Patent Application
20230054441
The present invention relates to a process for preparing a polyamide, more particular to a continuous solid-state polymerization process for preparing a polyamide derived from diamine and dicarboxylic acid.
The preparation of polyamides from diamines and dicarboxylic acids involves the reaction between the amine groups in the diamines and the carboxylic acid groups in the dicarboxylic acids, resulting in amide groups with the formation of water as side product. This reaction is a condensation reaction, and the process is known as a polymerization process involving polycondensation. Polyamides derived from diamines and dicarboxylic acids are also known as AA-BB polyamides.
There are various ways to produce a polyamide from diamines and dicarboxylic acids. The known processes include melt polymerization, solution polymerization, suspension polymerization, and solid-state polymerization, and combinations thereof. Polyamides prepared from diamine and dicarboxylic acid are often manufactured by condensing appropriate salts of diamine and dicarboxylic acid in a molten state, or in a liquid state where the salt is dissolved in water. Such a procedure wherein the salt is polymerized in the molten state or dissolved in water, however, is less suitable for more heat-sensitive and high melting polyamides, as this generally leads to side reactions resulting in degradation of the polymers or branching and gel formation. Therefore, there is an interest in low temperature processes for their preparation. Well-known and widely applied processes for the preparation of polyamides are multi-step processes comprising solid-state post condensation as a further or final step. Examples thereof include processes wherein in a first step a prepolymer is made in aqueous solution, in suspension in an inert liquid, or in a melt. The prepolymer so formed is isolated from the solution or suspension, and solidified, or directly solidified from the melt, and further polymerized to a higher molecular weight polymer while in solid-state. Such process step comprising further polymerization of a prepolymer in the solid-state is also known as a solid-state post-condensation (or SSPC) process, which is referred to herein as Post-SSP.
For AA-BB polyamides also solid-state polymerization processes are known wherein salts of diamine and dicarboxylic acid are polymerized directly to a polyamide polymer of desired molecular weight, with all steps in the solid state, starting, for example, with a salt in the form of a powder. Such a full solid-state polymerization is also known as direct solid-state polymerization, which is referred to herein as Direct-SSP.
Solid-state polymerization processes for polyamides, both Post-SSP and Direct-SSP are described in the book “Solid-state Polymerization” by. C. D. Papaspyrides and S. N. Vouyiouka, Wiley, 2009.
Although solid-state polymerization processes for polyamides have been known for a long time, and Post-SSP processes are applied globally extensively on industrial scale, Direct-SSP processes have remained primarily subject of technical and scientific studies, and are hardly applied, if at all, on industrial scale. This even though Direct-SSP is energetically very attractive, since only the salt is heated, and only to a temperature below the melting point of the salt and the polyamide. This is in contrast with processes comprising a melt step followed by Post-SSP, wherein the salt is first heated to a temperature above the melting point of the salt and the polyamide prepolymer, after which the prepolymer is cooled and converted into granules, and in contrast with processes involving polymerization in an aqueous solution or in a suspension, followed by Post-SSP, wherein the salt is first dissolved or suspended in water or in an inert liquid, the solution or suspension is heated to a temperature and pressure high enough to prepare polyamide prepolymer, after which the water or the inert liquid has to be removed and the prepolymer is isolated and cooled and converted into granules, and after which the granules are heated again to further polymerize the prepolymer in the Post-SSP step to obtain the polyamide.
A huge problem in upscaling Direct-SSP to industrial scale is the amount of condensation water that is produced during the polymerization. This amount can be well in the range of 10 to 15 wt. %, relative to the weight of the starting materials of diamine and dicarboxylic acid. This condensation water must be removed from the reaction mixture or reaction medium. In processes wherein a prepolymer is made in aqueous solution, in suspension in an inert liquid, or in a melt, followed by a solid-state post-condensation step, the largest part of the condensation water is already produced and removed in the first step, wherein the reaction mixture is still in a mobile liquid state. In a Direct-SSP process, this can be accomplished in a batch process with a stirred bed of granular material or, on very small scale, with a static packed bed of granular material. In both situations, either with a stirred bed, or with a very small scale static bed batch process, the reaction speed must be very slow and carefully controlled to prevent the produced condensation water and the initially formed low molecular weight prepolymer from causing sticking and agglomeration of the granular material. These problems of sticking and agglomeration are described in, for example, “Solid-state Polymerization” by. C. D. Papaspyrides and S. N. Vouyiouka, Wiley, 2009. These aspects make upscaling to industrial scale difficult and make the process economically inefficient, since reaction times are long, reducing reactor capacity and making equipment costly.
