EP3055057A2 - Apparatur und verfahren zur untersuchung von diskontinuierlichen produktfluidströmen bei der umsetzung von eduktfluidströmen an feststoffkatalysatoren - Google Patents
Apparatur und verfahren zur untersuchung von diskontinuierlichen produktfluidströmen bei der umsetzung von eduktfluidströmen an feststoffkatalysatorenInfo
- Publication number
- EP3055057A2 EP3055057A2 EP14781876.9A EP14781876A EP3055057A2 EP 3055057 A2 EP3055057 A2 EP 3055057A2 EP 14781876 A EP14781876 A EP 14781876A EP 3055057 A2 EP3055057 A2 EP 3055057A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- fluid
- line
- reaction
- space
- valve
- 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.)
- Withdrawn
Links
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Classifications
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- G—PHYSICS
- G01—MEASURING; TESTING
- G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
- G01N31/00—Investigating or analysing non-biological materials by the use of the chemical methods specified in the subgroup; Apparatus specially adapted for such methods
- G01N31/10—Investigating or analysing non-biological materials by the use of the chemical methods specified in the subgroup; Apparatus specially adapted for such methods using catalysis
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- 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
- B01J19/0046—Sequential or parallel reactions, e.g. for the synthesis of polypeptides or polynucleotides; Apparatus and devices for combinatorial chemistry or for making molecular arrays
-
- 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
- B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
- B01J2219/00277—Apparatus
- B01J2219/00279—Features relating to reactor vessels
- B01J2219/00281—Individual reactor vessels
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- 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
- B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
- B01J2219/00277—Apparatus
- B01J2219/00279—Features relating to reactor vessels
- B01J2219/00281—Individual reactor vessels
- B01J2219/00286—Reactor vessels with top and bottom openings
-
- 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
- B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
- B01J2219/00277—Apparatus
- B01J2219/00477—Means for pressurising the reaction vessels
-
- 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
- B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
- B01J2219/00277—Apparatus
- B01J2219/00479—Means for mixing reactants or products in the reaction vessels
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- 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
- B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
- B01J2219/0068—Means for controlling the apparatus of the process
- B01J2219/00702—Processes involving means for analysing and characterising the products
- B01J2219/00704—Processes involving means for analysing and characterising the products integrated with the reactor apparatus
-
- 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
- B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
- B01J2219/0068—Means for controlling the apparatus of the process
- B01J2219/00702—Processes involving means for analysing and characterising the products
- B01J2219/00707—Processes involving means for analysing and characterising the products separated from the reactor apparatus
-
- 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
- B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
- B01J2219/00718—Type of compounds synthesised
- B01J2219/00745—Inorganic compounds
- B01J2219/00747—Catalysts
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- C—CHEMISTRY; METALLURGY
- C40—COMBINATORIAL TECHNOLOGY
- C40B—COMBINATORIAL CHEMISTRY; LIBRARIES, e.g. CHEMICAL LIBRARIES
- C40B30/00—Methods of screening libraries
- C40B30/08—Methods of screening libraries by measuring catalytic activity
-
- C—CHEMISTRY; METALLURGY
- C40—COMBINATORIAL TECHNOLOGY
- C40B—COMBINATORIAL CHEMISTRY; LIBRARIES, e.g. CHEMICAL LIBRARIES
- C40B60/00—Apparatus specially adapted for use in combinatorial chemistry or with libraries
- C40B60/12—Apparatus specially adapted for use in combinatorial chemistry or with libraries for screening libraries
Definitions
- the present invention relates to an apparatus and a method for the investigation of discontinuous product fluid streams, which are formed, for example, in the reaction of educt fluid streams of solid catalysts.
- the product fluid streams formed during catalytic processes can sometimes be subject to considerable changes over time, since the catalyst samples to be investigated have, for example, aging effects or lose or completely deactivate a large portion of activity due to deposits within short operating times.
- the effects of catalyst aging and catalyst deactivation are reversible and the catalysts can be reactivated by means of a suitable regeneration phase.
- the investigation of catalyst aging and regeneration is of great economic and technical interest with regard to the development of new catalysts and catalytic processes which have improved properties.
- improving catalytic processes is a major technical challenge.
- the development and improvement of high throughput methods is a key element in catalyst research to bring new and improved products to market in less time.
- liquid phase separators are also known in the field of catalytic laboratory equipment used for high-throughput research.
- WO2005 / 063372 by the hte Aktiengesellschaft, in which different embodiments of catalyst test equipment are described, which allow the parallelized investigation of solid state catalysts.
- WO2005 / 063372 several embodiments of catalyst test apparatuses are shown in which each reaction chamber of the reaction chambers arranged in parallel is followed by one liquid phase separator per reaction space in each case.
- WO2005 / 063372 in Figure 6 discloses a catalyst test apparatus in which each reaction space is connected to two liquid phase separators each, which are arranged sequentially and which function as high pressure and low pressure separators.
- WO2004 / 052530 discloses an apparatus for testing catalysts by means of which a large number of fluid streams are generated, which are supplied for analytical characterization.
- the individual fluid streams which emerge from the reaction vessels (8) arranged in parallel are first led to a respective gas splitter (12).
- the individual gas splitter (12) are connected via lines (12) and pressure reduction elements (18) with a common multiportortventil.
