WO2010020715A1 - Procédé et dispositif de séparation en lit mobile simulé à débit de fluide de dérivation modulé - Google Patents
Procédé et dispositif de séparation en lit mobile simulé à débit de fluide de dérivation modulé Download PDFInfo
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- WO2010020715A1 WO2010020715A1 PCT/FR2009/000946 FR2009000946W WO2010020715A1 WO 2010020715 A1 WO2010020715 A1 WO 2010020715A1 FR 2009000946 W FR2009000946 W FR 2009000946W WO 2010020715 A1 WO2010020715 A1 WO 2010020715A1
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- WIPO (PCT)
- Prior art keywords
- zone
- lines
- synchronicity
- extract
- raffinate
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Classifications
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- 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
- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
- B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
- B01D15/1814—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns recycling of the fraction to be distributed
- B01D15/1821—Simulated moving beds
- B01D15/1828—Simulated moving beds characterized by process features
- B01D15/1835—Flushing
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/06—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with moving sorbents or sorbents dispersed in the oil
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/12—Recovery of used adsorbent
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1096—Aromatics or polyaromatics
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
Definitions
- the invention relates to the field of separations of natural or chemical products, which can hardly be separated by distillation.
- a family of methods, and associated devices, known as methods, or devices for simulated moving bed separation, are then used, either in simulated countercurrent or in simulated co-current, which will be referred to hereinafter as the generic name "LMS".
- LMS simulated co-current
- LMS liquid crystal separation
- a column operating in simulated moving bed comprises at least three zones, and possibly four or five, each of these zones being constituted by a certain number of successive beds, and each zone being defined by its position lying between a point d feed and a draw point.
- an LMS column is fed with at least one charge F to be fractionated and a desorbent D (sometimes called an eluent), and at least one raffinate R and an extract E are withdrawn from said column.
- D sometimes called an eluent
- the feed and withdrawal points are modified over time, typically shifted in the same direction by a value corresponding to a bed.
- Zone 1 zone of desorption of the compounds of the extract, between the injection of the desorbent D and the extraction of the extract E,
- Zone 2 zone of desorption of the compounds of the raffinate, between the taking of the extract E and the injection of the charge to be fractionated F,
- Zone 3 adsorption zone of the compounds of the extract, between the injection of the feedstock and the withdrawal of the raffinate R 1
- the LMS devices typically comprise at least one column (and often two columns), divided into several successive adsorbent beds Aj, said beds being separated by trays.
- each plate P comprising one, two or four chambers for performing the sequential operations of feeding the feed or injection of the desorbent and extracting the raffinate or extract.
- Only one chamber can perform the 4 operations, but the present invention relates to columns with 2 chambers per tray.
- Several solutions are possible for the use of the two chambers, each of which can be used for injection or withdrawal of one or more streams.
- a first chamber can perform charge or desorbent injection operations, and the other chamber performs raffinate or extract extraction operations.
- Another possible scenario is to use a chamber for the injection of the feedstock and the withdrawal of the raffinate, the other managing the injection of desorbent and withdrawal of the extract.
- the controlled means for dispensing and extracting fluids from an LMS are typically one of two major types of technology: - either, for each tray, a plurality of all or nothing controlled valves for feeding or fluid withdrawal, these valves being typically located in the immediate vicinity of the corresponding plate.
- Each tray P typically comprises at least 4 2-way valves, controlled in all or nothing, to respectively perform the fluid supply F and D and withdrawing fluids E and R.
- the present invention is in the context of LMS units using a plurality of valves to ensure the supply and withdrawal of the different fluids.
- Each of the trays P 1 typically comprises a plurality of distributor-mixer-extractor panels, called "DME trays" fed by lines or distribution / extraction systems.
- the trays can be of any type and any geometry. They are generally divided into panels, corresponding to adjacent sectors of the section of the column, for example angular sector panels such as those shown in US Pat. No. 6,537,451, FIG. 8, or parallel sector panels as described in US Pat. US 6,797,175.
- the separation column according to the invention comprises DME trays of parallel sector type and asymmetrical feeds.
- each of the beds requires a collection of the main flow from the previous bed, the possibility of injecting an ancillary fluid or secondary fluid while mixing the best possible two fluids, or the possibility of taking a portion of the collected fluid , extract it to send it to the outside of the device and also to redistribute a fluid on the next bed.
- a generic problem with all the LMS devices is to minimize the pollution generated by the liquid in the different zones of the fluid supply and draw-off circuit of the trays, during modifications of the feed points and racking during operation of the LMS.