Solid state polymerization apparatus and assemblies, as well as suitability and drawbacks thereof, are also described in Solid-state Polymerization” by. C. D. Papaspyrides and S. N. Vouyiouka, Wiley, 2009 (page 26-28). To prevent such problems of sticking or sintering, solid-state polymerization is either carried out under stirring or other forms of mechanical agitation. These processes can be carried out under a stream of nitrogen gas. Suitably, a combination of stirring and a stream of nitrogen gas is applied.
During the whole process the reaction mixture is stirred, in order to keep the particles moving with respect to each other. Such a process can be carried out as a batch process, for example in a stationary apparatus in which reaction proceeds while stirring with a rotary vane mounted on a top side of a vertical reactor, or in a tumbler type apparatus in which starting material is introduced into a reactor, both upper and lower portions of which are conical, and the reactor is sealed, followed by performing reaction while rotating the entire body of the reactor under a vacuum.
Such equipment can be used in a batch process, however, has disadvantages of low output per batch cycle, long cycle time, and huge energy loss due to continuous repetition of heating and cooling processes for reaction, all of which lead to increase in production costs. Scaling up of such equipment for large scale production, using equipment with moving parts, sealing parts and heating elements, is all very costly.
On the other hand, continuous processes are often applied in post-condensation for increasing the molecular weight and intrinsic viscosity of prepolymers. Herein solid polyamide prepolymer is fed through a reactor without stirring, moving downwardly as a packed bed of granulate material, meanwhile applying a countercurrent of heated inert gas for heating the granulate polyamide material and removing the water vapor resulting from the solid-state post-condensation reactions. Maintaining a packed bed with a plug flow character is essential for obtaining a product with a consistent and desired end-viscosity within a reasonable residence time.
In a Direct-SSP process, the amount of water produced is typically much higher than in post-condensation processes, it can be about ten times as high, or even more. When the water vapor resulting from the condensation reactions is not continuously and effectively removed from the reactor, without stirring, the solid granulate material will cake and form big lumps. Preventing this would require such a large gas flow, that it could even result in fluidizing and entrainment of the salt particles from the top of the reactor, and otherwise would require very wide equipment to reduce the gas velocity leading to very long residence times. Furthermore, this would also require extensive investment in equipment and extensive costs for cleaning, drying, reheating and recycling of the stream of inert gas. Altogether this would make such a process very uneconomical.
Apart from the above, there is another problem with Direct-SSP processes, which has to do with the volatility of some of the monomers. It is a known fact, that in Direct-SSP, diamine monomers are often partly lost to the gas phase, in particular with high gas flow rates. A fact of matter is that higher gas flows during reaction tend to strip off larger amounts of volatile components, and therefore are detrimental to the task of producing polyamides via Direct-SSP. In particular stripping of diamines in AA-BB type polyamides increases the acid-base unbalance and thereby significantly limits molecular weight build-up. Various solutions, ranging from polymerization in a closed vessel under autogenous pressure to in-situ replenishing of diamine were proposed.
An example of the first is described U.S. Pat. No. 3,232,909. This patent addresses the issue of loss of diamine but does not provide a solution to overcome the problem of sticking. Herein a polyamide precursor salt of hexamethylene diamine and terephthalic acid is polymerized under autogenous pressure developed by retaining effluent vapors in a closed reaction space during polymerization, while causing movement of the particles of said precursor with respect to each other. By said process, vapors produced during the heating and polymerization and stemming from water of reaction and volatile diamine, are retained in the reactor. It is claimed that a polyamide with good properties is obtained, even when a slight excess of terephthalic acid is used, due to the fact that the stoichiometry of monomer reactants is substantially maintained, and harmful loss of diamine has been overcome. In the process of U.S. Pat. No. 3,232,909, wherein an essentially dry salt, i.e. in absence of a visible liquid phase, is charged to the reactor, the polymerization temperature is kept below that of the polymer produced and the heat expended in said process is said to be insufficient to completely melt the particles of the polymerizing mass. However, at a certain moment during the polymerization, the water of reaction forms a liquid phase in which low polymer, i.e. low molecular weight polymer, is dissolved, through which the mass in the reactor becomes a suspension of solid polymer in water and stirring remains possible.