- the individual gas splitter (12) connecting lines (14) to a common container (42), in which a separation of liquid and gaseous components takes place.
- the container (42) is connected via a pressure reduction element (46) with an exhaust air line (48), wherein an analysis unit (50) is connected downstream.
- FIG. 5 shows a schematic representation of an apparatus equipped with two parallel reactors. Each reactor is followed by a separator (4001), each separator having one outlet for liquids and one outlet for gases.
- WO 2008/012073 discloses a catalyst test apparatus with reactors arranged in parallel, which is equipped with liquid phase separators and gas collection containers. WO 2008/012073 relates to the handling of multicomponent mixtures which consist of at least two incompletely miscible fluid phases.
- DE 102004039378 discloses an apparatus and method for controlled sampling of samples from pressure vessels in which the containers may be in a parallel arrangement. Downstream of the pressure vessel according to the invention is a sample storage unit, which is in operative connection via a first valve with the pressure vessel and a second valve with the sample receiving unit. The invention allows the discontinuous removal of samples from the pressure vessel, wherein the sample is transferred via the sample storage unit to an analysis unit.
- An object of the invention is to provide an apparatus and a method which makes it possible to investigate catalytic processes in conjunction with discontinuous product fluid streams with an improved temporal resolution than is possible with the apparatus and methods known in the prior art.
- the apparatus according to the invention and the method according to the invention should in particular relate to the investigation of processes which have a high tendency to deactivate. Thus, the accuracy of the prior art methods for analyzing processes associated with catalyst deactivation and other temporal effects should be improved.
- an apparatus for reacting solid catalysts and processes in which discontinuous fluid streams occur comprising a feedstock fluid feed (01), a reaction space (21/1) and at least one fluid mixing space (33 ), at least one throttle element (1 1) and at least one pressure control valve (51) at least one analyzer (43), wherein the apparatus is characterized in that the reaction space (21) on the output side via a connecting line (22) and partial flow line (36) at least one fluid mixing chamber (33) is in operative connection and the at least one fluid mixing chamber (33) with a throttle element (1 1) is connected, wherein the throttle elements (1 1) with
- the connecting pipe (22) is operatively connected to the pressure regulating valve (51) and to an exhaust pipe (63), the pressure regulating valve (51) being located either downstream or upstream of the partial flow pipe (36) and, if the pressure regulating valve (51) is upstream of the partial flow pipe
- reaction space (21) on the output side via an arrangement of connecting line (23), fluid container (24), connecting line (25) and a partial flow line (36) with at least one fluid mixing chamber (33) is in operative connection and the fluid mixing chamber (33) with a throttle element (1 1) is connected, wherein the one or more throttle elements (1 1) with a) an analyzer (43) and
- connection line (25) is operatively connected to the pressure control valve (51) and to an exhaust duct (63), the pressure regulating valve (51) being located either downstream or upstream of the partial flow duct (36) and, if the pressure regulating valve (51) upstream of the partial flow duct (36), the output line (62) with a second pressure regulating valve (51/2) and a pump (91) is provided.
- the apparatus according to the invention is characterized in that it has at least two or more reaction chambers arranged in parallel [(21/1), (21/2), ... or (21 / x)], each of the reaction spaces with, respectively at least one fluid mixing chamber (33 / x) is in operative connection, the individual fluid mixing chambers each have an operative connection to a multiple valve (41/1), wherein the multiple valve (41/1) is preferably equipped as a multiport valve and / or in the respective operative connection (22 ) of the reaction chamber (21 / x) and fluid mixing chamber (33 / x), a valve (83) is arranged directly in front of the fluid mixing chamber (33 / x).
- the apparatus has at least four reaction spaces (21/01 - 21/04), preferably eight reaction spaces (21/01 - 21/08), and the multiple valve is designed as a multiport valve (41/1).
- the apparatus is characterized in that each connecting line between the outlet side of a reaction space and the respective gas mixing chamber (33 / x) each has a partial flow line (36 / x), the individual partial flow lines (36 / x) with the output line (62 ) are operatively connected, wherein the control device (51) is preferably arranged downstream of the connection of the partial flow lines to the output line (62).
- each partial flow line is in operative connection with a second multiport valve (41/2), that the multiport valve (41/2) has an operative connection with the output line (62) and with a second analyzer ( 43/2), wherein the connection of multiport valve to the output line - and also the output line of the second analyzer to the output line (62) - upstream of the control device (51) is present.
- the connection to the output line (62) can be designed differently in different embodiments of the apparatus according to the invention.
- that embodiment of the apparatus which has a multiport valve in the operative connection from the throttle element to the output line can also have an output line (45) leading from the multiport valve (41) to the output line and thereby bypassing the analyzer (43/1) (such as, for example shown in FIG. 5).
- the apparatus is characterized in that, on the output side to the reactor space (21 / x), a switching valve (83 / x) is in operative connection with the fluid mixing chamber (33 / x) via a partial flow line (36 / x).
- reaction spaces (21 / x) are tubular reactors, each having an interior volume in the range from 0.1 to 5000 ml, preferably from 0.2 ml to 200 ml, more preferably from 0.5 to 100 ml.
- the apparatus is characterized in that, on the output side to the reactor chamber (21 / x), a fluid container (24 / x) is in operative connection with the partial flow line (36 / x).
