WO2022152712A1 - Mischkneter zur verabeitung eines transfergemisches zu einer formlösung nach dem direktlöseverfahren - Google Patents
Mischkneter zur verabeitung eines transfergemisches zu einer formlösung nach dem direktlöseverfahren Download PDFInfo
- Publication number
- WO2022152712A1 WO2022152712A1 PCT/EP2022/050476 EP2022050476W WO2022152712A1 WO 2022152712 A1 WO2022152712 A1 WO 2022152712A1 EP 2022050476 W EP2022050476 W EP 2022050476W WO 2022152712 A1 WO2022152712 A1 WO 2022152712A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- kneader
- product
- mixing kneader
- water
- mixture
- Prior art date
Links
- 239000000203 mixture Substances 0.000 title claims abstract description 140
- 238000000034 method Methods 0.000 title claims abstract description 123
- 238000012546 transfer Methods 0.000 title claims abstract description 86
- 238000012545 processing Methods 0.000 title claims abstract description 20
- 238000000465 moulding Methods 0.000 title abstract description 9
- 229910001868 water Inorganic materials 0.000 claims abstract description 91
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 88
- 229920002678 cellulose Polymers 0.000 claims abstract description 46
- 239000001913 cellulose Substances 0.000 claims abstract description 45
- 230000002829 reductive effect Effects 0.000 claims abstract description 12
- 239000002245 particle Substances 0.000 claims abstract description 9
- 238000002156 mixing Methods 0.000 claims description 113
- 238000010438 heat treatment Methods 0.000 claims description 45
- 239000010409 thin film Substances 0.000 claims description 41
- 238000001704 evaporation Methods 0.000 claims description 40
- 239000007788 liquid Substances 0.000 claims description 31
- 239000007858 starting material Substances 0.000 claims description 19
- 239000012530 fluid Substances 0.000 abstract description 9
- 235000010980 cellulose Nutrition 0.000 description 41
- LFTLOKWAGJYHHR-UHFFFAOYSA-N N-methylmorpholine N-oxide Chemical compound CN1(=O)CCOCC1 LFTLOKWAGJYHHR-UHFFFAOYSA-N 0.000 description 32
- 230000008020 evaporation Effects 0.000 description 29
- 238000000354 decomposition reaction Methods 0.000 description 25
- 238000004519 manufacturing process Methods 0.000 description 20
- 238000004898 kneading Methods 0.000 description 14
- 238000013021 overheating Methods 0.000 description 14
- 238000004090 dissolution Methods 0.000 description 11
- 239000000463 material Substances 0.000 description 10
- 238000011282 treatment Methods 0.000 description 8
- WAZPLXZGZWWXDQ-UHFFFAOYSA-N 4-methyl-4-oxidomorpholin-4-ium;hydrate Chemical compound O.C[N+]1([O-])CCOCC1 WAZPLXZGZWWXDQ-UHFFFAOYSA-N 0.000 description 7
- 238000010276 construction Methods 0.000 description 7
- 238000004880 explosion Methods 0.000 description 7
- 239000000725 suspension Substances 0.000 description 7
- 238000001816 cooling Methods 0.000 description 6
- 238000013461 design Methods 0.000 description 6
- 230000000930 thermomechanical effect Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 230000007423 decrease Effects 0.000 description 4
- 239000002608 ionic liquid Substances 0.000 description 4
- 238000004886 process control Methods 0.000 description 4
- 208000012886 Vertigo Diseases 0.000 description 3
- 230000001154 acute effect Effects 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- 238000002203 pretreatment Methods 0.000 description 3
- 238000010008 shearing Methods 0.000 description 3
- 238000009987 spinning Methods 0.000 description 3
- 239000003381 stabilizer Substances 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000001419 dependent effect Effects 0.000 description 2
- 239000002360 explosive Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000017525 heat dissipation Effects 0.000 description 2
- 238000000265 homogenisation Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 210000000056 organ Anatomy 0.000 description 2
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 2
- 238000013341 scale-up Methods 0.000 description 2
- 238000007493 shaping process Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000013480 data collection Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 150000004683 dihydrates Chemical class 0.000 description 1
- 238000011978 dissolution method Methods 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 230000002255 enzymatic effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- -1 iron ions Chemical class 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000013386 optimize process Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003908 quality control method Methods 0.000 description 1
- 238000007348 radical reaction Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 230000008961 swelling Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
- 239000003039 volatile agent Substances 0.000 description 1
Classifications
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
- D21C9/18—De-watering; Elimination of cooking or pulp-treating liquors from the pulp
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
- D21B1/00—Fibrous raw materials or their mechanical treatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0082—Regulation; Control
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/22—Evaporating by bringing a thin layer of the liquid into contact with a heated surface
- B01D1/222—In rotating vessels; vessels with movable parts
- B01D1/223—In rotating vessels; vessels with movable parts containing a rotor
- B01D1/225—In rotating vessels; vessels with movable parts containing a rotor with blades or scrapers
- B01D1/226—In rotating vessels; vessels with movable parts containing a rotor with blades or scrapers in the form of a screw or with helical blade members
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08B—POLYSACCHARIDES; DERIVATIVES THEREOF
- C08B1/00—Preparatory treatment of cellulose for making derivatives thereof, e.g. pre-treatment, pre-soaking, activation
- C08B1/003—Preparation of cellulose solutions, i.e. dopes, with different possible solvents, e.g. ionic liquids
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D1/00—Treatment of filament-forming or like material
- D01D1/02—Preparation of spinning solutions
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F2/00—Monocomponent artificial filaments or the like of cellulose or cellulose derivatives; Manufacture thereof
Definitions
- the invention relates to a kneading mixer for processing a transfer mixture into a form solution using the direct dissolution method according to the preamble of claims 1 , 2 and 11 .