On the other hand, replenishment of diamine is a known solution for Post-SSP processes. However, diamine added during or at the end of such a process, suffers from inefficiency as a large amount of diamine is not absorbed. If carried out in a batch process, it will immediately evaporate when coming into contact with hot polymer particles and will be difficult and time consuming to be fully taken up and reacted with the polymer. In a continuous process carried out under a flow of inert gas for heating, a large part of the diamine is carried away with the gas flow. Moreover, recovery from the exhaust stream will be complicated as it will be mixed with a large amount of water and volatile by-products of the reactions.
In view of the above there is a need for an economic process, in terms of energy costs and scalability, while limiting the risk of sticking and agglomeration in a Direct-SSP and which allows for an effective manner of maintaining or adjusting the monomer balance.
Therefore, the goal of the present invention is to provide a solid-state polymerization process for preparing a polyamide that is economically attractive and scalable to large industrial scale and in which the risk for sticking and agglomeration is reduced to the minimum, and wherein the monomer balance can be maintained or adjusted in an effective manner.
This goal has been achieved with the process according to the invention, which is a continuous solid-state polymerization process for preparing a polyamide derived from diamine and dicarboxylic acid, which process is carried out in a flow-through reactor comprising a reactor column comprising successive zones with different sections. The process according to the invention comprises steps of:
Optionally the process comprises a step of introducing an inert gas into the residence zone via a second gas-inlet section, while further transporting the polyamide as a moving packed bed through the residence zone. Herein the second gas-inlet section is positioned below the first gas-inlet section in the residence zone, suitably at the end of the residence zone. By positioning the second gas-inlet section below the first gas-inlet section, the second gas-inlet section is positioned downstream relative to the first gas-inlet section, and the moving packed bed will first pass the first gas-inlet section, and thereafter the second gas-inlet section.
In the process according to the current invention, solid material is transported substantially by gravity and is moving as a moving packed bed through the reactor column, passing through the multifunctional zones, and subsequently through the residence zone, positioned below or downstream the multifunctional zones. The solid material is heated by means of static heating elements in the heating sections. By using a reactor column comprising successive multifunctional zones comprising heating sections and gas-outlet sections, the solid material that is used in the process, is transported through a sequence of heating sections alternated with gas-outlet sections. Thus, the water vapor produced in a heating section is primarily removed via a gas-outlet section, or via gas-outlet sections adjacent to or nearby said heating section. With an adjacent or nearby gas-outlet section or a nearby array of gas outlet devices next to a heating section is herein meant a gas-outlet section, respectively an array of gas outlet devices directly upstream or directly downstream of the said heating section, and thus positioned between the said heating section and the first next upstream or downstream heating section.
Effectively, in the process according to the current invention, the water resulting from the condensation reactions between amine and acid groups is removed as superheated steam, without the need of inert gas as a carrier gas, via outlets in upward and downward direction and split in multiple zones, with limited hydrodynamic upward forces in the multifunctional zones, and a zero or almost zero net hydrodynamic force in the packed bed, while having drastically limited the risk of sticking and agglomeration without using stirring, thus promoting a steady downward flow of the moving packed bed, and meanwhile also having an overall very good temperature control throughout the reactor and having drastically limited the risk of or even eliminated fluidization and entrainment of particles from the reactor. Furthermore, in the process according to the invention, the loss of diamine during the polycondensation in the multifunctional zones is limited, while simultaneously by introducing a relatively small amount of diamine in the residence zone positioned downstream of the multifunctional zones, the monomer balance can be effectively steered or adjusted without the risk of a significant loss of diamine or need for extensive recovery or work-up of exhaust streams. The term adjacent is also used herein in respect of multifunctional zones and is meant herein to refer to multifunctional zones positioned in an upstream or downstream order directly next to each other.