- This first scan variant typically performs short-duration scans with a high concentration gradient. These scans are of short duration precisely to limit the effects of the discontinuities of composition.
- Another solution consists, as described in US Pat. Nos. 5,972,224 and 6,110,364, of passing a majority of the main stream into the column and a minority of this stream (typically from 1% to 20% of the main stream). ) outwards by external branch lines between successive trays.
- This scanning of the distribution / extraction system at a plateau level by a flow from the upper plateau is typically done continuously, so that the lines and zones of the distribution / extraction system are no longer "dead", but constantly swept.
- Such a system with continuous scanning via branch lines is presented in FIG. 2 of the patent FR 2,772,634.
- the branch lines are generally small in diameter and include a small diameter valve, which reduces the cost of the system.
- US patent teaching 5,972,224 and US 6,110,364 it is sought that the distribution / extraction system of a given plate is swept by liquid having a composition very close to that of the displaced liquid (liquid present in the system of distribution, or circulating at the plateau). Thus, mixtures of fluids of different composition are minimized, and the discontinuities in composition are reduced.
- patents US 5,972,224 and US 6,110,364 recommend implementing scanning rates in the branches so that the transit speed in each branch is substantially the same as the forward speed of the gradient of concentration in the main stream of the LMS. This is called “synchronous" or "synchronous rate” scanning.
- the different lines and capacities are scanned by a fluid which has a composition substantially identical to that of the liquid therein, and the circulating liquid is reintroduced into a bypass at a point where the composition of the main stream is substantially identical.
- the sweeps are therefore synchronous long-term concentration gradient low or zero.
- a scan is said to be "synchronous" when the scanning rate QS i / i + 1 from a plate P 1 to the following plate P i + 1 is equal to V / ST in which V is the cumulative volume of the distribution systems of trays Pi (ie V 1 ) and P 1 + 1 (ie V i +1 ), and the volume of the bypass line between these two trays (ie VL i / i + 1 ) and ST is the permutation period of the LMS between two successive permutations of the feeds / extractions.
- V 1 Volume of the dispensing / extraction system of the starting tray P 1 ;
- V 1 + 1 Volume of the distribution / extraction system of the arrival tray P i + 1 ;
- - VL 1Z i +1 Volume of the branch line between P 1 and P 1 + 1 ;
- the implementation of the synchronous scanning is typically carried out using a scan with a controlled flow rate, adapted to each zone, ranging from 50% to 150% of the synchronous rate in these zones, and ideally 100% of the flow rate.
- synchronous The flows in the branch lines of the 4 LMS zones are controlled by control means in each branch line.
- the skilled person could use a rate of 90% of the synchronous rate in all these areas, or 110%, or any other value close to 100% of the synchronous rate.
- the skilled person following the teaching of the aforementioned patent will naturally choose to control flow rates in the 4 zones that correspond exactly to the synchronous rate (100% of the synchronous rate).
- LMS separation device An example of a LMS separation device of great industrial importance is the separation of aromatic C8 cuts to produce purity paraxylene commercial, typically at least 99.7% by weight, and a raffinate rich in ethylbenzene, orthoxylene and metaxylene.
- Figure 1 shows a succession of 3 beds Pi -1 , P
- the effluent withdrawal lines (raffinate or extract) are located upstream of the isolation valve of the bypass line.
- the supply lines (charge or desorbent) are located downstream of the isolation valve.
- FIG. 2a represents an injection situation
- FIG. 2b shows a withdrawal situation in a configuration of the column according to FIG. 1.
- FIG. 3 shows the variations in the performance of the LMS, measured in terms of efficiency (R) in PX at desorbent flow rate, charge rate, product paraxylene purity and fixed permutation period, as a function of the synchronicity (S) of all unclosed bypass lines for each zone, maintaining 100% synchronicity for all non-closed bypass lines in the other zones.
- Zone 1 is represented by the diamond curve.
- Zone 2 is represented by the square curve.
- Zone 3 is represented by the triangle curve.
- Zone 4 is represented by the circle curve.
- FIG. 4 represents a succession of 3 beds P M , P 1, P 1 + 1 forming part of a simulated moving bed column (LMS).
- the effluent withdrawal lines (raffinate or extract) are located downstream of the bypass line isolation valve.
- the supply lines (charge or desorbent) are located upstream of the isolation valve.
- FIG. 5a represents an injection situation
- FIG. 5b shows a withdrawal situation in a configuration of the column according to FIG. 4.
