[go: up one dir, main page]

EP1888193A1 - Procédé de séparation - Google Patents

Procédé de séparation

Info

Publication number
EP1888193A1
EP1888193A1 EP06722799A EP06722799A EP1888193A1 EP 1888193 A1 EP1888193 A1 EP 1888193A1 EP 06722799 A EP06722799 A EP 06722799A EP 06722799 A EP06722799 A EP 06722799A EP 1888193 A1 EP1888193 A1 EP 1888193A1
Authority
EP
European Patent Office
Prior art keywords
stripper
distillation
fed
stream
column
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Withdrawn
Application number
EP06722799A
Other languages
German (de)
English (en)
Inventor
Stephan Rüdiger BLUM
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
White Fox Technologies Ltd
Original Assignee
White Fox Technologies Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by White Fox Technologies Ltd filed Critical White Fox Technologies Ltd
Publication of EP1888193A1 publication Critical patent/EP1888193A1/fr
Withdrawn legal-status Critical Current

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
    • B01D3/001—Processes specially adapted for distillation or rectification of fermented solutions
    • B01D3/003—Rectification of spirit
    • B01D3/004—Rectification of spirit by continuous methods
    • 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
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • 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
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • B01D3/146—Multiple effect distillation
    • 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
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • the invention relates to a separation process, in particular a distillation of ethanol as a final product from a mash.
  • Distillation column the mash is evaporated, whereby solid components can be removed as bottoms with water. A part of this bottom product is usually recycled to the distillation column after heating (reboiler).
  • the first vaporous distillate, still containing water, ethanol and fusel oil is, if necessary. via a collecting and mixing tank, fed to a second distillation column, which is designed as a rectification column.
  • a second distillation column which is designed as a rectification column.
  • Rectification carried a more extensive separation, in which the fuselages are discharged in a side stream.
  • a small proportion is returned to the rectification column again after heating (reboiler) and otherwise also removed, so that it exudes from the production process.
  • the distillate of the second distillation column still containing water and ethanol, can be partially recycled to the first and second distillation column, if necessary. over the already mentioned collection tank.
  • the predominant amount of the ethanol-water mixture constituting the second distillate of about 95% ethanol and 5% water undergoes a final dehydration to obtain as pure as possible a purity of 99 to 99.8% ethanol.
  • This last dehydration occurs by means of molecular sieves, in which crystalline zeolites adsorb spongy H 2 O molecules.
  • the zeolites of a molecular sieve are rapidly saturated in water. For a constant dehydration therefore water-saturated zeolites must be regenerated.
  • molecular sieves are regularly used in pairs. It can then be provided by a first active molecular sieve high purity ethanol, which can also be used for the regeneration of a second, passive molecular sieve. In the regeneration of a passive molecular sieve, the ethanol used there can be recycled to a distillation column, this reflux can be about 30% of the obtained pure ethanol of the active molecular sieve.
  • the constant change of the pressure load of the molecular sieves causes a dusty abrasion of the filling material. This burdens downstream plant stages, which must be completely replaced periodically. This is reflected adversely in investment and operating costs.
  • the object of the invention is to provide a separation process by means of which the economic efficiency, in particular in the dehydrogenation of ethanol from a mash, is markedly improved.
  • the separation method according to the invention has a number of advantages.
  • the energetic concept of a distillation plant was determined by the design of the stripper, so according to the invention the first distillation stage is operated according to the energetic specifications of the rectification column, which can thus be operated optimally. It thus determines the energy balance of the rectification column essentially that of the first distillation stage.
  • the feed is merely separated into two streams, so that both streams have similar energetic and / or chemical potentials, which streams are then fed to a respective distillation column. Also, most of the volume flow of the two streams will move in the same order of magnitude, each about half, but it may be appropriate in individual cases, depending on the configuration of the first and second distillation stage to specify the volume flows differently.
  • Process flow back distillation column is returned to a stripper as a front, improves the energy balance per liter of end product over conventional methods already by about 40%. If the feed is split equally into two streams and two strippers are provided in the first distillation stage, a stream is alternatively fed to each stripper, wherein then preferably the volume flows of the two streams are also about the same size. Is then still thought in a preferred embodiment, that a bottom product of a preferably operated at high pressure first stripper is fed to a preferably subjected to a lower pressure second stripper and further in that the distillate of the rectification in a
  • Membrane filtration device is cleaned, the energy balance improves by more than 60%
  • Retentate for example, a membrane separator in a stream of a stripper and the permeate are fed in a stream of a rectification column.
  • this stream with the elevated temperature becomes, in particular, a retentate, for example, a membrane separation device
  • Stripper preferably supplied at the top and is with the distillate of this stripper to the rectification.
  • the feed of the stream of lower temperature then takes place as permeate, for example, in a lower region of the stripping column.
  • a vapor phase generating separation device may be provided as an evaporator, in particular by a relaxation of a vapor phase generating or as a distillation column whose distillate is then present with the distillate of a stripper to the rectification and their bottom product to the stripper next a further stream of the feed is still supplied.
  • Separation method according to the invention used in an optimal manner, since the operation of the first distillation stage is completely determined by the rectification and the heat recovery from a final product.
  • distillation columns are preferably run at different operating pressures, in particular with those which allow optimal heat recovery. This ensures the lowest possible heat loss.
  • the heat recovered from the heat recovery from the final product is fed into the reboiler circuit of the operated at a medium energy level distillation column.