With downstream is herein meant downstream relative to the flow direction of the moving packed bed.
With solid state in the expressions “solid-state polymerization”, “solid diammonium dicarboxylate salt” and “keeping the salt, the polymerization mixture and the polyamide in the solid state” is herein meant that the key components, being the starting material, i.e. the salt, and the main reaction products, i.e. oligomers and other constituents in the polymerization mixture, and the polyamide, retain a solid state. This does not exclude that volatile components can be formed and released from or absorbed by the solid material, without changing the solid nature of the key components that make up the majority of the mass. Because of the retention of the solid state, the salt can be fed as a particulate material, for example a powder or a granular material, and the salt, the polymerizing mixture and the polyamide can be transported by gravity, or at least substantially so, downward through the reactor column as a solid particulate material with retention of their particulate form.
The advantages of the process according to the invention are first of all that it is a continuous process, with all operational advantages over batch processes, enabling the integration of all steps of salt handling, (pre-)polymer preparation and post-condensation in one integral sequence, without the need of dissolving and melting steps and intermediate isolation or cooling steps, and further that the process is low in energy costs for heating, does not require extensive expensive stirring equipment, is scalable to large industrial scale and has a low risk of sticking and agglomeration despite the large amount of condensation water produced in the polycondensation steps. More particular, through the segmentation of the heating segments where the condensation reactions predominantly take place, effective removal of the condensation water from the heating segments is achieved with a relatively low amount of inert gas, if at all, while at the same time the risk of wetting by condensation of water on cold material, being either the salt starting material or polyamide product in other segments after cooling, thereby causing sticking and agglomeration, is minimized.
The advantages of the process according to the invention are further that water vapor is removed without the need of large volumes of inert gas for entrainment of the water vapor or expensive reactors or equipment for stirring the salt and polymerizing mixture to transfer the heat from the wall to the reacting mass, and the process is economically friendly in that energy needed for heating the salt and energy loss through streams of inert gas are minimized, and that the process can be scaled to large production size. Furthermore, the process according to the invention allows for efficient heat transfer with small temperature gradients, and low static pressure, thereby minimizing chances of sticking and agglomeration.
By applying multiple multifunctional zones in the reactor column, each comprising a heating section and a gas-outlet section, thereby dividing the reactor column in successive sections comprising heating sections alternated with gas-outlet sections, the amount of water vapor produced per heating section is kept limited and is simply expelled from the heating sections and removed via nearby gas-outlet sections by the overpressure resulting from the production of water vapor by the polycondensation reaction, without the need of a stream of inert gas to entrain and remove water vapor, while simultaneously preventing sticking and agglomeration, thus allowing the use of a large and easily moving packed bed in the Direct-SSP process, wherein the salt, the polymerizing mixture and polyamide are kept in the solid-state.
Additional advantages are that the process according to the invention can be carried out at conditions of atmospheric pressure or close to atmospheric pressure, as the water vapor can escape even when being at essentially atmospheric pressure; without use of a carrier gas, while with the upward and downward in-situ removal of the water vapor, the gas velocities in the present invention are further reduced, thereby allowing for a large range of particle sizes, thus no need not limit the use of the apparatus to particles of large size, which would otherwise severely limit available techniques for making the salt precursor particles. In conventional Post-SSP processes, involving gas-heated columns, with typical cases requiring large residence times (often 24 hours), temperature upsets can last a long time and be the cause of a lot of off-spec material. The process according to the invention, using several contact-heating sections in combination with multiple gas-outlet sections in one flow-through column, allows for a much better steering and control of the (local) temperature inside the reactor column, enabling much less off-spec product being produced during start-up, grade changes and upset situations.
In the process according to the invention, water vapor produced via the condensation reactions in a multifunctional zone is at least partly removed via the gas-outlet section in the multifunctional zone and optionally via a nearby gas-outlet section in an adjacent multifunctional zone. The process can be carried out without any need for inert gas fed into the multifunctional zones, and otherwise, if inert gas is added at all, the amount of inert gas can be kept very low. Suitably, the reactor column does not comprise gas inlets in or between any of the heating sections in the multifunctional zones.