- FIG. 6 shows the variations in the performance of the LMS, measured in terms of efficiency (R) in PX at desorbent flow rate, charge flow rate, product paraxylene purity and fixed permutation period, as a function of the synchronicity (S) of all unclosed bypass lines for each zone, maintaining 100% synchronicity for all non-closed bypass lines in the other zones.
- Zone 1 is represented by the diamond curve.
- Zone 2 is represented by the square curve.
- Zone 3 is represented by the triangle curve.
- Zone 4 is represented by the circle curve.
- the object of the invention is to improve the performance of a simulated bed separation process compared with the teaching of US Pat. Nos. 5,972,224 and US 6,110,364.
- the invention also relates to an improved simulated moving bed separation device using a plurality of 2-way on / off controlled valves for feeding and extracting LMS process fluids, and performing long-duration gradient scans. low or no concentration.
- the present invention defines on each zone of the LMS unit a range of bypass flow having a certain degree of over-synchronicity specific to the area in question. This results in a complex optimum of the set of derivation rates, which depends both on the area of the LMS considered, and as will be seen in the detailed description, the number of closed branch lines in said area. This technical problem is totally absent from the teaching of the prior art and constitutes an increase of knowledge in the control of LMS type processes.
- the present invention thus relates to a simulated moving bed separation (LMS) method of a load F in an LMS device having at least one column, said column being composed of a plurality of adsorbent beds separated by trays P, each comprising a distribution / extraction system, in which the feedstock F and a desorbent D are fed, and at least one extract E and at least one raffinate R are withdrawn, the feed and withdrawal points being offset during the time of a value corresponding to an adsorbent bed with a permutation period ST, and determining a plurality of operating zones of the LMS, and in particular the following 4 main zones:
- a desorption zone 2 for the raffinate compounds between the withdrawal of the extract E and the supply of the feed F;
- each of the branch lines L w + 1 comprises automated control means the sweep rate, the degree of opening of said regulating means being defined by the following two rules:
- VLy 1 + 1 denotes the volume of the branch line between Pj and P i + 1 ; and ST designating the permutation period.
- the present invention also relates to a method for adjusting the scanning rates for each zone constituting the LMS column which can be defined as follows:
- the process according to the present invention is more particularly applicable to the separation of paraxylene or metaxylene in a mixture of C8 aromatic hydrocarbons.
- these two examples of application are in no way limiting and other applications are possible, especially in the field of separation of normal and iso paraffins or normal and iso olefins.
- the invention proposes a simulated moving bed separation (LMS) method of a load F in an LMS device having at least one column, said column being composed of a plurality of adsorbent beds separated by trays P, each comprising a distribution / extraction system, in which the feedstock F is fed with a desorbent D, and at least one extract E is withdrawn, and at least one raffinate R , the feeding points and withdrawal being shifted over time by a value corresponding to an adsorbent bed with a permutation period ST and determining a plurality of operating zones of the LMS 1 and in particular the following main zones:
- LMS simulated moving bed separation
- each of these branch lines Ui +1 comprises automated means for regulating the sweep rate.
- the external branch line L w + 1 directly joining two successive plates Pi, P 1 + 1 is said to belong to a zone when the bed between the plates P 1 and P i + i belongs to said zone.
- a bypass line is said to be closed when the flow rate in this bypass line is zero. This closure can be achieved using any technical means for canceling the flow in the bypass line such as including an on-off valve, a flow control valve or a non-return valve.
- the degree of opening of said regulating means is defined by the following two rules:
- Vj denotes the volume of the distribution / extraction system of the starting tray Pj
- V i + 1 denotes the volume of the distribution / extraction system of the arrival tray P i + 1
- VLi / i +1 denotes the volume of the branch line between P 1 and P 1 + 1 ; and ST designating the permutation period.
- the sweeping rate of the branch lines in a given operating zone is essentially related to the presence or not of at least one closed bypass line in said zone.
- the over-synchronicity S of the non-closed bypass lines of an area where there is at least one closed bypass line is defined by the ratio of the number of closed bypass lines (nf) in the area under consideration to the number total of the diversion lines of the zone (nt), ie on the number of beds of the zone considered.
- the branch line to be closed for injection or withdrawal depends in particular on the position of the injection and withdrawal lines with respect to the bypass line closure device.
- the position of an element (plate, bed, valve, valve, ...) downstream from another element is defined with respect to the direction of the progress of the withdrawal and introduction points during the permutation sequences. .