- a fluid container (24 / x) is in operative connection with the partial flow line (36 / x).
- the fluid container (24 / x) it is preferred that these each have an internal volume in the range of 5 to 5000 ml, preferably in the range of 10 to 3000 ml, more preferably 50 to 1000 ml.
- the fluid containers are temperature-controlled, wherein the temperature is preferably in the range of -20 to + 400 ° C, preferably in the range of -10 to + 350 ° C and more preferably in the range -5 to + 300 ° C.
- the fluid container is a condenser which separates condensable fluid components from the product stream.
- the Fluidbehalter may alternatively be designed as a damping vessel or as a condenser and damping vessel, with the help of short-term pressure fluctuations are intercepted.
- the short-term pressure fluctuations can be caused for example by changes between the fluid phases within a cycle, which can occur when switching the valves.
- the gas mixing chambers (33 / x), it is preferred that these each have an interior volume in the range of 5 to 5000 ml, more preferably 10 to 3000 ml, more preferably 50 to 1000 ml.
- the gas mixing chambers are heated and are heated at a predetermined temperature, so that all gas mixing chambers arranged in parallel have a defined temperature.
- all gas mixing chambers have the same temperature.
- the temperature of the gas mixing chambers is in the range of 0 - 400 ° C, preferably in the range of 0 to 350 ° C and more preferably in the range of 20 - 300 ° C.
- a suitable condenser is then preferably arranged in the line system upstream of the gas mixing chamber (33 / x), with a suitable apparatus having at least one condenser (24 / x) per reactor space (21 / x).
- the apparatus according to the invention is characterized in that it has at least two fluid mixing chambers in a sequential arrangement per reaction space and each reaction space (21 / x) has on the output side the first fluid mixing space (33 / ⁇ ') of this sequential arrangement Active connection is and the output side of the second fluid mixing chamber (33 / x ") or the output side of the sequentially last arranged fluid mixing chamber with throttle device (1 1/1) or (1 1 / x) is in operative connection.
- analytical devices all technical devices can be used, which are suitable for the quantitative and qualitative investigation of material flows. Examples include gas chromatographs, GC-MS, NIR, IR detectors, UV, UV-VIS. If the apparatus is equipped only with an analyzer, this may preferably be a GC or a GC-MS. If the apparatus is equipped with two or more analyzers, it includes, for example, in addition to a GC or a GC-MS at least also a hot gas flow analyzer.
- the essential parameters for characterizing a catalyst or a catalytic process are given by the determination of the activity and the selectivity with regard to a defined target reaction.
- the activity is defined as the total consumption rate of reactants.
- the activity can also be described in relation to the specified product components that arise in a catalytic process.
- Selectivity is the fraction of a given product component relative to the totality of all product components.
- the activity and the selectivity are time-dependent parameters and regularly change more or less rapidly in the course of a procedure. If the changes take place in short time periods, then these are so far difficult to study with the apparatuses and methods known in the prior art.
- the apparatus according to the invention may be in the form of a riser reactor, a downer reactor, a fixed bed reactor, a fluidized bed reactor, an eddy current reactor, a motor test bench or a combustion reactor.
- the invention relates to a method for the characterization of discontinuous fluid streams, the method comprising the following steps:
- the implementation of the method is characterized in that the average residence time of a molecule or a component in the fluid mixing chamber corresponds at least to the duration of a single cycle.
- the average residence time of a molecule or a component in the fluid mixing chamber of the time duration T corresponds to two to four cycles when the fluid stream is continuously transferred into the fluid mixing chamber.
- the controlled feed can be either a continuous feed, in which cyclic fluid flows occur, or a time-limited (ie discrete fluid stream) feed, in which at least one fluid flow phase is transferred to the gas mixing hopper by partial flow metering ,
- each cycle comprises at least two fluid flow phases, which take place alternately, so that the at least one fluid flow phase is in each case replaced by at least one second fluid flow phase, wherein the second phase can be replaced by a third fluid flow phase.
- the inventive method is preferably characterized in that the duration of a single cycle is in the range of 0.2 to 7200 s, preferably in the range of 1 - 3600 s.
- the time duration of the reactant stream phase is in the range 0.1-3600 s, preferably in the range of 0.1-1800 s and more preferably in the range of 0.1-900 s.
- the process according to the invention can have 1-50 fluid flow phases per cycle, preferably 2-10 fluid flow phases, and more preferably 2-5 fluid flow phases.
- the switching valve (83 / x) is switched so that first one and then no fluid stream flows into the gas mixing container. It is the beginning of the additional mixing time.
- the gas mixing chamber (33 / x) thus serves as a storage unit for a gas volume of the fluid phases, taking into account the amount of the withdrawn partial flow and the duration of the sampling.
- the switching valve (83 / x) is switched so that a fluid stream, preferably an inert gas, and more preferably nitrogen, from the gas supply device (02 / x) in the gas mixing chamber (33 / x) downstream of the switching valve ( 83 / x) and the previously stored in the gas mixing tank (33 / x) fluid volume from the gas mixing tank (33 / x) is flushed.
- This procedure effects backmixing of all fluid components for a single fluid flow phase as compared to carrying out the process without the switching valve (83 / x), as allowing a longer residence time of fluid volume in the gas mixing vessel (33 / x).