The polycondensation in the process according to the invention is suitably carried out in an inert atmosphere. This may be accomplished by applying a purge of an inert gas into the reactor column at the start-up of the process, and a small flow of inert gas fed into the reactor column at suitable locations, such as near the inlet position of salt and near the discharge position of the polymer.
As inert gas any gas inert for polyamides can be used. Examples of such gases are nitrogen, carbon dioxide and argon. Preferably, nitrogen is used as inert gas. It is noted that the water vapor formed by the condensation reactions also helps in inertizing the reactor content.
The process according to the invention can be carried out while feeding an inert gas into the multifunctional zones or without feeding an inert gas into the multifunctional zones. Suitably, the mass flow rate of inert gas fed into the multifunctional zones, if any, is at most 50%, on a mass basis, relative to the mass flow rate of the solid diammonium dicarboxylate salt fed into the reactor column. With the expression if any is meant that it is possible that the amount can be zero, i.e. that no inert gas is fed into the multifunctional zones. Preferably, the mass flow rate of inert gas fed into the multifunctional zones is at most 40%, more preferably at most 25%, even more preferably at most 10% of the mass flow rate of the solid diammonium dicarboxylate salt fed into the reactor column. The advantage of a low or zero mass flow rate of inert gas is that the cost of nitrogen, cost of construction and loss of volatile monomers are all reduced, hence the processing costs are lower and carriage of water vapor resulting from the condensation reactions to other zones, where it could condense, is reduced. Another advantage is that the even flow (i.e. plug flow) of solids through the reactor is least disturbed by minimizing the flow of gas, hence lowering the mass flow rate of inert gas.
Ultimately, using no inert gas has the advantage that the risk of fluidizing the powder particles in the packed powder bed and entrainment of powder particles into the gas-outlets is further reduced, and that by raising the energy input in said heating section or heating sections, the polycondensation reactions can be enhanced, while water vapor produced by said reaction in a heating section can still escape from the reactor column via the two nearby gas-outlet sections, without enhancing said risk of fluidization.
Furthermore, separating the gas-inlets in the residence zone from the gas outlets in the multifunctional zones has the advantage that the water vapor resulting from the condensation reactions during the polymerization can be removed without need of a carrier gas and be driven by in-situ hydrodynamic pressure at relatively low gas velocity. A concomitant effect is that the loss of diamine during the polycondensation in the multifunctional zones is limited. At the same time, diamine can be introduced into the reactor column and be spread through the packed bed in the residence zone with such a low gas velocity, that it has ample more time to react with the polyamide in the residence zone, while reducing the risk of being carried away or expelled unused from the reactor column. This also reduces the need for excess of diamine to compensate for the amount expelled, and thereby reduces the need to recycle or process exhaust gases comprising the expelled diamines. Thus, the process according the present invention results in lower losses of diamine compared to a conventional Post-SSP continuous operations with a countercurrent gas flow, and in particular when compared with a conventional (atmospheric) batch process.
In the process according to the invention, the solid diammonium dicarboxylate salt is suitably fed into the reactor column via a charging section and the resulting polyamide is discharged from the reactor column via a discharge section, while an inert gas is fed into the charging section or into a section nearby the charging section, or into the discharge section or into a section nearby the discharge section, or into both. This has the advantage that respectively the charging section and the discharging section are purged or blanketed with an inert gas, thus preventing oxygen entering the reactor column and eliminating the need for a purge of inert gas in or through the heating sections, where the polycondensation reactions take place, to prevent oxygen entering the heating sections. For blanketing the charging section with inert gas, it may be sufficient, for example, to apply a purge of inert gas on a supply unit from which the solid diammonium dicarboxylate salt is charged into the charging section of the reactor column.
The amount of inert gas fed into the charging section, the section nearby the charging section, the residence zone, the discharge section and the section nearby the discharge section, where applicable, can be kept low, while still being sufficient to blanket the charging section and the discharge section while preventing oxygen entering the reactor column and preventing volatile components (water, diamines) from leaving the reactor column via the charging and discharging sections.
