid stream, which leaves the last packing section 8 and is collected by the collector 30, is conducted into the sump container 4 via the line 31 and the opened valve 32.
- the liquid flowing from the outlet of the collector 30 is passed via line 31 and an open valve 33 into an additional container 34, which passes through the column downward flowing holdup.
- the valve 32 is of course closed to prevent contamination of the bottom product 4 'by the holdup.
- the liquid mixture collected in the additional container 34 can be mixed again with the new feed the next time the process is carried out and worked up again.
- the additional container 34 can also be installed in such a way (FIG. 3a) that the total amount of liquid dispensed by the collector 30 always flows into the additional container 34 first. After reaching the stationary operating point, the additional container 34 is first emptied into the sump container 4 and then the valve 36 is closed. Now, as in the preferred variant according to FIG. 3, the sump container 4 is emptied into the product tank 17 by opening the valve 14 and closing the valve 38.
- An additional line 39 with a valve 40 is also advantageous at the column head (FIG. 3).
- the additional line 39 is put into operation by opening the valve 40 and closing the valves 41, 42, so that the contents of the product container 2 are protected against possible faults which could contaminate its composition.
- the invention also includes the special case of "multivessel batch distillation", in which a column with only one distillate container 2 and one bottoms product container 4 are provided as product containers and the so-called central container (s) 3 are missing.
- Typical of such arrangements are, in particular, the batch reactors known per se with an attached column, as are shown schematically, for example, in FIG. 4 in an embodiment according to the invention.
- the product container 4 for the bottom product is designed here as a stirred tank reactor 35.
- the other product container in Figure 4 is the distillate container 2. Because of the above Advantages of the system shown in Figure 4 is operated with total return.
- the rectification column attached also serves to remove the excess of starting material after the reaction has taken place.
- An example of such a reaction is the preparation of an ester from an organic acid and an alcohol, as described for example in the already mentioned EP 0 464 045 B1.
- the value component is a relatively low volatility product from which the low boilers can be separated.
- the system according to FIG. 4 is particularly suitable for bottom products of high purity, which would suffer a loss of quality when mixed with the liquid stream flowing down from column 1. This has the further advantage that a distillation step for removing the low boilers originating from the holdup can be saved from the bottom product.
- An esterification reaction can serve as an example, where A is alcohol, B acid, C ester and D is water. If you simplify assuming that A, B, C, D are completely miscible, a homogeneous mixture is obtained.
- the column serves to continuously remove water (component D) from the reaction mixture with minimal losses of components A, B and C. This has a very advantageous effect on the reaction equilibrium in the reactor. In order to minimize the investment costs, one tries in practice to minimize the column height. Since the best separation performance is achieved with total reflux, the following procedure is recommended (FIG. 4), the valves 41, 42, 43 being open and the valve 40 being closed. Alternatively, the reaction is
- a low-boiling product C is to be separated.
- the goal here is to obtain a product “as pure as possible” in the distillate container 2.
- the valves 41, 42, 43 are first opened and the valve 40 is closed. If essentially the entire amount of product C has accumulated in the product container 2 and gradually also undesired by-products of the reaction are distilled off and also threaten to get into the product container 2, the additional line 39 is started by opening the valve 40 and the valves 41 , 42 closed. The valve 43 naturally remains open. In this way, the content of the product container 2 is protected from distilled by-products and from the excess component A or B.
- additional line 39 An alternative to the additional line 39 would be a known switchover to a further container 44 arranged in parallel by means of another additional line 45.
- the further container 44 and the other additional line 45 with the valves are shown in broken lines in FIG.
- the water of reaction D accumulated in the container 2 is removed, unless the water has already been removed from the container 2 during the reaction, and the excess component is distilled off A or B from the reaction mixture in order to obtain the product of value C with the highest possible purity.
- the excess of the starting component A or B is collected in the product container 2, which has the function of a distillate feed.
- the highest possible concentration (purity) of the content in the product container 2 is aimed for, since this component is generally returned to the reactor and used again in the next batch. The highest possible concentration makes it possible to achieve a high space-time yield in the reactor for the next batch.
- valves 41, 42, 43 are open and the valve 40 is closed.
- valves 41, 42 are closed and the valve 40 in the additional line 39 is opened, the valve 43 naturally remaining open. 2. To protect the valuable product C, the valve 33 is then opened and the valve 32 is closed.
- the content of the additional container 34 is pumped into the batch reactor 35.
- the content of the product container 2 is also pumped into the batch reactor 35.
- the plant according to FIG. 4 consists of a reactor 35 and a column 1.
- a reaction takes place coupled with a distillation, for example an esterification with distilling off water.
- a distillation for example an esterification with distilling off water.
- only one distillation takes place, for example distilling off the excess of starting materials.
- the system behaves like a conventional batch distillation.
- the difference lies in the unusually large sump area that is formed by the reactor. In conventional batch distillation, however, the sump is not a reactor.
- a test example according to the invention was run in a system according to FIG.
- the column with a diameter of 70 mm, two packs of type BX from Sulzer, each with a height of 1 m, were arranged. Each of these packs corresponded to 5 to 6 theoretical plates.
- the column was operated at a top pressure of 10 to 20 mbar, the pressure drop across the column being 4 to 8 mbar.
- the bottom temperature was 130 to 140 ° C.