- a correspondingly long residence time must be used so that the mixing is made possible in this way.
- the process according to the invention can have at least one reactant stream phase and at least one regeneration stream phase, these taking place in alternating operation so that the at least one educt stream phase is in each case detached from the at least one regeneration phase.
- a preferred mode of operation is characterized by the fact that a rinsing phase takes place between the educt current phase and the regeneration phase.
- an inert gas or a carrier gas is passed through (the reaction space (21) and) the feed line (36) into the fluid mixer (33), which has no educt or product components. Due to the rinsing phase, it is technically possible to Separation of Eduktstromphase and regeneration phase to allow and to avoid unwanted reactions between reactant stream and the regeneration stream.
- mean residence time of molecules or components refers to the residence times of the molecules or components in the fluid mixer (33).
- Supply of a fluid flow means that there is a conductive connection element (36) by means of which the supply of the fluid flow is accomplished.
- Characteristic of this feed element (ZFE) ie element (36)
- the fluid mixer (FM) ie, member (33)
- QFM cross-sectional area of the delivery member.
- the flow rate of the fluid flow in the fluid mixer (33) is less than the flow rate of the fluid flow in the delivery member (36).
- the respective design and configuration of the fluid mixing chamber (33) can be accomplished by a person skilled in the art with knowledge known to him.
- the fluid mixing chamber allows for efficient backmixing of the fluids.
- the characteristic property of a fluid mixer results from the average residence times of molecules and components within the fluid mixer and the duration of a fluid idstromphase or a single fluid flow cycle.
- the fluid mixer is a gas mixing chamber (33 / x).
- the simplest embodiment of such a gas mixing chamber is a pipe. It is obvious to the person skilled in the art which geometric designs and dimensions of the gas mixing chamber lead to higher remixing time constants.
- the mean residence time of the molecules and / or components in the gas mixing space (or fluid mixing space) is at least as long as the duration of a fluid flow phase, preferably at least as long as the duration of two fluid flow phases, more preferably at least as long as the duration of three or more fluid flow phases.
- the temperature of the fluid mixer can - in addition to the geometric design - be of great importance, as far as the accuracy of the method.
- the temperature and the molecular properties have a considerable influence on the diffusion behavior of the substances.
- a fluid mixer used for gaseous fluids differs from a fluid mixer for liquid fluids because the diffusion characteristics of liquids and gases differ.
- the "fluid stream" which is passed through the feed element has a discontinuous composition when the composition of the volume flow at a given point in the feed is considered at successive times.
- concentration profile is to be understood as referring to one or more components.
- the concentration of the component A in this volume element may change over time.
- the concentration profile results from plotting the concentration versus time.
- the fluid stream comprises at least one component or several components, wherein a carrier fluid flow must also be present, as long as the fluid flow has only a single component.
- the fluid flow is a multicomponent system.
- the multicomponent systems to be investigated can also be constructed very complex.
- the component or plurality of components can be present in very different concentrations.
- concentration of the individual components over time may change more or less, for example, related to the process of formation of the fluid flow.
- the inventive method is based on the fact that discontinuous fluid flows incurred. From these fluid streams, defined (or discrete) regions are selected, which are then integrally transformed in the fluid mixer (33) into a continuous region of fluid flow. The continuous region is discharged through the outlet, with parts of the fluid stream being subjected to analysis [(43) and (43/1), (43/2)], respectively.
- analysis [(43) and (43/1), (43/2)] respectively.
- a mixed fluid flow phase is formed, which then has a constant or nearly constant concentration profile over a defined time range.
- the statement regarding the constant or nearly constant concentration pro refers to a mixed fluid flow in a line element downstream of the fluid mixer or in the fluid mixing chamber (33).
- the integral amount of the fluid components of the cycle can be determined. Accordingly, the method of the invention enables the (parallelized) integral quantification of components of a fluid flow having a discontinuous concentration profile.
- the time duration of the educt current phase is chosen so that at least a significant part of the period of deactivation of the catalyst takes place in this period of time. In terms of the catalytic process, this means that the activity reduction of the process is in the range of 0.1% to 95% per second, preferably in the range of 1 to 50% per second.
- the method of the invention relates to the (analytical) characterization of fluid streams, wherein the fluid stream (s) originates from a catalytic test apparatus for catalytic process analysis and is a gaseous fluid stream, the GHSV being in the range of 250-200,000 r 1 , preferably from 500 to 150000 hr 1 and more preferably from 500 to 100000 hr 1 .
- Essential for the present invention is also the combination of partial flow withdrawal with downstream backmixing.
- the partial flow take-off has the advantage that, especially in the high GHSV range, at which GHSV values of 500 hr 1 are exceeded, the amount of product fluid flow is very high and exceeds the capacity of fluid mixing chambers (33 / x) or the dimensioning of the fluid mixing chambers ( 33 / x) becomes unsuitable for laboratory investigations, which is disadvantageous in particular for the parallelized arrangement of reaction spaces (21 / x).
- the specification of the GHSV value of 500 hr 1 relates in this case to catalyst volumes in the range of 1 ml.