  • the heat recovered from the final product can be significantly increased if the concentration of the final product in a feed is at least 20%. It is then possible to significantly reduce the energy input of the overall system in relation to the amount of final product obtained. Such an increase, for example, of an ethanol content of about 10% in one feed can be achieved by a corresponding fermentation technique. Alternatively, upstream processes are possible, for example, that the feed to a previously explained
  • Membrane separation process has an increased proportion of the final product. As a result of these measures, the proportion of the end product in the entire system increases significantly. These measures further lead to a significantly increased output of the end product and thus also to an increased heat recovery, which can then be reintroduced into the process.
  • Rectifying be purified in molecular sieves or preferably in a membrane separation process in a filtration device.
  • a regenerate of this a rectification in the Process flow subsequent filter device is fed into a stripper again.
  • Fig. 3 a further arrangement of three
  • Fig. 4 variants of a feed of a Renegats a
  • Fig. 9 a splitting into a liquid and a vapor phase by means of a distillation column and 10: a variant of this.
  • two strippers 1, 2 connected in parallel form a first distillation stage for a separation process, for example for the distillation of ethanol from a beer mash whose inflow 3, comprising about 11.5% ethanol, divided into two streams 40, 41 is more similar chemical and energetic potentials the two strippers 1,2 is fed in equal parts.
  • the distillate 4 of the two strippers 1,2 is fed together to a rectification column 5.
  • distillate 6 is purified by molecular sieves 7 and discharged as, for example, high-purity methanol of a purity of 99.6% as product stream 8.
  • the rectification column 5 is driven to the highest energy level. For example, approx. 18,000 kW of primary energy 9 are fed in, indicated by the heat exchanger in the reboiler cycle of the rectification column 5. An excess of energy of about 9,800 kW is present, which is indicated via a heat exchanger 10 in the return 12 of the rectification column 5 Part is fed into the stripper 2, so that it can be driven at a medium energy level.
  • Required for the operation of the stripper 2 are only about 8,500 kW, so that about 1,300 kW unused can be discharged from the circulation, indicated by the heat exchanger 11 in the return 12th
  • the stripper 1 is operated with the excess energy of the stripper 2, for which approximately 6,500 kW are required with a surplus of about 6,900 kW of the stripper 2, so that here again about 400 kW of excess energy can be discharged.
  • a portion of the excess energy can be used for the regeneration and operation of the molecular sieves 7.
  • distillate is ethanol
  • a production rate of 19.57 l / h can be achieved with 1.58 kg steam / 1 ethanol in this calculation example.
  • distillation columns are driven 1,2,5 with graduated, different pressures.
  • an optimal operation of the distillation columns 1,2 and 5 is possible with an optimal energy transfer.
  • both strippers 19, 20 are essentially to be operated in accordance with the specifications of the preceding exemplary embodiment.
  • the feed 25 contains a proportion of the end product, for example ethanol, at a level of 20%.
  • the amount of distillate 26 of the two strippers 27, 28 will be significantly increased, with slightly increased energy requirements and equal working pressures.
  • the rectification column 29 is acted upon at unchanged pressure with a primary energy 30 of about 14,500 kW, of which in the return 31 about 2,500 kW for the operation of the stripper 28 are available.
  • the distillate 32 supplied to a membrane filtration device 33 has an energy content of about 12,500 kW in the case of, for example, an ethanol content of 80%.
  • Permeats 34 flow to the rectification column 29 thereof about 4,700 kW. This leaves about 7,800 kW in the product stream 35, which, indicated by the heat exchanger 36, can be fed into the reboiler circuit 37 for the operation of the stripper 28, the here an energy requirement of Approximately 9,700 kW has an excess of 8,300 kW for the operation of the stripper 27, which requires only about 8,050 kW. Thus, enough energy is provided for the energetically cascaded strippers 27, 28, 29. In addition, the product stream 35 increases significantly to 30.46 l / h. This with an energy input of 0.83 kg of steam per liter of ethanol produced.
  • Figure 4 shows two strippers 42,43, which are acted upon by two similar streams 44,45 of an inlet 46.
  • the distillate 47 of the two strippers 42, 43 is fed to a rectification column 48 and its distillate 39 to a filtration device 49.
  • a renewed feed of a regenerate 50 of the filter 49, in particular again a membrane filtration device is carried out in this embodiment not in the rectification column 48, but in one of the stripper 42,43, indicated by dashed lines in the drawing.
  • both strippers 42, 43 can also be charged with the regenerate 50.
  • the streams 44, 45 of the same chemical and energetic potential are introduced by way of example in an upper region of the columns of the strippers 42, 43, and the distillate 47 of the strippers 42, 43 is introduced approximately in the center of the rectification column 48.
  • the two streams 53, 54 are fed into the stripper 51 and the rectification column 52.
  • the volume flows of the two streams 53, 54 also differ significantly from each other.
  • the bottom product 55 of the rectification column 52 is from the
  • FIG. 6 shows the division of an inlet 56 into two streams 57, 58 by a separating device 59.
  • Separator 59 formed for example by sieves, filters, membranes, centrifuges or the like, provides on the one hand for a significant increase in the proportion of the final product, for example. Ethanol, in the stream 57, which is supplied to a stripper 60.
  • this stream 57 will usually only have a low solids content or even be solids-free.
  • Suitably designed separating devices 61 may be, for example, evaporators and, in particular, strippers 85, for example, shown in FIG. 9.
  • Figure 8 shows a variant in which an inlet 66 is divided into two similar streams 67,68. The stream 68 is fed directly to a stripper 86.
  • the other stream 67 is again divided by a separating device 69 into two further streams 70, 71, of which the stream 70 present in particular in the vapor phase is supplied again to the stripper 86 on the top side and is present with the distillate at the rectification column 87.
  • the stream 71 can still be supplied to the stripper 86 and thus remain within the process.
  • a stripper 85 is provided as the separating device. While the distillate 72 of the stripper 85 of elevated temperature, in particular vapor phase, a stripper 73 is fed to the top and is present with the distillate at the rectification column 88, a feed of the bottom product 74 of the stripper 85 in the stripper 73rd
  • the stripper 73 is further supplied with a further, branched stream 75 of the feed still.
  • the distillation column 65 is driven at a higher pressure than the stripper 73.
  • FIG. 10 shows how two strippers 79, 80 are acted upon by an inlet 76, divided into two identical streams 77, 78.
  • Their distillate 81 is, for example, summarized as shown, fed to a further distillation column 82. Its bottom product 83 is then introduced into a rectification column 84.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)