- a cellulose-water-functional fluid mixture (hereinafter also referred to as product and cellulose, functional fluid and water as product components) is described, for example, in WO 1994/ 006530 A1, wherein N-methylmorpholine-N-oxide (hereinafter referred to as NMMO or also amine oxide) is used as the functional liquid and the process when NMMO is used as the functional liquid is also known as the amine oxide process.
- NMMO N-methylmorpholine-N-oxide
- the cellulose-water-functional liquid mixture or product is to be understood as meaning all water contents or substance mixture states, i.e.
- a form solution is described in more detail in DE 10 2012 103 296 A1, for example.
- the pre-treatment of the cellulose includes all process steps before it is fed into the direct dissolving process, which begins with the evaporation of the volatile mixture component (here water). These steps usually serve to adjust the solution properties or to shorten the dissolution time in the subsequent process steps.
- the pretreatment comprises process steps known to those skilled in the art, such as an enzymatic pretreatment, grinding of the cellulose or a swelling process.
- WO 1994/006530 A1 describes the widespread use of thin-film evaporators for evaporating water from a cellulose-NMMO-water mixture for the form-dissolving process according to the direct dissolving process Design are known and common, and which are all characterized by the fact that an evaporator shaft in the housing of the thin-film evaporator distributes the product to the inner housing surfaces serving as a heating surface, so that a thin layer is formed, which can also be turbulent with increasing rotational speed and decreasing viscosity, so that the product heats up quickly and part of the water evaporates.
- a heating surface is to be understood as meaning any heated surface that is intended to thermally exchange energy via a temperature difference between the heating surface and the product.
- thin film evaporators are mostly designed with a vertical orientation of the evaporator shaft, as described for example in WO 1994/006530 A1, they can also be designed with a horizontal orientation of the evaporator shaft, as described for example in WO2020249705A1.
- IL an ionic liquid
- IL or ionic liquids refers to a group of organic compounds which, despite their ionic structure, have a low melting point ( ⁇ 100°C) and are therefore also referred to as molten salts.
- the use of IL as a functional liquid therefore always means an embodiment within the group of ionic liquids that is suitable for the direct dissolution process.
- ILs tend to thermally decompose at elevated temperatures, so processes involving a heated IL Temperature of the IL must be kept below the decomposition temperature.
- the decomposition of the IL [DBNH][OAc] above temperatures of approx. 100 °C can be cited here as an example.
- the person skilled in the art is also aware that when the water content of an NMMO-water mixture is reduced at elevated temperatures, decomposition of the NMMO begins. At temperatures typically above 140°C, there is an increasing risk of explosion as the water content decreases, for example due to explosive autocatalytic decomposition, which results in a further increase in temperature and thus an acute risk of explosion.
- decomposition can already be observed at temperatures above 125°C, since the decomposition temperature can be reduced by the presence of reducing agents (such as cellulose) and heavy metal ions (such as iron ions).
- reducing agents such as cellulose
- heavy metal ions such as iron ions
- each composition of the mixture is assigned an equilibrium temperature under the prevailing process conditions (pressure) at which the mixture begins to boil. If energy is supplied to the system, some of the volatiles evaporate components (here water). At the same time, the composition of the mixture changes, which means that the equilibrium temperature also changes as a result. The mixture heats up when energy is supplied, while its composition changes along its equilibrium curve due to the evaporation of volatile components. As the water content decreases, the viscosity increases due to the increasing cellulose concentration and the increasing dissolving power of the functional liquid or the functional liquid-water mixture.
- the evaporating water in the product is increasingly at risk of transport limitations, so that evaporative cooling can no longer take place to a sufficient extent and the temperature of the water-functional liquid mixture and the product consequently rises to values above the equilibrium temperature.
- the equilibrium temperature of the mixture changes with its composition and with the process pressure.
- the temperature of the mixture increases over the course of the process even without transport-limiting effects, so that decomposition can also occur at the equilibrium temperature if the process parameters are selected appropriately.
- the person skilled in the art therefore selects process parameters at which the equilibrium temperatures that occur are always below the decomposition temperatures. Equilibrium temperatures in the range from 50° C. to 110° C. usually result over the course of the process for NMMO as a functional liquid.
- a process at temperatures below the decomposition temperature can also have a product-damaging or safety-endangering effect due to non-thermally induced decomposition processes (e.g. radical reactions). In practice, however, this is counteracted with standard stabilizers.
- non-thermally induced decomposition processes e.g. radical reactions
- dissolving processes do not take place instantaneously but within a period of time with a dissolving speed and require a minimum dissolving time.
- dissolution rates are influenced by various factors such as temperature, and in the case of the direct dissolution process described that, in addition to the temperature, the concentration of the functional liquid and the mechanical treatment of the mixture also have an influence on the dissolution rate. With the same composition and the same temperature, different states of dissolution can occur as a result of different mechanical treatment of the material for the same treatment time.
- the mold solution that is backing up in front of the pump can quickly overheat due to its high viscosity due to mechanical energy input from the evaporator shaft, which can result in acute product damage and with NMMO in particular poses a risk of explosion. If the rotation of the evaporator shaft is stopped, the product distributed as a thin layer in close contact with the heated inner housing surfaces can quickly overheat, which also poses an acute risk of product damage and especially explosion.
- the heated housing surfaces are referred to as heating surfaces.
- the person skilled in the art also has the disadvantage that, in order to avoid significant overheating of the product or the functional liquid, the temperature of the heating surface (also called the heating temperature or heating surface temperature) is greatly reduced in the discharge-side region of the thin-film evaporator. Due to the higher product viscosities there, compared to the upper area of the thin-film evaporator, there is also a higher energy input through dissipation. In addition, the transport speed of the product is reduced by the accumulation effect before discharge, which increases the time available for product heating, which not only increases the energy input through dissipation but also the thermal energy input.