- the backmixing is carried out under precisely controlled conditions and thus the discontinuous product fluid stream can be treated in a targeted and very well defined manner. It should be noted that it may also be advantageous in the method that a rinsing step is used to fill the gas mixer (33) (or the gas mixer (33 / x)) with fluid flow which in the composition is the fluid flow of the similar to experimental investigation. If a purge step is used, then flush the dead volume three times with this purge flow stream. With respect to the dead volume, which is located downstream of the reaction spaces (21 / x), the volume of the gas mixing chamber (33) has the largest volume and is flushed only by the partial flow. Thus, in particular, the volume within the gas mixing chamber (33) should be exchanged three times.
- the method according to the invention thus also comprises a rinsing step (ix) which precedes step (i) and which consists in passing a suitable fluid through the feed line (36) to the gas mixing chamber including gas mixing chamber (33). is passed, wherein the volume of the partial fluid flow about three times the dead volume fills this area of the apparatus.
- the rinsing step is not necessary if the method is carried out with the Figure 2 shown in Figure 2, in which the gas mixing chamber (33) is decoupled from the supply of the iden- and the flow of the fluid flow in part during the period expires, in which no fluid flow to the gas mixing chamber (33) takes place.
- the process according to the invention is suitable for the investigation of all discontinuous processes in which discontinuous fluid streams occur. This may be the case, for example, in processes that are performed in conjunction with temperature changes of the catalyst temperature, or in processes that are performed with feed changes (flow changes, concentration changes) or pressure changes. In addition, also in processes in connection with rapid catalyst deactivation (aging). The changes in the parameters mentioned here may be present individually or jointly.
- the method is suitable for investigating reversible processes.
- the method for characterizing fluid streams in a preferred embodiment is characterized in that the method is carried out at a pressure in the range of 0.5 to 200 bar, preferably 0.5 to 150 bar and more preferably 0.5 to 100 bar becomes.
- the analysis times depend both on the particular analyzer used ((43) or (43/1), (43/2)) and on the complexity of the product mixture to be analyzed.
- it is also the number of installed in an apparatus reaction chambers (21 / x) of importance, and whether, for example, four, eight, sixteen or more reaction spaces are arranged in parallel.
- the larger number of reaction rooms is associated with a larger number of gas mixing rooms (33 / x). It can also be seen that the design of the apparatus with increasing number of reaction spaces (21 / x) and gas mixing chambers (33 / x) is associated with greater technical requirements in terms of control and handling.
- the apparatus according to the invention has less than 200 reaction spaces, preferably less than 100 reaction spaces and even more preferably less than 50 reaction spaces.
- the information given here with regard to the upper limit for the number of reaction spaces (21 / x) is not intended to limit the invention in any way.
- each reactor is connected to a respective gas mixing chamber (33 / x). It is also conceivable that a single reactor with several gas mixing chambers [(33 / ⁇ '), (33 / x ”) ...] connected which can then be connected in series and filled in order to form subducts of product fluid and to carry out further kinetic investigations.
- the respective analysis time for the analysis of a product fluid stream taken in a gas mixing chamber (33) and the number of gas mixing chambers as well as the number of analyzers (43 / x) used to characterize the product mixture from the gas mixing chamber be used.
- the analysis times are in the time range between 30 s and 1800 s.
- the analysis time of a complex product mixture may be 1200 seconds.
- an analysis time in the range of 4 to 6 hours may result to analyze all product mixtures that are in the sixteen gas mixing spaces.
- the example given here relates to an apparatus which is equipped with an analyzer and in which each reactor is connected to a respective gas mixing chamber. Examples
- Table 1 shows the results of a first series of tests in which the duration of the fluid phases introduced into the gas mixing vessel was varied. Ethane (at a flow rate of 83.3 mL / min) was used as fluid phase 1, and nitrogen (at a flow rate of 62.6 mL / min) was used as fluid phase 2, each being alternately introduced into the gas mixing vessel. [The same flow rates - 83.3 mL / min ethane stream and 62.6 mL / min IS stream - were also used in Examples B5-B8. The data given here refers to standard liters.] Thus, a single cycle consisted of a phase 1 in which ethane was introduced into the gas mixing vessel and a phase 2 in which nitrogen was introduced into the gas mixing vessel.
- phase 1 and phase 2 the same phase lengths were chosen in all examples.
- the duration of the fluid phases was 5 minutes in Example 1, 10 minutes in Example 2, and 20 minutes in Example 3, respectively. This resulted in a cycle time of 10 minutes for example 1, 20 minutes of example 2 and 40 minutes for example 3.
- the switching times between the different phases and cycles were in the range of milliseconds, and thus without influence on the examination.
- the ethane concentration was is correct and the percentage standard deviation (STDP) is calculated.
- STDP percentage standard deviation
- Comparison with analysis of an ethane stream with 50.5% by volume in Example B4 gives a percentage standard deviation of 0.15% and shows the quality and the efficiency of high accuracy for the experimental examples according to the method according to the invention.
- the following formula was used as the basis for the calculation of the standard deviation:
- Xi is the respective measured value, Xm the mean value and n the number of measurements.
- the phase durations were chosen so that each individual phase had a duration of 5 minutes. This resulted in a cycle time of 10 minutes. Within one experiment, the cycles were repeated at least ten times.
- the ratio of the residence time t rt (the abbreviation rt is used here for retention time) for the cycle duration T cyc ie is a characteristic parameter for the method according to the invention.