Abstract

L'invention concerne un procédé de séparation, en particulier un procédé pour distiller l'éthanol contenu dans une trempe, en tant que produit final. Selon ce procédé, un courant d'alimentation est introduit dans un premier étage de distillation comportant au moins une colonne de distillation (colonne de strippage), et le distillat du premier étage de distillation est introduit dans une deuxième colonne de distillation (colonne de rectification). Selon l'invention, le courant d'alimentation est divisé en deux courants (40, 41) au niveau de deux colonnes de distillation (1, 2), de manière que la colonne de rectification (5) atteigne un bilan énergétique prédéterminé.
EP06722799A 2005-04-20 2006-04-19 Procédé de séparation Withdrawn EP1888193A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102005018508 2005-04-20
PCT/DE2006/000680 WO2007095875A1 (fr) 2005-04-20 2006-04-19 Procédé de séparation

Publications (1)

Publication Number Publication Date
EP1888193A1 true EP1888193A1 (fr) 2008-02-20

Family

ID=36791774

Family Applications (1)

Application Number Title Priority Date Filing Date
EP06722799A Withdrawn EP1888193A1 (fr) 2005-04-20 2006-04-19 Procédé de séparation

Country Status (9)

Country Link
US (1) US20080135396A1 (fr)
EP (1) EP1888193A1 (fr)
JP (1) JP2008536503A (fr)
CN (1) CN101163528A (fr)
BR (1) BRPI0610023A2 (fr)
CA (1) CA2605570A1 (fr)
DE (1) DE112006001685A5 (fr)
RU (1) RU2007142494A (fr)
WO (1) WO2007095875A1 (fr)

