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EP2661478A2 - Procédé et appareil pour l'évaporation d'halogénure d'hydrogène et d'eau à partir d'hydrolysats de biomasse d'acide halogénohydrique - Google Patents

Procédé et appareil pour l'évaporation d'halogénure d'hydrogène et d'eau à partir d'hydrolysats de biomasse d'acide halogénohydrique

Info

Publication number
EP2661478A2
EP2661478A2 EP11770676.2A EP11770676A EP2661478A2 EP 2661478 A2 EP2661478 A2 EP 2661478A2 EP 11770676 A EP11770676 A EP 11770676A EP 2661478 A2 EP2661478 A2 EP 2661478A2
Authority
EP
European Patent Office
Prior art keywords
evaporation
heat
transfer medium
hydrolyzate
heat transfer
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Withdrawn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
EP11770676.2A
Other languages
German (de)
English (en)
Inventor
Frank Kose
Matthias Schmidt
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.)
Green Sugar AG
Original Assignee
Green Sugar GmbH Produktinnovationen Aus Biomasse
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 Green Sugar GmbH Produktinnovationen Aus Biomasse filed Critical Green Sugar GmbH Produktinnovationen Aus Biomasse
Publication of EP2661478A2 publication Critical patent/EP2661478A2/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Withdrawn legal-status Critical Current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
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/40—Extractive distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/14—Evaporating with heated gases or vapours or liquids in contact with the liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/16—Evaporating by spraying
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • the usable energy for the evaporation was about 16.4 kJ per liter of heat transfer medium used.
  • the technical solution according to the further development (patent DE 10 2008 022 242 AI, filed on 6 May 2008) but about 50, 7 kJ per liter of the heat carrier used for the evaporation used.
  • the circulating oil quantity can be drastically reduced.
  • the heat carrier flow is conducted as a closed film on surfaces or slats in the room. • Superhydrophilic materials are used on surfaces for better distribution of fluid streams.
  • the heat transfer nozzle is indeed arranged above the phase boundary, a different arrangement in Bl would not be detrimental to the leveling of the phase boundary. It is important that the horizontal section of the riser and overflow pipe (also called “overflow”) is not completely filled in. This constraint can be easily achieved by taking into account the geometrical parameters of Bl ⁇ diameter), riser and overflow pipe (also diam B2 is in the sense of the arrangement shown also only one (under vacuum) collecting container, since the actual process of evaporation in Bl takes place. For this purpose, after leveling the phase boundary, a nozzle is switched on, which is arranged below the phase boundary (ie within the heat carrier) and over which the hydrolyzate is sprayed.
  • the apparatus procedure is much simpler. Spraying in the room requires very large volumes of containers. This corresponds to the mode of action, which is based on the fact that the hydrolyzate and heat transfer particles after the Spread the mixture finely in the room. Due to the unrestrained acceleration of gravity in a vacuum, sprayed particles are also accelerated so fast that a corresponding minimum height must be maintained. If you run the heat transfer medium as a film, smaller containers can be used. However, the required internals to achieve this are much more demanding than simple nozzles. By far the smallest volume between all three alternatives can be achieved with the arrangement according to the invention. This is due to the fact that the energy density based on a volume element of the evaporation space used is highest due to the closed phase of the heat carrier.
  • Hydrolyzate particles in the flowing medium This can be achieved in the following ways.
  • One possibility is to increase the height of Bl and place both nozzles higher. This is easy to do within certain limits, but not unlimited possible because the hydrostatic pressure of the liquid column (the heat carrier) also affects the evaporation.
  • a second possibility is to expand the riser and overflow pipe into a container, thereby increasing the residence time of the particles.
  • the diameter of the broadened riser (and thus the flow velocity) should be chosen so that the particles are carried upwards and thus reach the phase boundary again at the bend. This effect could already be detected in gradient experiments.
  • the volume flow of the hydrolyzate was increased uniformly at a constant volume flow of the heat carrier.
  • the outgoing in the riser vapors are removed via the trigger in B2 from the system. Both approaches are easy to implement in terms of apparatus.
  • the nozzle for the introduction of the hydrolyzate can be directed downwards above the heat transfer nozzle.