- the temperature of the heating surface is typically lowered to the point where it roughly corresponds to the temperature of the form solution (also referred to below as the form solution temperature) when it exits the thin-film evaporator, i.e. typically 100 to 105 °C with NMMO as the functional liquid, in order to merely temper the product.
- the zone on the discharge side with a reduced heating temperature typically affects 20% to 50% of the Thin film evaporator heating surface.
- avoiding this reduction in the heating temperature would mean an increase in the areas of the thin-film evaporator used for thermal energy input by 25% to 100%, ie the latter would mean a doubling.
- the purpose of reducing the heating surface temperature is, in particular, to compensate for this mechanical energy input in order to avoid significant overheating of the product or the product components and the associated risks of product damage and decomposition.
- a further disadvantage is rising energy costs due to the above-mentioned throttling of the thermal energy input in favor of the mechanical energy input, since instead of the typically inexpensive thermal energy input via the heating surface, there is typically an expensive electromechanical energy input via energy dissipation of the rotating evaporator shaft of the thin-film evaporator.
- WO 2013/156489 A1 would now like to solve this problem, which discloses two successive devices for evaporating water, the first being a thin-film evaporator and the second a thick-film evaporator, preferably a kneading reactor as described in DE 199 40 521 A1, the Kneading reactor is referred to as a mixing kneader. Thanks to good high-viscosity mixing properties and effective mechanical energy input via its shaft (hereinafter referred to as kneader shaft), the speed of which can be quickly set and also quickly reduced, the mixing kneader can regulate the temperature with great accuracy and safely and, as a rule, cool the product or heat dissipation avoid. Thin-film evaporator and mixing kneader are directly connected to one another by a connection, but WO 2013/156489 A1 is silent about the explicit embodiment of the connection.
- the water content in the NMMO of the concentrated pulp suspension is divided into three sections during the dissolving process. After the first section, the pulp suspension from the thin-film evaporator is fed out and into the mixing kneader.
- the first section shows no increase in viscosity and ends with the beginning of the release window, which corresponds to a 2.5 hydrate, which corresponds to an NMMO-water concentration (NMMO based on NMMO and water by mass) of approx. 72.2 wt% and where - as in WO 06/33302 A - Due to the high water content, a low risk of explosion is to be expected.
- the second section consists of the main dissolving process, so that the viscosity there begins to rise sharply and the associated necessary evaporation of water to about a 1.5 hydrate occurs, which corresponds to an NMMO water concentration of about 81.3 wt%.
- the homogenization takes place and water evaporates until a 0.8 to 1.0 hydrate (monohydrate) is formed, which corresponds to an NMMO water concentration of approx. 89.1 wt% to 86.7 wt%.
- the thin-film evaporator in this process is only responsible for the process task of evaporation, the disadvantage of this process is the still high proportion of water, which is not evaporated by a thin-film evaporator. This corresponds to an unused potential for increasing the process efficiency of the thin-film evaporator.
- a subsequent mixing kneader as described in WO 2013/156489 A1—still has to evaporate a large amount of water in the entry zone. Consequently, the two process tasks of evaporation and dissolving now fall to the mixing kneader.
- each kneader shaft can also have only one rotational speed in the case of the mixing kneader, this can lead to the disadvantages already mentioned, as in the case of the thin-film evaporator.
- a high speed selected as a result of the evaporation task to be performed can lead to product degradation in the dissolving task due to increased shearing or temperature damage.
- the integrated heating system also reduces the mechanical stability of the construction and consequently causes a reduction in the maximum size of the mixing kneader.
- the need for this design is further increased by the low viscosity of the concentrated pulp suspension when entering the mixing kneader with an NMMO-water concentration of approx are not sufficient to ensure sufficient water evaporation through the resulting friction and the resulting heating of the pulp suspension.
- various separate heating zones must also be provided, which can be operated at different temperature levels in order to react to any process changes.
- the flexibility of the system increases with the number of zones and consequently the possibility for process control. However, this is also accompanied by an increase in the design and manufacturing complexity, which ultimately leads to an increase in costs.
- the high proportion of water to be evaporated in the invention disclosed in WO 2013/156489 A1 means that there is such a high requirement for heating surfaces in the mixing kneader that the mixing kneaders are essentially to be designed according to the heating surface requirements (in technical jargon a "surface scale-up").
- the size of the mixing kneader is essentially determined by the fact that it has the required heating surface for water evaporation.
- the high water content at the entrance to the mixing kneader means not only a large amount of water to be evaporated, but also a low viscosity, which means a lot of thermal energy input via heated surfaces means because the viscosity required for mechanical energy input in the highly water-containing mixture is too low.
- the high water content means on the one hand a high evaporation load for the mixing kneader and on the other hand, due to the low viscosity, a low proportion of mechanical energy input with considerable economic disadvantages in industrial implementation.
- kneaders are known to those skilled in the art. They preferably have exactly one or exactly two kneader shafts, which are used to carry out highly viscous and crust-forming processes, which can be operated under vacuum, atmospheric or at overpressure and can be heated or cooled via thermal exchange surfaces.
- the kneader shaft and its shaft structures can very effectively heat the product with the typical product viscosities by rotation and the resulting energy dissipation.
- shaft structures of the kneader shaft mesh preferably during operation with static structures of the housing, for example so-called counter hooks. If there are exactly two kneader shafts, then there is a two-shaft mixing kneader, which is described, for example, in DE 41 18 884 A1.
- the shaft structures of the kneader shafts preferably mesh with one another during operation.
- the at least one kneader shaft comprises shaft structures in the form of discs and bars attached thereto, the shaft structures of the at least one kneader shaft being set up to mesh with the shaft structures of a second kneader shaft or with stationary counter-elements present in the mixing kneader during operation.