Families Citing this family (116)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100536974C (zh) * 2003-04-25 2009-09-09 2S－精密系统有限公司 蒸馏方法
US8002874B2 (en) * 2007-03-06 2011-08-23 Membrane Technology And Research, Inc. Liquid-phase and vapor-phase dehydration of organic/water solutions
DE102007043998A1 (de) * 2007-09-14 2009-03-19 White Fox Technologies Ltd. Vorrichtung für die Ethanolgewinnung
NO328571B1 (no) * 2007-10-12 2010-03-22 Epcon Energy & Process Control Fremgangsmate ved avvanning av en blanding av overveiende etanol og vann
US8546622B2 (en) 2008-07-31 2013-10-01 Celanese International Corporation Process for making ethanol from acetic acid using acidic catalysts
US8309773B2 (en) 2010-02-02 2012-11-13 Calanese International Corporation Process for recovering ethanol
US8304586B2 (en) 2010-02-02 2012-11-06 Celanese International Corporation Process for purifying ethanol
US8552226B2 (en) 2010-02-02 2013-10-08 Celanese International Corporation Process for heat integration for ethanol production and purification process
US8318988B2 (en) 2010-05-07 2012-11-27 Celanese International Corporation Process for purifying a crude ethanol product
US8575403B2 (en) 2010-05-07 2013-11-05 Celanese International Corporation Hydrolysis of ethyl acetate in ethanol separation process
US8314272B2 (en) 2010-02-02 2012-11-20 Celanese International Corporation Process for recovering ethanol with vapor separation
US8552225B2 (en) 2010-02-02 2013-10-08 Celanese International Corporation Process for vaporizing acetic acid for hydrogenation processes to produce ethanol
US8222466B2 (en) 2010-02-02 2012-07-17 Celanese International Corporation Process for producing a water stream from ethanol production
US8858659B2 (en) 2010-02-02 2014-10-14 Celanese International Corporation Processes for producing denatured ethanol
US8344186B2 (en) 2010-02-02 2013-01-01 Celanese International Corporation Processes for producing ethanol from acetaldehyde
US8394985B2 (en) * 2010-02-02 2013-03-12 Celanese International Corporation Process for producing an ester feed stream for esters production and co-production of ethanol
US8552224B2 (en) 2010-05-07 2013-10-08 Celanese International Corporation Processes for maximizing ethanol formation in the hydrogenation of acetic acid
US8747492B2 (en) 2010-02-02 2014-06-10 Celanese International Corporation Ethanol/fuel blends for use as motor fuels
US8680343B2 (en) 2010-02-02 2014-03-25 Celanese International Corporation Process for purifying ethanol
US8394984B2 (en) 2010-02-02 2013-03-12 Celanese International Corporation Process for producing an ethyl acetate solvent and co-production of ethanol
US8460405B2 (en) 2010-02-02 2013-06-11 Celanese International Corporation Ethanol compositions
US8932372B2 (en) 2010-02-02 2015-01-13 Celanese International Corporation Integrated process for producing alcohols from a mixed acid feed
US8541633B2 (en) 2010-02-02 2013-09-24 Celanese International Corporation Processes for producing anhydrous ethanol compositions
US8728179B2 (en) 2010-02-02 2014-05-20 Celanese International Corporation Ethanol compositions
US8668750B2 (en) 2010-02-02 2014-03-11 Celanese International Corporation Denatured fuel ethanol compositions for blending with gasoline or diesel fuel for use as motor fuels
US8680342B2 (en) 2010-05-07 2014-03-25 Celanese International Corporation Process for recovering alcohol produced by hydrogenating an acetic acid feed stream comprising water
US8704011B2 (en) 2010-05-07 2014-04-22 Celanese International Corporation Separating ethanol and ethyl acetate under low pressure conditions
US8604255B2 (en) 2010-05-07 2013-12-10 Celanese International Corporation Process for recovering ethanol with sidedraws to regulate C3+ alcohols concentrations
US8754267B2 (en) 2010-05-07 2014-06-17 Celanese International Corporation Process for separating acetaldehyde from ethanol-containing mixtures
US8569551B2 (en) 2010-05-07 2013-10-29 Celanese International Corporation Alcohol production process integrating acetic acid feed stream comprising water from carbonylation process
US8704010B2 (en) 2010-05-07 2014-04-22 Celanese International Corporation Alcohol production process with impurity removal
US8575404B2 (en) 2010-05-07 2013-11-05 Celanese International Corporation Process for recycling gas from acetic acid hydrogenation
US9017523B2 (en) 2010-06-14 2015-04-28 Pinnacle Engineering, Inc. Packed bed scrubber using a fusel oil solvent
US8859827B2 (en) 2011-11-18 2014-10-14 Celanese International Corporation Esterifying acetic acid to produce ester feed for hydrogenolysis
US8846988B2 (en) 2010-07-09 2014-09-30 Celanese International Corporation Liquid esterification for the production of alcohols
US9272970B2 (en) 2010-07-09 2016-03-01 Celanese International Corporation Hydrogenolysis of ethyl acetate in alcohol separation processes
SG186066A1 (en) 2010-07-09 2013-01-30 Celanese Int Corp Finishing reactor for purifying ethanol
US8809597B2 (en) 2010-07-09 2014-08-19 Celanese International Corporation Separation of vapor crude alcohol product
US8704008B2 (en) 2010-07-09 2014-04-22 Celanese International Corporation Process for producing ethanol using a stacked bed reactor