  • the evaporation takes place at the meeting of the two spray cones and when hitting the phase boundary.
  • the nozzle for the introduction of the hydrolyzate can be directed upward above the heat transfer nozzle and deposited by a second, downwardly directed heat transfer nozzle.
  • the hydrolyzate is already partly evaporated in the supply pipe to the hydrolyzate nozzle. This occurs with appropriate design and guidance of the supply pipe through the space filled with heat transfer medium ⁇ for example, as in Figure 1).
  • heat transfer medium ⁇ for example, as in Figure 1.
  • a two-substance atomization is performed. This principle of action is known, for example, in the case of deodorant bottles, with butane being evaporated within the feed line to the outlet nozzle and ensuring the finest atomization of the deodorant. In the present invention as well, this results in a finer distribution of the hydrolyzate.
  • An embodiment of the introduction device for the hydrolyzate as a nozzle is not mandatory in the sense of the invention described herein. It can be switched before the introduction device, a mixing apparatus in which the hydrolyzate already mixed with the heat transfer stream and then introduced into the Verdam tion space via a simple tube. In the evaporation room finds now only the heat transfer including evaporation but not the distribution in the heat carrier instead.
  • the evaporation is associated with the presence of a closed heat transfer phase, which completely fills a part of the evaporation tank, and by the evaporation (mainly and finally) is carried out until complete removal of hydrogen halide and water. It is not added to the hydrolyzate according to the invention (RP 362230), but hydrolyzate in this closed phase, ie the heat carrier.
  • the subspace of the evaporation tank, which is completely filled with the heat carrier will be referred to as "evaporation space”.
  • the heat transfer medium is supplied in warm form and discharged in cold form and heated outside the evaporation space (indirect heating),
  • the heat carrier in the evaporation space is heated by external heating (for example jacket heating) (direct heating),
  • the heat transfer medium under direct heating or discharged, there are a variety of ways to do so.
  • the heat transfer medium can be injected above the evaporation space and drawn off at the bottom (corresponds to the design in FIG. 1). This results in a vertically downward flow.
  • the heat transfer medium can also be entered below via a variety of insertion devices and discharged via an overflow at the top.
  • the container Bl and the riser and overflow pipe would be combined in a container. This results in a vertically upward heat carrier flow.
  • the lateral entry via nozzles which are arranged along the side wall, combined with a discharge via a tube projecting into the evaporation space is possible.
  • the apparatus options to dissipate the hydrolyzate after it has been freed of hydrogen halide and water are also as diverse as the problem is universal.
  • the upper area sieves are attached, although the gas pass, but not hydrolyzate particles. If these screens are arranged at an angle or shaped, the particles can be guided. For a tube, the shape of a pointed cone would be advantageous.
  • the flow carries the particles up. At the sieves, the separation of gas and solid phase takes place.
  • the particles are guided to the container axis and fall there into an axially arranged below the sieve collecting device, which is simultaneously connected to a tube for the continuous discharge of the particles.
  • the hydrolyzate particles with the cooled heat carrier from the evaporation space and there separate by settling tank and / or centrifuge and / or hydrocyclone and / or combination of these options from the heat carrier.
  • the apparatus design of the discharge is therefore not core of the invention but a part of the invention, namely expression of Necessity, heat carrier and hydrolyzate together for the purpose of evaporation in an evaporation space and then separated again.
  • An evacuated container is completely filled with a warm heat transfer medium in one part, called the evaporation space, which is chemically inert and does not mix with the hydrolyzate.
  • the inventive method described here for the continuous evaporation of liquids for the purpose of separation of dissolved ingredients whose behavior leads to evaporation problems to apparatus problems is not limited to hydrolysates.
  • the present invention may also be used to separate water from seawater for desalination purposes. Salt often forms strong encrustations in the evaporation tanks.
  • the salt can be removed in the form of salt crystals from the heat carrier without causing such apparatus difficulties. But it can also be separated mixtures. For example, acetone and water, since both evaporate at different temperatures. Instead of the solid particles, two phases would form after the evaporation, those of the heat carrier as well as the non-evaporated liquid.