The process according to the invention can be carried out at a pressure, or pressures, varying over a wide range from well below atmospheric pressure to far above. Suitably the process is carried out at atmospheric pressure (0 BarG, typically about 1 bara) or slightly below or above. The process may be carried out at a pressure below atmospheric pressure, but in that case preferably measures are taken to avoid air entering the reactor column and to make water vapor escape from the reactor column. The process may also be carried out at a pressure well above atmospheric pressure. This has the advantage that the risk for air entering the reactor column is reduced. Of course, designing for overpressure puts higher demands on the construction of the reactor. Preferably, the process is carried out at a gas pressure in the range of 0.9-1.5 bara, more preferably 0.95-1.2 bara, and even more preferably 1.0-1.1 bara. Herein the pressure is expressed in bars in absolute numbers. Alternatively, the process is preferably carried out at a gas pressure in the range of −0.1 to +0.5 BarG, more preferably −0.05 to +0.2 BarG, and even more preferably 0 BarG to 0.1 BarG. Herein the pressure is expressed in bars relative to atmospheric pressure. Herein the pressure is the pressure as measured at the exits of the gas-outlet sections in the multifunctional zones.
The process according to the invention suitably comprises a step, wherein the salt is pre-heated or dried, or a combination thereof, prior to entering a multifunctional zone wherein the salt is further heated and polycondensed. Such a pre-heating and drying step may be desirable when the salt comprises some volatiles, such as free water or crystal water. It is noted that during those phases of the process wherein the condensation reactions take place, a large amount of water results from the condensation reactions. This amount can be as high as 10-15 wt. %, for example 12 wt. % or 13 wt. %, relative to the weight of the salt, and even be lower or higher, depending on the molecular weight of the monomers. Next to that, the starting material comprising the salt may contain some water, being crystallized with, or absorbed by or adhered to the salt, without affecting the salt retaining its solid granular shape. Such crystallized, absorbed or adhered water can be, for example, 1.0 or 1.5 wt. % and may well amount to about 0-2.5 wt. % relative to the weight of the salt, and even higher. Such water is suitably removed, for example, by heating the salt to a temperature above 100° C., or by applying vacuum, or a combination thereof. Drying may be done inside the reactor column or outside the reactor column by heating the salt, or outside the reactor column by other means.
Suitably, the process comprises a combined pre-heating-and-drying step prior to the salt being fed into and entering the reactor column. Preferably, the pre-heating-and-drying is done inside the reactor column. This has the advantage that the heating and drying step can be integrated with the further heating steps in the reactor column, thereby simplifying the process design, which becomes less complicated, thus decomplexing the required installations so that less auxiliary equipment is needed, and investment costs are reduced. Herein, the process may comprise a separate salt pre-heating-and-drying step, or a step wherein the pre-heating and drying are combined with the first part of the polycondensation of the salt.
In a particular embodiment, the process comprises a pre-heating-and-drying step, comprising
The heat exchanger in the first multifunctional zone is heated to a temperature referred to as T1.
In this pre-heating and drying step, the heat exchanger in the first multifunctional zone is suitably heated to a temperature T1 in the range of 100-220° C., preferably 110-210° C., more preferably 120-200° C. Also suitably, T1 is kept below Tonset, preferably below {Tonset−5° C.}, more particular more than 10° C. below Tonset. The advantage of a lower heating temperature T1 is that during the heating step the salt can be heated faster and dried while water vapor produced from initial condensation reactions, if any, is limited.
With the term onset temperature Tonset is herein understood the temperature, measured by TGA under nitrogen with the method according to ISO-11358 with a first heating rate of 15° C./minute during a first heating step from 30° C. to 150° C., retention at 150° C. for 15 minutes, followed by a second heating rate of 10° C./minute during a second heating step from 150° C. to 250° C., and retention at 250° C. for 360 minutes, wherein T-onset is determined by the intersection of the starting-mass line and the tangent to the TG curve at the point of maximum gradient.