- Mixing kneaders with such intermeshing elements are known and are referred to as “self-cleaning” because the combing described detaches any buildup from the intermeshing elements.
- the kneader shafts with discs and bars described above are known from the prior art, for example from DE 41 18 884 A1.
- Ingots and discs also called “supports”
- supports can also be made in one piece, for example, so the term "fixed” should be interpreted broadly.
- DE 41 18 884 A1 shows a twin-shaft mixing kneader
- CH 674 472 A5 shows a single-shaft mixing kneader with hook-like static kneading counter-elements (so-called "kneading counter-hook") on the inner wall of the housing.
- the housing, kneader shaft(s), shaft structures and static counter kneading elements can be designed as described in the aforementioned publications.
- thermal exchange surfaces are typically designed as welded-on half-tubes or preferably as double walls.
- thermal exchange surfaces mean that the kneader shaft is designed as a hollow shaft and preferably has an inflow and a return flow of the heat transfer medium or cooling medium, for example with an inner tube.
- Discs with thermal exchange surfaces have cavities or bores for electrical heating elements or a heat transfer medium or cooling medium, the latter having an inflow that is separated from the inflow in the Kneader shaft is fed, and have an outlet that flows back to the reflux in the kneader shaft.
- the cavities can typically be designed as double walls or bores and require greater wall thicknesses and larger dimensions of the shaft structures and kneader shaft with thicker walls and cause a significantly greater production effort compared to cavity-free (hereinafter also referred to as heating cavity-free) discs, which typically due to the omission of thermal exchange surfaces can be built smaller and easier.
- the object of the present invention is to overcome the disadvantages of the prior art.
- a kneading mixer for processing a transfer mixture is to be described, which primarily makes it possible to reduce the size of the kneading mixer and thereby improve the product quality and process control.
- the subject matter of the present invention is a mixer kneader for processing a transfer mixture as the last process stage of an at least two-stage process according to the direct dissolving process in a mixer kneader, which takes into account all the facts mentioned in the context of the task.
- the last process stage is defined by the fact that a mold solution is produced from the transfer mixture in this last process stage.
- a discharge element and then other interposed pumps and buffer containers or the like, which are still necessary up to the spinning/shaping are to be named below, for example.
- the processing of the transfer mixture into a mold solution consists on the one hand of a dissolving process.
- the processing of the transfer mixture into a form solution also consists of evaporating the water remaining in the transfer mixture to the proportion required for the dissolving process and the form solution.
- this evaporation task is subordinate to the dissolving task of the mixing kneader and does not determine its size.
- the mixing kneader requires not only the mechanical energy input resulting from viscosity in combination with a process volume and with at least one rotating kneader shaft, but also heating surfaces for thermal energy input, which are arranged in the mixing kneader.
- the capacity of the mixing kneader means, on the one hand, an evaporation capacity and, on the other hand, a form solution flow capacity.
- the inventive mixing kneader uses the hitherto unknown knowledge that mixing kneader from a certain water content in the Transfer mixture can no longer be carried out with a smaller process volume, because from this water proportion onwards, the process volume necessary for the dissolving time must be applied - the form solution flow capacity is therefore design-determining. Conversely, this means that with increasing water content in the transfer mixture, the mixing kneader must be built larger than would be required for the form solution flow capacity from a certain water content, because the evaporation capacity requires a larger design in order to arrange corresponding heating surfaces in the mixing kneader.
- the mixing kneader according to the invention therefore consists of a mixing kneader whose size only meets the requirements of a mold solution flow capacity.
- the evaporation capacity of the preceding process element for producing the transfer mixture by evaporating essentially water (hereinafter referred to as main evaporation) is adjusted accordingly and results from the heating surfaces and the viscosity-dependent mechanical energy input capacity of the mixing kneader. It is also provided within the scope of the invention that the transfer mixture is produced from a starting material in a plurality of preceding process elements. These preceding process elements can be connected in series or in parallel.
- the mixing kneader according to the invention for processing the transfer mixture into a form solution according to the direct dissolving process is a mixing kneader with a feed, a housing, at least one kneader shaft rotating in the housing and a discharge, the feed containing a product in the form of the transfer mixture consisting essentially of cellulose, water and a Brings functional liquid into the housing, with the transfer mixture being processed with stirring until part of the water has evaporated, so that the form solution is formed, with the form solution flowing onto the discharge with a feed stream, and then the downstream process organ, such as for example the discharge screw, the transfer pump, the buffer tank, the spinning pump and the spinneret.
- the downstream process organ such as for example the discharge screw, the transfer pump, the buffer tank, the spinning pump and the spinneret.
- the product should be fed into the mixing kneader in the form of a transfer mixture and not a suspension.
- the residence time in the mixing kneader can be reduced to a range between 2 and 15 minutes, with the residence time being largely determined by the dissolving time of the cellulose and the precise Dissolving time depends, for example, on the cellulose concentration, the cellulose type, its pre-treatment, the main evaporation and the type of functional liquid and can also go beyond these ranges.
- the same production capacity can be achieved with a mixer-kneader volume of 2,500 L at the same process pressure, whereby heating of the discs of the kneader shaft and division into several temperature zones can be dispensed with, provided the product is introduced into the mixer-kneader with a concentration corresponding to a 1.3 hydrate becomes. This corresponds to a reduction in process volume of more than 80% and a reduction in residence time to around 12 minutes.
- the transfer mixture is characterized by a water content at which the temperature of the heating surface of the thin-film evaporator - in particular against the discharge - is not significantly lowered compared to the entry, without the product being significantly overheated.
- the transfer mixture differs from the forming solution in that it corresponds to the product in a state before it is converted into a formable or spinnable solution (i.e. a forming solution).