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)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un procédé et un appareil à l'aide desquels un halogénure d'hydrogène et de l'eau peuvent être séparés d'hydrolysats de biomasse d'acide halogénohydrique. Les avantages sont la compacité de l'appareil, l'efficacité de l'évaporation et la multitude de possibilités de configuration, qui permet une adaptation à chaque objectif. L'invention concerne notamment un contenant évacué qui est alimenté en continu avec un caloporteur et qui est rempli dans une partie en totalité avec le caloporteur (chambre d'évaporation). L'hydrolysat de biomasse est également introduit en continu dans cette chambre d'évaporation. Un transfert de la chaleur depuis le caloporteur vers l'hydrolysat se produit dans le contenant, l'halogénure d'hydrogène et l'eau étant évaporés en continu. Les particules d'hydrolysat restantes sont déchargées en continu avec le caloporteur refroidi et séparées en continu du caloporteur. L'invention peut être mise en oeuvre selon diverses configurations techniques. L'invention ici décrite peut également être utilisée pour le traitement d'autres mélanges ou solutions à des fins d'évaporation. Les caractéristiques essentielles du caloporteur utilisé sont : ° il est chimiquement inerte vis-à-vis des substances introduites. ° il ne se mélange que très mal avec les substances introduites, de sorte que des accumulations ne puissent pas se poursuivre sans encombre (ajustement de l'équilibre) et que sa présence continue ne conduise pas à une modification chimique du caloporteur telle qu'il ne puisse pas être remplacé par échange partiel d'une manière économique.
EP11770676.2A 2010-07-14 2011-07-12 Procédé et appareil pour l'évaporation d'halogénure d'hydrogène et d'eau à partir d'hydrolysats de biomasse d'acide halogénohydrique Withdrawn EP2661478A2 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102010027174 2010-07-14
DE102011104723A DE102011104723A1 (de) 2010-07-14 2011-06-15 Verfahren und Apparatur zur Entfernung von Halogenwasserstoffsäuren und Wasser aus halogensauren Biomassehydrolysaten
PCT/DE2011/001423 WO2012013177A2 (fr) 2010-07-14 2011-07-12 Procédé et appareil pour l'évaporation d'halogénure d'hydrogène et d'eau à partir d'hydrolysats de biomasse d'acide halogénohydrique

Publications (1)

Publication Number Publication Date
EP2661478A2 true EP2661478A2 (fr) 2013-11-13

Family

ID=44992430

Family Applications (1)

Application Number Title Priority Date Filing Date
EP11770676.2A Withdrawn EP2661478A2 (fr) 2010-07-14 2011-07-12 Procédé et appareil pour l'évaporation d'halogénure d'hydrogène et d'eau à partir d'hydrolysats de biomasse d'acide halogénohydrique

Country Status (6)