- LMS unit consisting of 24 beds, length 1, 1 m and internal radius 3.5 m, with a charge injection, an injection of desorbent (which can also be called eluent or solvent), a withdrawal of extract and a raffinate withdrawal.
- desorbent which can also be called eluent or solvent
- the trays are two mixing chambers, one being an injection box (filler and desorbent), the other being a tundish (extract and raffinate).
- the effluent withdrawal lines (raffinate or extract) are located upstream of the bypass line isolation valve (it will be more simply called "upstream of the bypass line valve").
- the supply lines (charge or desorbent) are located downstream of the isolation valve ( Figure 1).
- the beds are distributed according to the configuration 5/9/7/3 ie that the distribution of the beds is as follows:
- the adsorbent employed is a BaX zeolite, and the eluent is paradiethylbenzene.
- the temperature is 175 ° C., and the pressure is 15 bars.
- the filler is composed of 20% paraxylene, 24% orthoxylene, 51% metaxylene and 5% ethylbenzene.
- the permutation period used is 70.8 seconds.
- the yield of PX is the ratio between the amount of PX withdrawn in the extract and the amount of PX injected.
- Zone 1 is represented by the diamond curve.
- Zone 2 is represented by the square curve.
- Zone 3 is represented by the triangle curve.
- Zone 4 is represented by the circle curve.
- the four optimum synchronicity values are simultaneously imposed, ie 102% in zone 1, 110% in zone 2, 105% in zone 3 and 140% in zone 4.
- Example 2 An LMS unit consisting of 15 beds of length 1.1 m and of internal radius 3.5 m is now considered, with a charge injection, an injection of desorbent (also called eluent or solvent), extraction of extract and a raffinate withdrawal.
- desorbent also called eluent or solvent
- the trays are two mixing chambers, one being an injection box (filler and desorbent), the other being a tundish (extract and raffinate).
- this type of bypass line leads to: - close two branch lines in zone 1 (injection of the desorbent by a line connected to the bypass line of the first bed of the zone and extraction of the extract by a line connected to the bypass line of the last bed of the zone) ,
- zone 3 injection of the load by a line connected to the bypass line of the first bed of the zone and withdrawal of the raffinate by a line connected to the bypass line of the last bed of the zone).
- the beds are distributed according to the configuration 3/6/4/2 that is to say that the distribution of the beds is as follows: - 3 beds in zone 1,
- the adsorbent employed is a BaX zeolite, and the eluent is paradiethylbenzene.
- the temperature is 175 ° C., and the pressure is 15 bars.
- the filler is composed of 20% paraxylene, 24% orthoxylene, 51% metaxylene and 5% ethylbenzene.
- the permutation period used is 113.28 seconds.
- a solvent ratio S / F 1, 1.
- Zone 1 is represented by the diamond curve.
- Zone 2 is represented by the square curve.
- Zone 3 is represented by the triangle curve.
- Zone 4 is represented by the circle curve.
- the yield of PX is the ratio between the amount of PX withdrawn in the extract and the amount of PX injected.
- the four optimal synchronicity values are simultaneously imposed, ie 170% in zone 1, 105% in zone 2, 133% in zone 3 and 100% in zone 4.
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
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US13/059,773 US8123952B2 (en) | 2008-08-19 | 2009-07-29 | Process and device for simulated moving bed separation with a modulated by-pass fluid flow |
CN200980132189.7A CN102123775B (zh) | 2008-08-19 | 2009-07-29 | 具有调制的旁通流体流的模拟移动床分离方法和装置 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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FR08/04.637 | 2008-08-19 | ||
FR0804637A FR2935100B1 (fr) | 2008-08-19 | 2008-08-19 | Procede et dispositif de separation en lit mobile simule a debit de fluide de derivation module |
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WO2010020715A1 true WO2010020715A1 (fr) | 2010-02-25 |
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PCT/FR2009/000946 WO2010020715A1 (fr) | 2008-08-19 | 2009-07-29 | Procédé et dispositif de séparation en lit mobile simulé à débit de fluide de dérivation modulé |
Country Status (6)
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US (1) | US8123952B2 (fr) |