US8664454B2 (en) 2010-07-09 2014-03-04 Celanese International Corporation Process for production of ethanol using a mixed feed using copper containing catalyst
US8710280B2 (en) 2010-07-09 2014-04-29 Celanese International Corporation Weak acid recovery system for ethanol separation processes
US9150474B2 (en) 2010-07-09 2015-10-06 Celanese International Corporation Reduction of acid within column through esterification during the production of alcohols
US8901358B2 (en) 2010-07-09 2014-12-02 Celanese International Corporation Esterification of vapor crude product in the production of alcohols
US8884080B2 (en) 2010-07-09 2014-11-11 Celanese International Corporation Reduced energy alcohol separation process
US9024083B2 (en) 2010-07-09 2015-05-05 Celanese International Corporation Process for the production of ethanol from an acetic acid feed and a recycled ethyl acetate feed
US8846986B2 (en) 2011-04-26 2014-09-30 Celanese International Corporation Water separation from crude alcohol product
US8710279B2 (en) 2010-07-09 2014-04-29 Celanese International Corporation Hydrogenolysis of ethyl acetate in alcohol separation processes
US9126125B2 (en) 2010-07-09 2015-09-08 Celanese International Corporation Reduced energy alcohol separation process having water removal
US8536384B2 (en) 2010-07-09 2013-09-17 Celanese International Corporation Recovering ethanol sidedraw by separating crude product from hydrogenation process
US9308469B2 (en) 2010-07-22 2016-04-12 Nippon Steel & Sumikin Engineering Co., Ltd. Device for producing ethanol and method for producing ethanol
US8927784B2 (en) 2011-04-26 2015-01-06 Celanese International Corporation Process to recover alcohol from an ethyl acetate residue stream
US8927788B2 (en) 2011-04-26 2015-01-06 Celanese International Corporation Process to recover alcohol with reduced water from overhead of acid column
US9024084B2 (en) 2011-04-26 2015-05-05 Celanese International Corporation Reduced energy alcohol separation process having controlled pressure
US8927787B2 (en) 2011-04-26 2015-01-06 Celanese International Corporation Process for controlling a reboiler during alcohol recovery and reduced ester formation
US9024082B2 (en) 2011-04-26 2015-05-05 Celanese International Corporation Using a dilute acid stream as an extractive agent
US8461399B2 (en) 2011-04-26 2013-06-11 Celanese International Corporation Separation process having an alcohol sidestream
US9000233B2 (en) 2011-04-26 2015-04-07 Celanese International Corporation Process to recover alcohol with secondary reactors for hydrolysis of acetal
US9024085B2 (en) 2011-04-26 2015-05-05 Celanese International Corporation Process to reduce ethanol recycled to hydrogenation reactor
US8907141B2 (en) 2011-04-26 2014-12-09 Celanese International Corporation Process to recover alcohol with secondary reactors for esterification of acid
US8927783B2 (en) 2011-04-26 2015-01-06 Celanese International Corporation Recovering ethanol with sidestreams to regulate C3+ alcohols concentrations
US9073816B2 (en) 2011-04-26 2015-07-07 Celanese International Corporation Reducing ethyl acetate concentration in recycle streams for ethanol production processes
US8686200B2 (en) 2011-04-26 2014-04-01 Celanese International Corporation Process to recover alcohol from an acidic residue stream
US8884081B2 (en) 2011-04-26 2014-11-11 Celanese International Corporation Integrated process for producing acetic acid and alcohol
US9000232B2 (en) 2011-04-26 2015-04-07 Celanese International Corporation Extractive distillation of crude alcohol product
US8592635B2 (en) 2011-04-26 2013-11-26 Celanese International Corporation Integrated ethanol production by extracting halides from acetic acid
US8927780B2 (en) 2011-04-26 2015-01-06 Celanese International Corporation Process for removing aldehydes from ethanol reaction mixture
US8748675B2 (en) 2011-06-16 2014-06-10 Celanese International Corporation Extractive distillation of crude alcohol product
US8754268B2 (en) 2011-04-26 2014-06-17 Celanese International Corporation Process for removing water from alcohol mixtures
US8933278B2 (en) 2011-04-26 2015-01-13 Celanese International Corporation Process for producing ethanol and reducing acetic acid concentration
US8686199B2 (en) 2011-04-26 2014-04-01 Celanese International Corporation Process for reducing the concentration of acetic acid in a crude alcohol product
US8704012B2 (en) 2011-06-16 2014-04-22 Celanese International Corporation Distillation of crude alcohol product using entrainer
US8877986B2 (en) 2011-08-03 2014-11-04 Celanese International Corporation Process for recovering alcohol
US8884079B2 (en) 2011-08-03 2014-11-11 Celanese International Corporation Reducing impurities in hydrogenation processes with multiple reaction zones
US8440866B2 (en) 2011-08-03 2013-05-14 Celanese International Corporation Process for separating ethanol having low acid
US8877987B2 (en) 2011-08-03 2014-11-04 Celanese International Corportation Process for producing anhydrous ethanol using extractive distillation column