- the ratio of residence time to cycle time (trt / T cyc ie ratio) should have a value greater than 4. In this context, it should be noted that it is difficult to conclude on a preferred value of this parameter.
- a plot of the measurement results in FIGS. 9 and 10 shows that the quantitative measured values of the ethane content have slight differences, which are due to very small pressure fluctuations of the apparatus. Such deviations in the quantitative indication of the measured values can be compensated for by adding an internal standard. These pressure fluctuations occur during the fluid change. Therefore, their contribution is proportional to the frequency of the fluid changes ( ⁇ 1 / T cyc ie). Irrespective of the deviation of the absolute values, the fluctuation of the measured values lies in the range of the accuracy of the analyzer, which thus demonstrates the particular suitability of the method according to the invention.
- Table 1 shows a representation of the experimental parameters and test results of a back-mixing experiment by means of the design and method according to the invention, wherein in Examples B1 to B3 the length of the phase duration was changed. All three examples used a fluid mixing space formed by three sequentially arranged containers. Each individual container had an internal volume of 50 mL, resulting in a total internal volume of 150 mL. For comparison, a comparable ethane concentration was determined in B4 using the same analysis unit. B4 thus clarifies the analysis accuracy.
- Table 2 shows a representation of the test parameters and test results of a back-mixing experiment by means of the construction and method according to the invention, the influence of the geometry of the gas-mixing container being investigated.
- Example B5 an array of three sequentially arranged containers was used. Each of the three containers had an internal volume of 50 mL.
- Example B6 a single gas mixing vessel with an internal volume of 150 mL was used.
- Table 3 shows a representation of the experimental parameters and test results of a back-mixing experiment by means of the design and method according to the invention, wherein the influence of the internal volume of the gas mixing container on the mixing efficiency was determined.
- a gas mixing vessel with an internal volume of 75 mL was used and in example B8 a gas mixing vessel with 150 mL was used.
- the product stream composition was continuously analyzed with a second analyzer. From the data obtained, the integral product stream composition was determined over a number of cycles and contacted with the appropriate reactant stream. As described above, the product stream analysis was carried out for each change in the reaction condition (temperature or duration of a feedstock phase) from the time from which the product flow phase has no time change due to backmixing effects from the fluid mixing spaces. To determine the necessary time period, preliminary experiments were carried out analogously to the investigation described in FIG. For clarity, the hydrocarbons having a number of six or more carbon atoms of the six carbon atom (ie carbon number 6) linking group have been summarized for clarity.
- Table 5 shows the amount of catalyst and inert material used in these experiments and the nature of the arrangement of these materials in the reactor.
- the inert material served as a diluent.
- Catalyst Catalyst m (catalyst) m (inert material) Type of arrangement in the example (particle size (particle size reactor
- Table 7 shows the reaction parameters used for these experiments used to test the catalysts listed in Table 4.
- FIG. 12 shows the propane conversions of the three neat catalysts K1, K6 and K1 1 at 500 ° C., 550 ° C. and 600 ° C. It can be seen that a significantly higher conversion was achieved with increasing temperature, wherein K1 is significantly more active at each temperature than Example K6 and Example K1. At a temperature of 550 ° C, a decrease in activity over time was observed for K1 and K6. The decrease in activity over time could also be observed at a temperature of 600 ° C. An extension of the starting material phase from 10 s to 20 s at a temperature of 550 ° C did not lead to a significant change in the deactivation rate. Activity and decrease in activity over time correlate with the material properties listed in Table 4.
- Figure 13 Figure 15 and Figure 17 show the influence of the amount of catalyst or the influence of GHSV on the activity of the example of the respective catalyst material. It can be seen that with a larger amount of catalyst, a higher conversion is achieved. The deactivation rate is similar for all amounts of catalyst at the particular temperature.
- FIG. 14, FIG. 16 and FIG. 18 show the influence of the catalyst dilution and thus indirectly on the influence of the heat of reaction on the activity of the catalyst at the respective temperatures. It can be seen that undiluted catalysts tend to achieve a higher propane conversion.
- Figure 19 shows the product distribution of K1 determined at each of the first measurement points of the individual temperature stages, i. at 500 ° C, 550 ° C and 600 ° C. It can be seen that the C3 yield and in particular the propane yield became lower with increasing temperature, whereas the C1, C2 (paraffin), C2 (olefin), C3 (olefin) and C6 yield increase with increasing temperature. Similar tendencies were also observed for K6 ( Figure 20) and for K1 1 ( Figure 21), with differences in product distribution correlating with lower activity of the respective catalyst.
- Figure 22 shows the product distribution of each measurement point of K1 at 500 ° C. Due to the barely changing propane conversion over time (see Figure 12) at this temperature, the product flow composition can be used as an indicator of the reproducibility of the measurement.
- Figure 23 shows the product distribution of each measurement point (at different times) of K1 at 600 ° C. It can be seen that, as already evident from FIG. 12, the propane yield increases over time or the propane conversion decreases over time. In addition, it can be seen that with increasing time at a temperature of 600 ° C, the C6 yield decreases.
- Figure 1 shows a schematic representation of the apparatus for the investigation of reactions in a cyclic operation, in which a reaction space (21) via a partial flow line (36) with a gas mixing chamber (33) is in operative connection.