In another embodiment of the process according to the invention, pre-heating-and-drying may also be combined with a first part of condensation of the salt. Suitably, the process comprises herein a first heating step, wherein pre-heating-and-drying is combined with a first part of condensation of the salt, comprising
In this combined pre-heating, drying and condensation step, the heat exchanger is suitably heated to a temperature T1 above 210° C., preferably in the range of 220-260° C., more preferably 220-240° C. Herein T1 is also suitably at least equal to Tonset, preferably at least equal to {Tonset+5° C.}, more particular T1 is more than 10° C. above Tonset. The advantage of a higher heating temperature T1 is that during the heating step the salt can be dried while simultaneously initial condensation reactions may take place.
This embodiment is suitably combined with an inert gas being fed into the charging section or into a section nearby the charging section. The advantage thereof is that the inert gas, or at least a part thereof, may flow through the heating section of the first multifunctional zone, entrain evaporated water and be released via the gas-outlet section, thereby reducing the risk of condensation of water vapor on cold solid material and excessive wetting of said cold solid material.
To keep the solid material in the column in the solid state, the salt, the polymerizing mixture and the polymer are suitably not heated to a temperature equal to or above the melting point of respectively the salt, the polymerizing mixture and the polymer. To keep the temperature of the salt, respectively of the polymerizing mixture and of the polymer, below its melting point, the static heat exchangers in the multifunctional zones are suitably heated to a temperature (referred to as Temperature Heat Exchangers, or ‘THE’) sufficiently high such that reaction can take place, but still below the melting temperature of the salt (Tm-salt), respectively the meting temperature of the polymerizing mixture (Tm-mixture), and the melting temperature of the polyamide (Tm-polyamide). Preferably, THE of the static heat exchanger in a first multifunctional zone and optionally in one immediately following or more immediately following successive multifunctional zones is kept at least 15° C., more preferably at least 25° C. below the melting temperature of the salt (Tm-salt). Also, THE of the static heat exchanger in a last multifunctional zone and optionally in one or more immediately preceding multifunctional zones is preferably kept at least 15° C., more preferably at least 25° C. below the melting temperature of the polyamide (Tm-polyamide). More preferably, THE of the of the static heat exchangers in all multifunctional zones is kept at least 15° C., even more preferably at least 20° C., and most preferably at least 25° C. below the lowest of the melting temperature of the salt (Tm-salt), the meting temperature of the polymerizing mixture (Tm-mixture), and the melting temperature of the polyamide (Tm-polyamide). Herein the melting temperature (Tm) is the peak temperature measured by the DSC method according to ISO-11357-3.2, 2009, in a nitrogen atmosphere with heating rate of 20° C./min, in the first heating cycle.
The space in the reactor column in which the process is carried out is confined by the wall of the reactor column. In the process solid material is transported through the column, passing through multiple successive heating sections and gas-outlet sections. Herein, each of the sections is confined by a section of the wall of the reactor column. Suitably, the wall sections confining the multiple successive heating sections and gas-outlet sections are heated. The temperature of a wall section is herein also referred to as TWS. In a particular embodiment of the process according to the invention, wherein the sections in the column are confined by wall sections of the column, the wall sections of the heating sections are heated to a temperature TWS in the range from {THE−10° C.} to and including {THE+10° C.}. Preferably, TWS is in the range from {THE−5° C.} to and including {THE+5° C.}.
The process according to the invention is carried out in a reactor column comprising multifunctional zones comprising heating sections and gas-outlet sections. Herein the number of such multifunctional zones may vary largely and may be for example as low as three (3), and as high as ten (10), and even higher. Suitably, the reactor column comprises at least 3 successive multifunctional zones comprising heating sections and gas-outlet sections. This can be sufficient in case when pre-heating-and-drying and a first part of the condensation are done in a first step in the first multifunctional zone, and the further polycondensation is done in the two successive multifunctional zones. The necessary heat input capacity in each of the heating sections can herein be attained by using sufficient contact surface, and where necessary by increasing the contact surface, particularly by increasing the length of the static heat exchangers, or by reducing the distance between the plate heat exchangers or the diameter of the tubes in the case of shell-and-tube heat exchangers.