US8927782B2 (en) 2011-08-03 2015-01-06 Celanese International Corporation Vapor separation in alcohol production
US8748676B2 (en) 2011-08-03 2014-06-10 Celanese International Corporation Process for purifying a crude ethanol product
US8575405B2 (en) 2011-08-03 2013-11-05 Celanese International Corporation Reducing acetals during ethanol separation process
US8895786B2 (en) 2011-08-03 2014-11-25 Celanese International Corporation Processes for increasing alcohol production
US8802901B2 (en) 2011-11-18 2014-08-12 Celanese International Corporation Continuous ethyl acetate production and hydrogenolysis thereof
US9024089B2 (en) 2011-11-18 2015-05-05 Celanese International Corporation Esterification process using extractive separation to produce feed for hydrogenolysis
US8748673B2 (en) 2011-11-18 2014-06-10 Celanese International Corporation Process of recovery of ethanol from hydrogenolysis process
US8829251B2 (en) 2011-11-18 2014-09-09 Celanese International Corporation Liquid esterification method to produce ester feed for hydrogenolysis
US8829249B2 (en) 2011-11-18 2014-09-09 Celanese International Corporation Integrated esterification and hydrogenolysis process for producing ethanol
US8853468B2 (en) 2011-11-18 2014-10-07 Celanese International Corporation Vapor esterification method to produce ester feed for hydrogenolysis
EP2782890A1 (fr) 2011-11-22 2014-10-01 Celanese International Corporation Estérification d'un mélange d'éthanol et d'acide acétique pour produire une charge d'ester pour l'hydrogénolyse
US12195781B2 (en) * 2011-12-12 2025-01-14 Jupeng Bio (Hk) Limited Management of ethanol concentration during syngas fermentation
WO2013089990A1 (fr) 2011-12-14 2013-06-20 Celanese International Corporation Produit de réacteur multiphase issu de l'hydrogénation d'acide acétique en matière première d'acétate d'éthyle pour produire de l'éthanol
US8927790B2 (en) 2011-12-15 2015-01-06 Celanese International Corporation Multiple vapor feeds for hydrogenation process to produce alcohol
US8907139B2 (en) 2011-12-28 2014-12-09 Celanese International Corporation Process for acetal removal in the purification of a crude ethanol product
WO2013101305A1 (fr) 2011-12-30 2013-07-04 Celanese International Corporation Distillation commandée par pression pour produire et récupérer de l'éthanol à partir d'un processus d'hydrogénation
BR112014015584A8 (pt) 2012-01-06 2017-07-04 Celanese Int Corp catalisadores de hidrogenação com suportes modificados com cobalto
US9024086B2 (en) 2012-01-06 2015-05-05 Celanese International Corporation Hydrogenation catalysts with acidic sites
EP2617479A1 (fr) * 2012-01-23 2013-07-24 Methanol Casale SA Procédé et appareil pour la distillation de méthanol avec récupération de chaleur
US9353034B2 (en) 2012-02-07 2016-05-31 Celanese International Corporation Hydrogenation process with reduced residence time for vapor phase reactants
US9051235B2 (en) 2012-02-07 2015-06-09 Celanese International Corporation Process for producing ethanol using a molar excess of hydrogen
US9050585B2 (en) 2012-02-10 2015-06-09 Celanese International Corporation Chemisorption of ethyl acetate during hydrogenation of acetic acid to ethanol
US8729311B2 (en) 2012-02-10 2014-05-20 Celanese International Corporaton Catalysts for converting acetic acid to acetone
JP5956772B2 (ja) * 2012-02-20 2016-07-27 東洋エンジニアリング株式会社 熱交換型蒸留装置
JP5923335B2 (ja) * 2012-02-24 2016-05-24 東洋エンジニアリング株式会社 熱交換型蒸留装置
US8802903B2 (en) 2012-03-13 2014-08-12 Celanese International Corporation Stacked bed reactor with diluents for producing ethanol
JP5923367B2 (ja) * 2012-03-30 2016-05-24 東洋エンジニアリング株式会社 熱交換型蒸留装置
US8957262B2 (en) 2012-11-20 2015-02-17 Celanese International Corporation Olefin hydration for hydrogenation processes
US9000237B2 (en) 2012-12-20 2015-04-07 Celanese International Corporation Ethanol refining process using intermediate reboiler
US8926718B2 (en) 2013-03-15 2015-01-06 Celanese International Corporation Thermochemically produced ethanol compositions
US8975451B2 (en) 2013-03-15 2015-03-10 Celanese International Corporation Single phase ester feed for hydrogenolysis
CN103601329B (zh) * 2013-11-20 2015-06-03 上一环保科技（杭州）有限公司 一种费托合成水的醇水分离回收装置
US10486079B1 (en) 2016-01-08 2019-11-26 Whitefox Technologies Limited Process and system for dehydrating a byproduct stream in ethanol production
EP3195915A1 (fr) * 2016-01-20 2017-07-26 Sulzer Chemtech AG Système de purification d'un solvant organique et procédé pour son utilisation
US10729987B1 (en) 2016-12-09 2020-08-04 Whitefox Technologies Limited Process and system for heat integration in ethanol production
JP2020075864A (ja) * 2017-03-14 2020-05-21 三菱ケミカル株式会社 アルコールの製造方法
CN112118897B (zh) 2018-05-07 2022-07-01 怀弗克斯技术有限公司 在具有分子筛和膜的乙醇生产中使产物流脱水的方法和系统
CN110591752B (zh) * 2019-09-24 2021-04-27 青岛华世洁环保科技有限公司 二氯甲烷-白油混合液回收提纯的方法及装置
EP4370225A4 (fr) * 2021-07-12 2025-03-12 Whitefox Technologies Limited Production de solvant organique par distillation et déshydratation
CN116745015B (zh) * 2021-10-08 2025-09-09 株式会社Lg化学 热集成分离系统
US12005381B2 (en) 2021-10-15 2024-06-11 Whitefox Technologies Limited Heat integrated process and system for ethanol production using vapor recompression