- FIG. 2 shows a schematic representation of the apparatus for the investigation of reactions, which is identical to the apparatus shown in FIG. 1, with the exception that a switching valve (83) via a partial flow line (36) with a fluid mixing vessel (33) is provided on the input side to the fluid mixing vessel (33) ) is in operative connection.
- a gas supply device (02) interacts with the switching valve (83).
- FIG. 3 shows a schematic representation of the apparatus for the investigation of reactions in a cyclical mode of operation, in which a reaction space (21) is in operative connection via a partial flow line (36) with a gas mixing space (33).
- a reaction space (21) is in operative connection via a partial flow line (36) with a gas mixing space (33).
- an analysis unit (43/2) on the input side to the control valve (51).
- FIG. 4 shows a schematic representation of an apparatus for the investigation of reactions in which each reactor space (21/1, 21/2) on the output side with a side stream line (36) is in operative connection, which in turn to a gas mixing tank (33/1, 33/2 ) connected is.
- Each gas mixing tank (33/1, 33/2) is on the output side via a restrictor element (1 1/1, 1 1/2) with the multiport valve (41) in operative connection.
- FIG. 5 shows a schematic representation of an apparatus for investigating reactions, which is identical to the apparatus shown in FIG. 4, except for the exception that for each fluid mixing tank (33 / x), a switching valve (83 / x) via a partial flow line (36 / x) is in operative connection with a fluid mixing container (33 / x). In addition, a gas supply device (02 / x) interacts with the switching valve (83 / x).
- FIG. 6 shows a schematic representation of an apparatus for investigating reactions, which is identical to the apparatus shown in FIG. 4, except that the reactor-outlet-side connection of each reactor space (21/1, 21/2) to a multiport valve (41 / 2) is in operative connection. On the output side to the multiport valve (41/2) there is an operative connection to the regulating valve (51).
- FIG. 7 shows a schematic representation of an apparatus for analyzing reactions, which is identical to the apparatus shown in FIG. 4, with the exception that the fluid supply component consists of valve 1 (81), valve 2 (82), gas supply device for fluid component A and Gas supply device for fluid component A.
- the fluid supply component consists of valve 1 (81), valve 2 (82), gas supply device for fluid component A and Gas supply device for fluid component A.
- FIG. 8.a shows a schematic representation of the influence of the gas mixing container according to the invention on a sequence of educt fluid phases A (A1-A4) which are determined by the invention.
- the arrangement according to the invention is backmixed in such a way that a concentration B can be determined with an analysis unit.
- FIG. 8.b shows a schematic representation of an apparatus which is referred to the application example described in FIG. 6, with the exception that no gas mixing container is used.
- C shows a non-stationary concentration profile.
- FIG. 9 shows the time profile of the measured ethane concentrations including the rinsing time for examples B1, B2, B3.
- FIG. 10 shows the time profile of the measured ethane concentrations after stabilization of the concentrations for Examples B1 to B4. The values were used to determine the percent standard deviation. If the cycle time (B3) is too long, the fluctuation of the concentration can be recognized with a period duration analogous to the cycle time.
- Figure 1 1 shows a schematic representation of the apparatus for the investigation of reactions, which is identical to the apparatus shown in Figure 1 with the exception that on the output side to the reaction space (21), a fluid container (24) with the partial flow line (36) is in operative connection.
- Figure 12 shows the time course of the propane conversion for K1, K6 and K1 1 at the reaction parameters listed in Table 7.
- FIG. 13 shows the time profile of the propane conversion for K1, K2 and K3 in the reaction parameters listed in Table 7.
- Figure 14 shows the time course of the propane conversion for K1, K2, K3, K4 and K5 at the reaction parameters listed in Table 7.
- Figure 15 shows the time course of the propane conversion for K6, K7 and K8 at the reaction parameters listed in Table 7.
- Figure 16 shows the time course of the propane conversion for K6, K7, K8, K9 and K10 at the reaction parameters listed in Table 7.
- FIG. 17 shows the time profile of the propane conversion for K1 1, K12 and K13 in the reaction parameters listed in Table 7.
- Figure 18 shows the time course of the propane conversion for K1 1, K12, K13, K14 and K15 at the reaction parameters listed in Table 7.
- Figure 19 shows the product distribution of K1 at 500 ° C (A), 550 ° C (B) and 600 ° C (C) for the respective first measurement point at the respective temperature.
- Figure 20 shows the product distribution of K6 at 500 ° C (A), 550 ° C (B) and 600 ° C (C) for the respective first measurement point at the respective temperature.
- FIG. 21 shows the product distribution of K1 1 at 500 ° C. (A), 550 ° C. (B) and 600 ° C. (C) for the respective first measuring point at the respective temperature.
- Figure 22 shows the product distribution of K1 at 500 ° C at time 1: 1, 3 hours (A), 22.0 hours (B), 32.6 hours (C), 43.2 hours (D).
- Figure 23 shows the product distribution of K1 at 600 ° C at time 159, 1h (A), 169.8h (B), 180.5h (C), 191, 1h (D), 201, 7h ( E), 212.4 hours (F).
- an aspect of the invention also relates to the parallelization of the apparatus and the method, since in this case the efficiency can be further increased.