KR (1) | KR101614974B1 (fr) |
CN (1) | CN102123775B (fr) |
FR (1) | FR2935100B1 (fr) |
TW (1) | TWI454302B (fr) |
WO (1) | WO2010020715A1 (fr) |
Families Citing this family (9)
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FR2935100B1 (fr) * | 2008-08-19 | 2011-03-18 | Inst Francais Du Petrole | Procede et dispositif de separation en lit mobile simule a debit de fluide de derivation module |
FR2944215B1 (fr) * | 2009-04-10 | 2011-04-01 | Inst Francais Du Petrole | Procede et dispositif de separation en lit mobile simule comportant des lignes de derivation d'un lit sur deux et a debit de fluide de derivation module |
FR2956037B1 (fr) * | 2010-02-11 | 2012-02-17 | Inst Francais Du Petrole | Procede et dispositif de separation en lit mobile simule comportant des lignes de derivation d'un lit sur deux avec debits de balayage controles lors des injections et des soutirages |
US9017558B2 (en) * | 2011-12-15 | 2015-04-28 | Uop Llc | System and process for recovering products using simulated-moving-bed adsorption |
FR3066401B1 (fr) * | 2017-05-17 | 2021-04-23 | Ifp Energies Now | Procede de separation des xylenes en lit mobile simule et conditions operatoires optimisees pour les unites traitant des charges riches en paraxylene |
FR3082755B1 (fr) | 2018-06-20 | 2022-12-30 | Ifp Energies Now | Procede et dispositif de separation en lit mobile simule a nombre de lits reduit avec debit de fluide de derivation |
FR3082754B1 (fr) * | 2018-06-20 | 2022-12-30 | Ifp Energies Now | Procede et dispositif de separation en lit mobile simule a debit de fluide de derivation |
US11027221B2 (en) | 2018-10-19 | 2021-06-08 | Uop Llc | Process for a dual extract flush |
FR3116443B1 (fr) | 2020-11-24 | 2023-07-28 | Ifp Energies Now | Procédé et dispositif de production de paraxylene en lit mobile simulé réactif avec lignes de court-circuit reactives |
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FR2794836B1 (fr) * | 1999-06-09 | 2001-08-03 | Inst Francais Du Petrole | Vanne rotative amelioree |
FR2833499B1 (fr) * | 2001-12-19 | 2004-08-20 | Inst Francais Du Petrole | Dispositif d'injection d'un fluide devie dans un procede de separation en lit mobile simule |
FR2935101B1 (fr) * | 2008-08-19 | 2011-04-08 | Inst Francais Du Petrole | Procede et dispostif de separation en lit mobile simule a debit de fluide de derivation non regule automatiquement |
FR2935100B1 (fr) * | 2008-08-19 | 2011-03-18 | Inst Francais Du Petrole | Procede et dispositif de separation en lit mobile simule a debit de fluide de derivation module |
FR2944215B1 (fr) * | 2009-04-10 | 2011-04-01 | Inst Francais Du Petrole | Procede et dispositif de separation en lit mobile simule comportant des lignes de derivation d'un lit sur deux et a debit de fluide de derivation module |
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2008
- 2008-08-19 FR FR0804637A patent/FR2935100B1/fr active Active
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2009
- 2009-07-29 CN CN200980132189.7A patent/CN102123775B/zh active Active
- 2009-07-29 US US13/059,773 patent/US8123952B2/en active Active
- 2009-07-29 KR KR1020117006092A patent/KR101614974B1/ko active IP Right Grant
- 2009-07-29 WO PCT/FR2009/000946 patent/WO2010020715A1/fr active Application Filing
- 2009-08-17 TW TW098127631A patent/TWI454302B/zh active
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US5912395A (en) * | 1997-03-12 | 1999-06-15 | Uop Llc | Raffinate line flush in simulated continuous moving bed adsorptive separation process |
US5972224A (en) * | 1997-12-22 | 1999-10-26 | Hotier; Gerard | Process and device for improving the purity of a product in a simulated fluid bed |
US6110364A (en) * | 1997-12-22 | 2000-08-29 | Institut Francais Du Petrole | Device for improving the purity of a product in a simulated fluid bed |
US20050269268A1 (en) * | 2004-05-25 | 2005-12-08 | Gerard Hotier | Simulated moving bed separation process and device |
Also Published As
Publication number | Publication date |
---|---|
CN102123775A (zh) | 2011-07-13 |
KR101614974B1 (ko) | 2016-04-22 |
TW201016292A (en) | 2010-05-01 |
CN102123775B (zh) | 2014-05-28 |
US20110201865A1 (en) | 2011-08-18 |
TWI454302B (zh) | 2014-10-01 |
FR2935100B1 (fr) | 2011-03-18 |
KR20110043768A (ko) | 2011-04-27 |
US8123952B2 (en) | 2012-02-28 |
FR2935100A1 (fr) | 2010-02-26 |
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