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4328074A (en) * 1980-11-12 1982-05-04 Resources Conservation Company Production of concentrated alcohol and distillery slop
DE3303571C2 (de) * 1982-03-11 1984-07-26 Buckau-Walther AG, 4048 Grevenbroich Verfahren und Anlage zur Herstellung von Äthanol
US5124004A (en) * 1983-08-22 1992-06-23 Trustees Of Dartmouth College Distillation process for ethanol
JPH08119239A (ja) * 1994-10-31 1996-05-14 Sony Corp カートン処理システム及びカートン処理方法
JP2000503920A (ja) * 1996-01-26 2000-04-04 テトラ ラバル ホールデイングス エ フイナンス ソシエテ アノニム 包装材料に画像を印刷する方法と装置
US7291250B1 (en) * 1999-10-20 2007-11-06 Bionorica Ag Vacuum distillation system and use thereof for concentrating organic-aqueous solvent mixtures
ES2339223T3 (es) * 2001-10-19 2010-05-18 Mitsubishi Chemical Corporation Aparato de destilacion de material organico soluble en agua.
WO2004088230A2 (fr) * 2003-03-28 2004-10-14 Thermal Kinetics Systems, Llc Distillation d'ethanol au moyen d'un appareil de recuperation de solides solubles d'alambics
CN100536974C (zh) * 2003-04-25 2009-09-09 2S－精密系统有限公司 蒸馏方法