- the inscriptions have partly been supplemented with a partial line and number or the letter x. How this system is understood should be understood by those skilled in the art.
- an addition of / x means that it may be a plurality of devices arranged in parallel.
- a numbering with the characters / 1, 12, 13 ... means that it is the first, the second, the third component ....
- the number of the respective components depends on the degree of parallelization.
- the number of multiport valves used results from the number of supply connections to the particular type of valve used, which may differ with respect to supply lines and technical specifications. However, the degree of parallelization of the apparatus must also be taken into account, since the number of reactors also results in the number of required supply lines to the multiport valve.
- a sequential arrangement of mixing containers is identified by the following numbering [(33 / ⁇ '), (33 / x ”) ...], where (33 / ⁇ ') refers to the first element and (33 / x") to the second element of the sequential arrangement relates.
- the connecting lines (22) between component can be configured the same or different. In the case of differently constructed connecting lines, these are then identified by (22 / x). Preferably, the connecting lines are designed the same. LIST OF REFERENCE NUMBERS
- Throttling element 1 1 1/1, 1 1/2 ,.
- Throttling element 2 ... (or (1 1 / x))
- connecting line from the reaction chamber outlet with gas mixing tank in parallel designed apparatus, the connecting lines (22) can be configured the same or different
- Fluid / gas mixing chamber 1 Fluid / gas mixing chamber 2
- fluid / gas mixing chamber 2 Fluid / gas mixing chamber 3
- Partial flow line 1 Partial flow line 1, partial flow line 2, ... (or (36 / x))
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DE102013016585.7A DE102013016585A1 (de) | 2013-10-08 | 2013-10-08 | Apparatur und Verfahren zur Untersuchung von diskontinuierllichen Produktfluidströmen bei der Umsetzung von Eduktfluidströmen an Feststoffkatalysatoren |
PCT/EP2014/071502 WO2015052212A2 (de) | 2013-10-08 | 2014-10-08 | Apparatur und verfahren zur untersuchung von diskontinuierlichen produktfluidströmen bei der umsetzung von eduktfluidströmen an feststoffkatalysatoren |
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EP (1) | EP3055057A2 (de) |
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EP3960286B1 (de) | 2020-08-26 | 2023-08-16 | HTE GmbH The High Throughput Experimentation Company | Vorrichtung und verfahren zur untersuchung von feststoffen |
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FR2795513B1 (fr) * | 1999-06-28 | 2001-08-03 | Inst Francais Du Petrole | Methode et dispositif multi-reacteurs automatique d'evaluation de catalyseurs avec une charge lourde |
ES2166310B1 (es) | 2000-02-08 | 2003-10-16 | Univ Valencia Politecnica | Dipositivo automatico y metodo de test catalitico multiple |
EP1256377A1 (de) * | 2001-05-11 | 2002-11-13 | Avantium International B.V. | Vorrichtung, geeignet zur Hochdurchsatzuntersuchung |
US20050169815A1 (en) | 2002-05-13 | 2005-08-04 | Avantium International B.V. | System for chemical experiments |
US7141217B2 (en) | 2002-12-05 | 2006-11-28 | Uop Llc | Elevated pressure apparatus and method for generating a plurality of isolated effluents |
DE10361003B3 (de) | 2003-12-23 | 2005-07-28 | Hte Ag The High Throughput Experimentation Company | Vorrichtung und Verfahren zur Druck- und Flusskontrolle in Parallelreaktoren |
DE102004039378A1 (de) | 2004-08-13 | 2006-02-23 | Hte Ag The High Throughput Experimentation Company | Vorrichtung zur kontrollierten Entnahme von Fluidproben aus Druckbehältern |
DE102006034172B3 (de) | 2006-07-24 | 2007-09-20 | Hte Ag The High Throughput Experimentation Company | Vorrichtung und Verfahren zur Handhabung von Multikomponenten-Gemischen |
DE102006053078A1 (de) | 2006-11-10 | 2008-05-15 | Hte Ag The High Throughput Experimentation Company | Vorrichtung und Verfahren zur kontinuierlichen Überführung und Analyse von Fluiden |
DE102010050599B4 (de) | 2009-11-07 | 2014-11-13 | Hte Gmbh The High Throughput Experimentation Company | Vorrichtung und Verfahren zur Testung von Katalysatoren mit verbesserter Prozessdruckeinstellung |
US9228985B2 (en) * | 2010-10-22 | 2016-01-05 | Hte Gmbh The High Throughput Experimentation Company | Device and method for testing catalysts with variable process pressure adjustment |
DE102011109454A1 (de) * | 2011-08-04 | 2013-02-07 | Hte Aktiengesellschaft | Verfahren zur Behandlung von Produktfluidströmen |
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2013
- 2013-10-08 DE DE102013016585.7A patent/DE102013016585A1/de not_active Withdrawn
-
2014
- 2014-10-08 WO PCT/EP2014/071502 patent/WO2015052212A2/de active Application Filing
- 2014-10-08 EP EP14781876.9A patent/EP3055057A2/de not_active Withdrawn
- 2014-10-08 US US15/028,242 patent/US10338042B2/en not_active Expired - Fee Related
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US10338042B2 (en) | 2019-07-02 |
US20160252485A1 (en) | 2016-09-01 |
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