- a common reflux divider (Normag) with electromagnetic operation was used.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/526,956 US20060090995A1 (en) | 2002-09-07 | 2003-08-29 | System and method for carrying out a discontinuous rectification or reaction |
EP03753367A EP1534400A1 (de) | 2002-09-07 | 2003-08-29 | Anlage und verfahren zum durchführen einer diskontinuierlichen rektifikation oder reaktion |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10241482A DE10241482A1 (de) | 2002-09-07 | 2002-09-07 | Anlage und Verfahren zum Durchführen einer diskontinuierlichen Rektifikation oder Reaktion |
DE10241482.3 | 2002-09-07 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2004022195A1 true WO2004022195A1 (de) | 2004-03-18 |
Family
ID=31724485
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2003/009605 WO2004022195A1 (de) | 2002-09-07 | 2003-08-29 | Anlage und verfahren zum durchführen einer diskontinuierlichen rektifikation oder reaktion |
Country Status (4)
Country | Link |
---|---|
US (1) | US20060090995A1 (de) |
EP (1) | EP1534400A1 (de) |
DE (1) | DE10241482A1 (de) |
WO (1) | WO2004022195A1 (de) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8317166B2 (en) * | 2010-11-10 | 2012-11-27 | Koch-Glitsch, Lp | Liquid collection and distribution device for mass transfer column and process involving same |
RU2755176C1 (ru) * | 2020-11-17 | 2021-09-13 | Федеральное государственное бюджетное образовательное учреждение высшего образования "Сибирский государственный университет науки и технологий имени академика М.Ф. Решетнева" (СибГУ им. М.Ф. Решетнева) | Контактная ступень колонны термической ректификации |
BE1030125B1 (nl) * | 2021-12-28 | 2023-07-26 | De Neef Chemical Proc N V | Batch-destillatiewerkwijze en batch-destillatiekolom met zij-afvoerpunt |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE4322725A1 (de) * | 1993-07-08 | 1995-01-12 | Basf Ag | Verfahren zur Durchführung von destillativen Trennungen in diskontinuierlicher Betriebsweise |
EP0928782A2 (de) * | 1998-01-13 | 1999-07-14 | Huntsman Petrochemical Corporation | Verfahren zur Reindarstellung von Maleinsäureanhydrid |
US6143927A (en) * | 1996-06-24 | 2000-11-07 | Rpc Inc. | Methods for removing catalyst after oxidation of hydrocarbons |
Family Cites Families (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA1088021A (en) * | 1977-01-18 | 1980-10-21 | Robert J. Coker | Modified process for resin manufacturing using a continuous separate distillation column |
US4166773A (en) * | 1977-12-22 | 1979-09-04 | Union Carbide Corporation | Continuous process for separating high boiling, heat sensitive materials |
DE3138423A1 (de) * | 1981-09-26 | 1983-04-14 | Basf Ag, 6700 Ludwigshafen | Trennung von stoffmischungen |
GB8903009D0 (en) * | 1989-02-10 | 1989-03-30 | Shell Int Research | Vacuum distillation process |
GB8903013D0 (en) * | 1989-02-10 | 1989-03-30 | Shell Int Research | Vacuum distillation process |
US6245727B1 (en) * | 1989-03-20 | 2001-06-12 | Henkel Kommanditgesellschaft Auf Aktien | Discontinuous process for conducting a heterogeneously catalyzed reaction and installation for heterogeneously catalyzed manufacture of products |
FR2666025B1 (fr) * | 1990-08-22 | 1993-09-17 | Berberi Anwar | Procede et installation pour la production de diluants de peinture, d'encre, d'adhesif, et de vernis, a partir de leurs dechets. |
US5308452A (en) * | 1992-01-31 | 1994-05-03 | Progressive Recovery, Inc. | Photopolymer washout fluid solvent distillation apparatus and method |
DE4239117A1 (de) * | 1992-11-20 | 1994-05-26 | Wacker Chemie Gmbh | Verfahren zur Isolierung von reinem Diketen unter Rückgewinnung von Wertstoffen |
JP4558870B2 (ja) * | 1999-11-08 | 2010-10-06 | 株式会社日本触媒 | 塔式処理方法および装置 |
-
2002
- 2002-09-07 DE DE10241482A patent/DE10241482A1/de not_active Withdrawn
-
2003
- 2003-08-29 EP EP03753367A patent/EP1534400A1/de not_active Withdrawn
- 2003-08-29 US US10/526,956 patent/US20060090995A1/en not_active Abandoned
- 2003-08-29 WO PCT/EP2003/009605 patent/WO2004022195A1/de not_active Application Discontinuation
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE4322725A1 (de) * | 1993-07-08 | 1995-01-12 | Basf Ag | Verfahren zur Durchführung von destillativen Trennungen in diskontinuierlicher Betriebsweise |
US6143927A (en) * | 1996-06-24 | 2000-11-07 | Rpc Inc. | Methods for removing catalyst after oxidation of hydrocarbons |
EP0928782A2 (de) * | 1998-01-13 | 1999-07-14 | Huntsman Petrochemical Corporation | Verfahren zur Reindarstellung von Maleinsäureanhydrid |
Non-Patent Citations (1)
Title |
---|
DAVIS J ET AL: "COMPUTER CONTROL OF A DESULFURIZER FRACTIONATOR", CHEMICAL ENGINEERING PROGRESS, AMERICAN INSTITUTE OF CHEMICAL ENGINEERS. NEW YORK, US, vol. 82, no. 3, March 1986 (1986-03-01), pages 62 - 66, XP001048631, ISSN: 0360-7275 * |
Also Published As
Publication number | Publication date |
---|---|
DE10241482A1 (de) | 2004-03-18 |
EP1534400A1 (de) | 2005-06-01 |
US20060090995A1 (en) | 2006-05-04 |
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