- a solution that can be shaped or spun is present when all the essential cellulosic components of the starting material have dissolved.
- essential means such a low proportion of undissolved components that the so-called filter service life reaches an economically acceptable level.
- Filter life refers to filters that are typically used after the forming solution preparation stage and before the forming/spinning stage.
- the filter service life corresponds to the length of time or the period of use until a filter has to be replaced because the pressure drop across the filter becomes too high, which increases due to the accumulation of components undesirable for further processing. These components can represent, for example, undissolved cellulosic fibers as well as non-cellulosic contaminants.
- the concrete choice of a filter service life is therefore subject to macroeconomic costs and quality-optimizing aspects.
- the transfer mixture also differs from the starting material in that part of the cellulose present in the starting material is already in solution in the transfer mixture as a result of thermo-mechanical treatment in the thin-film evaporator.
- the mixing kneader according to the invention for processing the transfer mixture into a form solution in a mixing kneader is characterized in that the product in the mixing kneader has the smallest possible water content, which corresponds to the water content which still has to be evaporated during the dissolving time, which has the advantage that the mixing kneader can be built as small as possible and ideally not all surfaces need to be heated.
- the inlet concentration of water in the mixing kneader is adjusted with the aid of the upstream evaporator stage, resulting in a minimum volume of the mixing kneader.
- the evaporator performance of the thin-layer is adjusted, e.g. with the help of the heating temperature of the thin-layer, so that the desired composition of the form solution at the outlet of the mixing kneader is obtained with the maximum possible throughput of the mixing kneader and compliance with a minimum necessary dissolving time.
- this also means that the discs can only be designed without heating cavities or as pure supports with a minimized side surface, which relieves the kneader shaft and simplifies its production.
- the heating power of the thin layer is adjusted according to the invention so that just enough mechanical power of the mixing kneader is introduced into the product that contact cooling in the mixing kneader is not necessary for a safe and energy-efficient process.
- the process variant described has the advantage of minimal thermal stress on the mixture in the mixing kneader, which is beneficial to the product quality of the molding solution. In terms of apparatus, this means that the kneader shaft does not have several must have heating/cooling zones. There is preferably no contact cooling in the mixing kneader.
- the shaft structures can preferably be designed without heating cavities and the input of energy introduced by kneading is sufficient to produce a molding solution from the transfer mixture.
- the preceding process element in the form of the thin-film evaporator removes so much water during the production of the transfer mixture according to the invention that the task of the mixing kneader is no longer the previously decisive evaporation of water, but rather the kneading of the transfer mixture to form the mold solution.
- the evaporation capacity of the preceding process element is thus set in such a way that the process energy required for heating and evaporating the mixture in the mixing kneader preferably results only from the mechanical capacity of the mixing kneader.
- Another advantage here is the increased energy efficiency and process reliability in combination with a suitable preceding process element, such as preferably a thin-film evaporator for the entire conversion of a starting material into a mold solution.
- an IL or NMMO is added as the functional liquid for the starting material.
- the functional liquid serves to dissolve the cellulose under the right conditions.
- a preferred embodiment of the mixing kneader is characterized in that it is designed for the processing of a transfer mixture, which is selected so that the viscosity of the transfer mixture is not only low enough that a significant Overheating in the thin-film evaporator is avoided, but also large enough that the mechanical energy input caused by friction in the mixing kneader is so high that the need for thermal energy input in the mixing kneader - supplementing the mechanical energy input - is so low that the structures of the kneader shaft do not meet the must serve thermal heat exchange, but can be designed without heating cavity. This enables a significantly simpler, cheaper and faster construction of the kneader shaft.
- the transfer mixture processed into a form solution in the mixing kneader according to the invention is therefore selected in such a way that it is suitable for specific process conditions, essentially mixing and kneading intensity, degree of filling, gas pressure and heating temperature, as well as for a specific type and proportion of cellulose and its type of pretreatment and a certain type and proportion of a functional liquid has a water concentration such that at least one of the following conditions is met or at least one of the following embodiment variants according to the invention is given:
- the size of the mixing kneader is designed exclusively for the requirements of a form solution flow capacity, and the resulting water evaporation capacity of the mixing kneader corresponds to the water evaporation capacity that is necessary in order to be able to evaporate the water content of the transfer mixture required for the production of a form solution.
- the mixing kneader is designed in such a way that a reduction in the proportion of water in the transfer mixture or an increase in the evaporation capacity of the mixing kneader, for example due to higher heating temperatures, does not result in the mold solution flow capacity being able to be increased.
- the transfer mixture is chosen so that - in addition to (1) and (2) above - it has a water concentration that also applies:
- the mixer kneader is equipped with at least one kneader shaft, the superstructure of which does not have to be heatable, and the transfer mixture has sufficient viscosity to be heated by means of mechanical energy input, in addition to the thermal energy input, via a heatable kneader shaft of the mixer kneader and a heatable housing of the mixer kneader to achieve the evaporation capacity required in the mixing kneader to produce a mold solution.
- the starting material is a mixture of cellulose, water and functional fluid, the composition of which can vary greatly.
- the starting material becomes a transfer mixture.
- This process step can preferably take place in one or more thin-film evaporators.
- the thin-layer evaporator(s) is/are the preceding process element.
- the cellulose is partially dissolved and in the case of NMMO as the functional liquid, the water content in the NMMO can be taken from the mathematical formula.
- the formulas for describing the transfer mixture relate to the production of a transfer mixture under thermo-mechanical conditions that allow low-risk operation of a thin-film evaporator and have proven themselves in practice. Because of the explained Influences on the rate of dissolution of the cellulose, however, it is possible that the formula predicts a spinnable solution, while in practice, despite low water contents, there is still a transfer mixture according to the invention with undissolved cellulose components, since a special thermomechanical treatment was chosen, such as very short times of the product between feed and outlet. Due to the associated lower water content in the transfer mixture, such thermo-mechanical treatments are associated with an increased process risk due to significant overheating and explosive decomposition.