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2007095875A1 *

Also Published As

Publication number Publication date
RU2007142494A (ru) 2009-08-10
BRPI0610023A2 (pt) 2010-05-18
US20080135396A1 (en) 2008-06-12
CA2605570A1 (fr) 2007-08-30
WO2007095875A1 (fr) 2007-08-30
DE112006001685A5 (de) 2008-04-03
JP2008536503A (ja) 2008-09-11
CN101163528A (zh) 2008-04-16

Similar Documents

Publication Publication Date Title
EP1888193A1 (fr) Procédé de séparation
EP1620191B1 (fr) Procede de distillation
DE3303571C2 (de) Verfahren und Anlage zur Herstellung von Äthanol
DE3610011C2 (fr)
DE4223746C2 (de) Verfahren zur Lösungsmittelrückgewinnung aus einer nicht flüchtige Materialien enthaltenden Mutterlauge durch ein Wärmepumpensystem
DE2635935A1 (de) Verfahren zur reinigung von essigsaeure
DE3311316A1 (de) Verfahren zur erzeugung von methanol in chemie-qualitaet
DE2906698B2 (de) Verfahren zur Gewinnung von Ethylenoxid, das von Aldehydverunreinigungen und Wasser praktisch frei ist
EP1115681B1 (fr) Procede de production de monoethylene glycol a haute purete
EP1115682A1 (fr) Procede de production de monoethylene glycol de haute purete
DE69716497T2 (de) Verfahren zur Rückgewinnung von Wertstoffen aus Gärungsschlempe
EP0428022B1 (fr) Procédé pour éliminer de l'eau d'un mélange contenant de l'eau, du bioxyde de carbone et de l'amine
DE3002460A1 (de) Verfahren und vorrichtung zur nachbehandlung, insbesondere fuer harnstoff- und ammonnitratanlagen
DE3112603C2 (de) Verfahren zur Abtrennung polarer organischer Verbindungen, insbesondere niederer aliphatischer Alkohole, aus Fermentationsflüssigkeiten
DE69410993T4 (de) Trennverfahren
EP1339469B1 (fr) Procede et dispositif servant a separer les differentes composantes d'un melange de matieres, par distillation extractive dans une colonne a paroi de separation
DE19833941B4 (de) Verfahren und Destillationsvorrichtung zur Gewinnung von 1-Okten
DE69707597T2 (de) Verfahren zur Extraktion von 2-Phenylethanol
DE102011080611A1 (de) Abtrennung flüchtiger Verbindungen aus Fermentationsbrühen
EP0253091B1 (fr) Procédé de séparation d'alcools à bas poids moléculaires de solution aqueuse
DE967075C (de) Verfahren und Vorrichtung zur kontinuierlichen Trennung entwaesserter Rohphenol-Gemische
DE4222783C1 (de) Verfahren zur Rückgewinnung von hochsiedenden Komponenten aus Abwasser
EP1805151A1 (fr) Procede de traitement d'une eau contenant des triazines dans une usine de melamine
EP1224962A2 (fr) Procédé de séparation des mélanges azéotropiques
DE2452651C2 (de) Verfahren zur destillativen Gewinnung von Butandiol-(1,4)

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20071114

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LT LU LV MC NL PL PT RO SE SI SK TR

AX Request for extension of the european patent

Extension state: AL BA HR MK YU

DAX Request for extension of the european patent (deleted)
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20101103