Country Link
US (1) US9254451B2 (fr)
EP (1) EP2661478A2 (fr)
CN (1) CN103261373A (fr)
DE (1) DE102011104723A1 (fr)
EA (1) EA024291B1 (fr)
WO (1) WO2012013177A2 (fr)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IL206678A0 (en) 2010-06-28 2010-12-30 Hcl Cleantech Ltd A method for the production of fermentable sugars
IL207329A0 (en) 2010-08-01 2010-12-30 Robert Jansen A method for refining a recycle extractant and for processing a lignocellulosic material and for the production of a carbohydrate composition
DE112015005318A5 (de) 2014-11-26 2017-10-12 Green Sugar Gmbh Produktinnovationen Aus Biomasse Verfahren zur Säureführung in Hydrolyseanlagen zur sauren Hydrolyse von pflanzlichen Biomassen mittels konzentrierter Salzsäure
CN107208165A (zh) * 2014-12-18 2017-09-26 阿凡田知识中心有限公司 从水性糖溶液生产固体糖的方法
US20200299791A1 (en) * 2015-11-09 2020-09-24 Avantium Knowledge Centre B.V. Process for the Production of a Saccharide Product from an Aqueous Solution
CN107153113A (zh) * 2016-03-04 2017-09-12 北京慧荣和科技有限公司 对流式voc定量加热挥发管和对流式voc定量加热挥发装置
WO2023021432A1 (fr) 2021-08-17 2023-02-23 Frank Kose Procédé pour hydrolyser des biomasses végétales au moyen d'hydracide halogéné, en particulier de l'acide chlorhydrique spécial

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE362230C (de) * 1918-10-15 1922-10-25 Erik Haegglund Dr Verfahren zum Abscheiden fluechtiger Saeuren aus waessrigen Gemischen, insbesondere von Salzsaeure aus Loesungen der Holzverzuckerung
DE102008022242A1 (de) * 2008-05-06 2009-11-12 Green Sugar Gmbh Apparatur zur Entfernung von Halogenwasserstoffsäuren aus Biomassehydrolysaten

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR916382A (fr) * 1943-04-08 1946-12-04 Economisch Technologish Inst O Procédé pour la récupération d'acide chlorhydrique dans l'hydrolyse de matières végétales avec de l'acide chlorhydrique concentré
DE845779C (de) * 1950-03-14 1955-08-01 Bergin Ag Deutsche Verfahren zur Wiedergewinnung und Nutzbarmachung von Salzsaeure und Chlorwasserstoff aus durch Hydrolyse von cellulosehaltigem Material anfallenden sauren Zuckerloesungen
US4237110A (en) * 1979-04-30 1980-12-02 The Dow Chemical Company Process for separating and recovering concentrated hydrochloric acid from the crude product obtained from the acid hydrolysis of cellulose
FI58346C (fi) 1979-12-18 1981-01-12 Tampella Oy Ab Foerfarande foer kontinuerlig foersockring av cellulosa av vaextmaterial
US6007636A (en) 1999-01-04 1999-12-28 Lightner; Gene E. Method to recycle an aqueous acidic liquor used for depolymerization of cellulose
AU2008224486B2 (en) * 2007-03-15 2011-10-20 Hcl Cleantech Ltd. A process for the recovery of HCl from a dilute solution thereof
DE102008064325A1 (de) * 2008-12-20 2010-07-01 Green Sugar Gmbh Enzymatisches Nachbehandlungsverfahren von Biomassehydrolysaten, welche durch Behandlung mit wässrigen Halogenwasserstoffsäuren gewonnen wurden
EP3401322B1 (fr) * 2011-04-07 2022-06-08 Virdia, LLC Procédés et produits de conversion de lignocellulose

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE362230C (de) * 1918-10-15 1922-10-25 Erik Haegglund Dr Verfahren zum Abscheiden fluechtiger Saeuren aus waessrigen Gemischen, insbesondere von Salzsaeure aus Loesungen der Holzverzuckerung
DE102008022242A1 (de) * 2008-05-06 2009-11-12 Green Sugar Gmbh Apparatur zur Entfernung von Halogenwasserstoffsäuren aus Biomassehydrolysaten

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of WO2012013177A2 *

Also Published As

Publication number Publication date
DE102011104723A1 (de) 2012-03-22
WO2012013177A4 (fr) 2012-07-19
WO2012013177A3 (fr) 2012-03-22
EA201490293A1 (ru) 2014-05-30
CN103261373A (zh) 2013-08-21
US20130168226A1 (en) 2013-07-04
US9254451B2 (en) 2016-02-09
WO2012013177A2 (fr) 2012-02-02
EA024291B1 (ru) 2016-09-30

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