- this can also mean that the starting material, even if the composition is within the concentration range, is fed to the preceding process step, which describes the general transfer mixture.
- a transfer mixture which is characterized by a partial dissolution of the cellulose, is usually only created through the process-specific thermo-mechanical treatment of the starting material (increased temperature and shearing effect).
- the transfer mixture is then further processed in a mixing kneader to form a form solution, which is more suitable for safely converting the transfer mixture into a form solution than the upstream process element such as a thin-film evaporator, since the mixing kneader, as described above, is particularly suitable for good high-viscosity mixing properties and effective mechanical energy input via the kneader shaft, the speed of which can be quickly set and also quickly reduced again, can regulate the temperature with great accuracy and safely and, as a rule, - avoids cooling or heat dissipation.
- the transfer mixture firstly passes through a transfer device or devices downstream of the thin-film evaporator or multiple thin-film evaporators, before it is fed into the mixing kneader.
- the increased energy efficiency and process reliability not only applies to the process step of producing the mold solution from the transfer mixture in the mixing kneader, but also in combination with a suitable upstream processing element for the entire conversion of a starting material into a mold solution.
- the maximum water content x H20 describes the composition that corresponds to the dihydrate when considering water and NMMO.
- NMMO molecules have the ability to form two hydrogen bonds. The hydrogen bonds lead on the one hand to the formation of structures with water molecules bound over them and on the other hand to the detachment of cellulose molecules. From a ratio of less than two water molecules per NMMO molecule, there is theoretically a dissolving capacity of the NMMO for cellulose molecules. This separates the transfer mixture from the pure suspension as the upper water content limit. For example, it is also described in the literature that with appropriate thermomechanical treatment, a part of cellulose is already in solution at NMMO-water concentrations of approx. 75%.
- the formula for describing the maximum water content x H20 of the preferred transfer range is based on results from industrial applications of the direct dissolution process and data collection from the inventors' test series on a pilot plant scale. It marks the upper limit of the transfer range, within which optimal utilization of the specific, process-relevant mixing kneader characteristics is guaranteed.
- the transfer mixture is in a pre-solution state in its general composition and also in its preferred composition (each described by the corresponding formulas above).
- This also means that the mold release process takes place under optimal operating parameters of the thin-film evaporator and the comparatively difficult material conditions of the mold release are avoided if, for example, encrustations occur in the thin-film evaporator or overdrying or decomposition takes place.
- These difficult material states do not lead to problematic process states in the subsequent mixing kneader according to the invention, because this is generally designed, for example, for higher torques and the avoidance of crust formation.
- the maximum proportion of water is in Comparison to the definition of the general transfer mixture, already closer to the full solution.
- the minimal proportion of water is at a greater distance from this complete solution.
- the processing of the transfer mixture into a form solution in the mixing kneader according to the invention can be realized in a short process time, corresponding at most to the duration of the dissolution, and at the same time the risk of overdrying of the material can be reduced.
- the transfer mixture is removed from a moldable or spinnable solution after a processing time of two to several minutes, during which the product is homogenized in the mixing kneader and any residual water is evaporated.
- the product and thus also the starting material essentially contain cellulose, water and a functional liquid.
- the product contains other chemicals such as stabilizers, etc., which need not be listed in detail within the scope of the invention, since they are known to the person skilled in the art and require adaptation for each individual case of use.
- Figure 1 is a graph of the general and preferred material properties of a transfer mix.
- the subject of this example is the production of a molding solution with a cellulose content of 12% by weight using the direct solution process.
- NMMO is used as the functional fluid. All of the following proportions relate to the total mass of the cellulose-NMMO-water mixture.
- a starting material with a cellulose content of approx. 7.2 wt% is produced from cellulose and aqueous NMMO solution, resulting in an NMMO content of approx. 46.1 wt%.
- This starting material is introduced into a thin-film evaporator at a flow rate of approx. 417 kg/h and concentrated there to form a transfer mixture.
- the thin-film evaporator is operated at a process pressure of 70 mbara, so that the equilibrium temperature of the starting material is around 43 °C.
- the heating temperature of the thin-film evaporator is 130° C.
- the mixture is transferred within the preferred transfer range with a cellulose content of approx. 11.5 wt% and an NMMO content of approx. 73.9 wt%. At the present process conditions this corresponds to an equilibrium temperature of the transfer mixture of approx. 100 °C.
- the ratio of water and NMMO at this point is approximately that of a 1.3 hydrate.
- the transfer mixture provided by the thin-film evaporator is then brought into the mixing kneader at a flow rate of approx.
- the form solution leaves the mixing kneader at a flow rate of approx. 217 kg/h with a cellulose content of 12.0 wt%, an NMMO content of approx. 77.0 wt% and a temperature of approx. 107oC.
- the subject of this example is the production of a molding solution with a cellulose content of 12% by weight using the direct solution process.
- an ionic liquid is used as the functional liquid. All of the following proportions relate to the total mass of the mixture.
- a starting mixture with a cellulose content of approx. 8.2 wt% is made from cellulose and aqueous IL solution, resulting in an IL content of approx. 58.6 wt%.
- This starting material is introduced into a thin-film evaporator at a flow rate of approx. 475 kg/h and concentrated there to form a transfer mixture.
- the mixture is transferred with a cellulose content of approx. 11.5 wt% and an IL content of approx.
- the transfer mixture provided by the thin-film evaporator is then fed into the mixing kneader at a flow rate of approx. 347 kg/h. There, the mixture is finally concentrated by evaporation and homogenization, resulting in a complete mold solution.
- the residence time of the mixture in the mixing kneader is 12 minutes.
- the process volume of the kneader is therefore approx. 115 L.
- the form solution leaves the mixing kneader in one stream of approx. 333 kg/h with a cellulose content of 12.0 wt% and an IL content of approx. 83.0 wt%.
- Shown in Figure 1 is a graph showing the general and preferred material composition of the transfer mix.
- the range of the solution L is first reached and with a further decrease in the water content, the crystallization K of the NMMO takes place.
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Mechanical Engineering (AREA)
- Textile Engineering (AREA)
- Health & Medical Sciences (AREA)
- Materials Engineering (AREA)
- Biochemistry (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Wood Science & Technology (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
- Processes Of Treating Macromolecular Substances (AREA)
- Accessories For Mixers (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Mixers Of The Rotary Stirring Type (AREA)
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN202280013605.7A CN116917015A (zh) | 2021-01-13 | 2022-01-12 | 用于按照直接溶解法将转移混合物处理成模制溶液的混合捏合机 |
EP22702871.9A EP4277717A1 (de) | 2021-01-13 | 2022-01-12 | Mischkneter zur verabeitung eines transfergemisches zu einer formlösung nach dem direktlöseverfahren |
JP2023542506A JP2024502636A (ja) | 2021-01-13 | 2022-01-12 | 直接溶解法に従って移送混合物を成形溶液へ処理するための混合混練機 |
CA3204866A CA3204866A1 (en) | 2021-01-13 | 2022-01-12 | Kneader mixer for processing a transfer mixture into a moulding solution according to the direct dissolving method |
KR1020237027433A KR20230132520A (ko) | 2021-01-13 | 2022-01-12 | 직접 용해 방법에 따라 이송 혼합물을 성형 용액으로처리하기 위한 혼합 혼련기 |
US18/272,195 US20240076832A1 (en) | 2021-01-13 | 2022-01-12 | Kneader mixer for processing a transfer mixture into a moulding solution according to the direct dissolving method |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102021100480.2A DE102021100480A1 (de) | 2021-01-13 | 2021-01-13 | Mischkneter zur Verarbeitung eines Transfergemisches zu einer Formlösung nach dem Direktlöseverfahren |
DE102021100480.2 | 2021-01-13 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2022152712A1 true WO2022152712A1 (de) | 2022-07-21 |
Family
ID=80222083
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2022/050476 WO2022152712A1 (de) | 2021-01-13 | 2022-01-12 | Mischkneter zur verabeitung eines transfergemisches zu einer formlösung nach dem direktlöseverfahren |
Country Status (9)
Country | Link |
---|---|
US (1) | US20240076832A1 (de) |
EP (1) | EP4277717A1 (de) |
JP (1) | JP2024502636A (de) |
KR (1) | KR20230132520A (de) |
CN (1) | CN116917015A (de) |
CA (1) | CA3204866A1 (de) |
DE (1) | DE102021100480A1 (de) |
TW (1) | TW202244063A (de) |
WO (1) | WO2022152712A1 (de) |
Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4196282A (en) | 1977-11-25 | 1980-04-01 | Akzona Incorporated | Process for making a shapeable cellulose and shaped cellulose products |
CH674472A5 (de) | 1987-05-06 | 1990-06-15 | List Ag | |
DE4118884A1 (de) | 1991-06-07 | 1992-12-10 | List Ag | Mischkneter |
WO1994006530A1 (en) | 1992-09-17 | 1994-03-31 | Courtaulds Fibres (Holdings) Limited | Forming solutions |
WO1997011973A1 (de) * | 1995-09-27 | 1997-04-03 | Lenzing Aktiengesellschaft | Dünnschichtbehandlungsapparat |
DE19940521A1 (de) | 1999-08-26 | 2001-04-19 | List Ag Arisdorf | Mischkneter |
WO2006033302A1 (ja) | 2004-09-21 | 2006-03-30 | Sony Corporation | 印刷装置及び印刷方法 |
WO2008086550A1 (en) * | 2007-01-17 | 2008-07-24 | Lenzing Aktiengesellschaft | Forming solutions |
DE102012103296A1 (de) | 2012-04-17 | 2013-10-17 | List Holding Ag | Verfahren zur Herstellung von Formkörpern |
WO2020249705A1 (de) | 2019-06-12 | 2020-12-17 | Aurotec Gmbh | Dünnschichtbehandlungsvorrichtung |
-
2021
- 2021-01-13 DE DE102021100480.2A patent/DE102021100480A1/de active Pending
-
2022
- 2022-01-12 CA CA3204866A patent/CA3204866A1/en active Pending
- 2022-01-12 JP JP2023542506A patent/JP2024502636A/ja active Pending
- 2022-01-12 CN CN202280013605.7A patent/CN116917015A/zh active Pending
- 2022-01-12 US US18/272,195 patent/US20240076832A1/en active Pending
- 2022-01-12 WO PCT/EP2022/050476 patent/WO2022152712A1/de active Application Filing
- 2022-01-12 EP EP22702871.9A patent/EP4277717A1/de active Pending
- 2022-01-12 KR KR1020237027433A patent/KR20230132520A/ko unknown
- 2022-01-13 TW TW111101528A patent/TW202244063A/zh unknown
Patent Citations (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4196282A (en) | 1977-11-25 | 1980-04-01 | Akzona Incorporated | Process for making a shapeable cellulose and shaped cellulose products |
CH674472A5 (de) | 1987-05-06 | 1990-06-15 | List Ag | |
DE4118884A1 (de) | 1991-06-07 | 1992-12-10 | List Ag | Mischkneter |
WO1994006530A1 (en) | 1992-09-17 | 1994-03-31 | Courtaulds Fibres (Holdings) Limited | Forming solutions |
WO1997011973A1 (de) * | 1995-09-27 | 1997-04-03 | Lenzing Aktiengesellschaft | Dünnschichtbehandlungsapparat |
DE19940521A1 (de) | 1999-08-26 | 2001-04-19 | List Ag Arisdorf | Mischkneter |
WO2006033302A1 (ja) | 2004-09-21 | 2006-03-30 | Sony Corporation | 印刷装置及び印刷方法 |
WO2008086550A1 (en) * | 2007-01-17 | 2008-07-24 | Lenzing Aktiengesellschaft | Forming solutions |
DE102012103296A1 (de) | 2012-04-17 | 2013-10-17 | List Holding Ag | Verfahren zur Herstellung von Formkörpern |
WO2013156489A1 (de) | 2012-04-17 | 2013-10-24 | List Holding Ag | Verfahren zur herstellung von formkörpern |
WO2020249705A1 (de) | 2019-06-12 | 2020-12-17 | Aurotec Gmbh | Dünnschichtbehandlungsvorrichtung |
Non-Patent Citations (1)
Title |
---|
DIENER A ET AL: "CONTINUOUS DISSOLUTION PROCESS OF CELLULOSE IN NMMO", CHEMICAL FIBERS INTERNATIONAL,, vol. 49, no. 1, 1 March 1999 (1999-03-01), pages 40 - 42, XP000827372, ISSN: 0340-3343 * |
Also Published As
Publication number | Publication date |
---|---|
CN116917015A (zh) | 2023-10-20 |
JP2024502636A (ja) | 2024-01-22 |
CA3204866A1 (en) | 2022-07-21 |
US20240076832A1 (en) | 2024-03-07 |
TW202244063A (zh) | 2022-11-16 |
KR20230132520A (ko) | 2023-09-15 |
EP4277717A1 (de) | 2023-11-22 |
DE102021100480A1 (de) | 2022-07-14 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP0356419B1 (de) | Verfahren zur Herstellung von Lösungen von Cellulose | |
EP1144455B1 (de) | Verfahren zur herstellung einer cellulosesuspension | |
EP0817802B1 (de) | Verfahren zur herstellung von celluloselösungen in wasserhaltigen tertiären amin-n-oxiden | |
EP4079385A1 (de) | Dünnschichtbehandlungsvorrichtung | |
AT402902B (de) | Dünnschichtbehandlungsapparat | |
EP1127609A2 (de) | Verfahren zum Behandeln eines Produktes in zumindest einem Mischkneter | |
AT403531B (de) | Vorrichtung zum regeln des druckes in einer strömenden, viskosen masse | |
EP1745166B1 (de) | Lyocell-verfahren und -vorrichtung mit steuerung des metallionen-gehalts | |
EP0065775A2 (de) | Verfahren und Vorrichtung zur kontinuierlichen Verdampfungskristallisation | |
WO1996005338A9 (de) | Vorrichtung und anlage zur verwendung bei der verarbeitung von celluloselösungen | |
WO2022152712A1 (de) | Mischkneter zur verabeitung eines transfergemisches zu einer formlösung nach dem direktlöseverfahren | |
AT505450B1 (de) | Dünnschichtbehandlungsapparat | |
AT505449B1 (de) | Dünnschichtbehandlungsapparat | |
WO2022152713A1 (de) | Verfahren zur herstellung eines transfergemisches nach dem direktlöseverfahren und einem dünnschichtverdampfer | |
WO2023144422A1 (de) | Anlage und verfahren zur verarbeitung eines ausgangsmaterials zu einer formlösung nach dem trockenlöseverfahren | |
DE10029044A1 (de) | Verfahren und Vorrichtung zur Herstellung von Fäden, Fasern, Folien oder Formkörpern aus Cellulose | |
EP3891161A1 (de) | Kontinuierliches verfahren zur gewinnung eines kristallinen monosaccharides und vorrichtung zur kontinuierlichen kristallisierung | |
EP4219567A1 (de) | Anlage und verfahren zur verarbeitung eines ausgangsmaterials zu einer formlösung nach dem trockenlöseverfahren | |
DE102022102177A1 (de) | Anlage und Verfahren zur Verarbeitung eines Ausgangsmaterials zu einer Formlösung nach dem Trockenlöseverfahren | |
AT505461B1 (de) | Dünnschichtbehandlungsapparat | |
EP0899009A2 (de) | Verfahren zur Herstellung von Feststoffen durch Fällung | |
WO2018107193A1 (de) | Verfahren zur herstellung einer stabilisatorzusammensetzung und damit hergestellte stabilisatorzusammensetzung | |
EP1477223A2 (de) | Grossvolumiger Reaktor mit mehreren Prozessräumen | |
WO2022152711A1 (de) | Dünnschichtverdampfer und verfahren zur herstellung eines transfergemisches | |
EP3659773A1 (de) | Verfahren und vorrichtung zur aufbereitung einer styrol-acrylnitril-schmelze |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 22702871 Country of ref document: EP Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2023542506 Country of ref document: JP |
|
ENP | Entry into the national phase |
Ref document number: 3204866 Country of ref document: CA |
|
WWE | Wipo information: entry into national phase |
Ref document number: 18272195 Country of ref document: US |
|
WWE | Wipo information: entry into national phase |
Ref document number: 202280013605.7 Country of ref document: CN |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2023/0525.1 Country of ref document: KZ |
|
ENP | Entry into the national phase |
Ref document number: 20237027433 Country of ref document: KR Kind code of ref document: A |
|
WWE | Wipo information: entry into national phase |
Ref document number: 1020237027433 Country of ref document: KR |
|
ENP | Entry into the national phase |
Ref document number: 2022702871 Country of ref document: EP Effective date: 20230814 |