Preferably, the reactor column comprises at least 4 successive multifunctional zones. This can be sufficient in case when pre-heating-and-drying is done in a first step in the first multifunctional zone, and the polycondensation is done in the three successive multifunctional zones. The advantage hereof is that the capacity for water vapor removal is increased thereby increasing the through-put capacity of the reactor column
More preferably, the reactor column comprises at least 5 successive multifunctional zones, still more preferably at least 6, and even better at least 7 successive multifunctional zones. The advantage thereof is that the polycondensation can be done in and split over more successive multifunctional zones, thereby allowing a higher through-put through the column without increasing the risk of sticking and agglomeration of the solid material in the moving packed bed and distributing the water vapor formed over more gas removal sections, thus reducing the risk of entraining solid material into the gas removal sections.
After the multifunctional zones, the polyamide is further transported as a moving packed bed of solid particles through the residence zone, while introducing a gaseous diamine into the residence zone via a first gas-inlet section inside the residence zone.
Herein the gaseous diamine suitably comprises a mixture of diamines. The gaseous diamine may also be part of a gaseous mixture; the gaseous mixture may comprise, for example, a mixture of a diamine and water vapor. Suitably, the gaseous diamine is prepared by heating and evaporating a feedstock of diamine comprising water. Suitably, the mount of other volatile components different from diamine in the gaseous mixture, is limited. Preferably, the amount is at most 50 wt. %, more preferably at most 20 wt. %, and even more preferably in the range of 0-10 wt. %, relative to the total mass of diamine and other volatile components.
After being introduced into the residence zone, the diamine can react with the polyamide. By extending the length of the residence zone above and below the first gas-inlet section, the diamine has more time to react and there is less risk for unreacted diamine being carried away or expelled unused from the reactor.
Preferably, inert gas introduced into the reactor via the second gas-inlet section at the end of the residence zone has a pressure at least equal to the pressure of the gas in the first gas-inlet section wherein the diamine is introduced.
In a preferred embodiment, the pressure of the inert gas is equal to pressure of the gas in the first gas-inlet section. This limits the gas velocities inside the residence zone, while effectively retaining the diamine in the reactor.
In another preferred embodiment, the inert gas is introduced at a slight overpressure relative to the pressure of the gas in the diamine inlet section. Suitably the overpressure is at most 50 mbar, preferably at most 20 mbar, and more preferably at most 10 mbar. This is beneficial for maintaining a counter-current contacting pattern between diamine gases and polymer particles, and for an effective mass transfer of diamine from the gas phase to the polymer.
The first gas-inlet section and, where applicable, the second gas-inlet section, suitably both comprise an array of multiple gas-inlet devices to spread the gas or gases introduced evenly over the cross section of the residence zone. The gas-inlet devices in such array are preferably regularly spaced from one another and distributed uniformly over a cross-section of the gas-inlet section. Preferably in a manner that promotes the even distribution of both the gases, and the solids.
The residence zone may optionally comprise a heating or cooling section comprising contact heat exchangers for controlling the temperature of the polyamide particles in the residence zone.
The amount of diamine introduced in the residence zone is suitably balanced with the mass flow of salt fed to the reactor. Suitably, the mass flow of diamine is in the range between 0 and 5 wt. %, more particular in the range of 0.1-3 wt. %, and preferably 0.5-2.5 wt. %, relative to the mass flow of salt fed to the reactor. In particular cases, the mass flow of diamine introduced in the residence zone may be in the range 1.0-2.0 wt. %, relative to the mass flow of salt fed to the reactor.
Once the polyamide is produced, the polyamide is suitably cooled prior before being collected or packed or further processed. This cooling may be done outside the reactor column after discharging the polyamide from the reactor column, or alternatively inside the reactor column before discharging the polyamide from the reactor column. In a preferred embodiment, the polyamide is cooled inside the reactor column. For that purpose, the reactor column suitably comprises a cooling zone comprising at least one cooling section comprising static heat exchangers and the process comprises a cooling step, prior to the discharging step, comprising transporting the polyamide to and through the cooling section, while cooling the polyamide in the cooling section, and transporting the cooled polyamide to a discharge section. The advantage of this embodiment is that the process allows multiple process steps to be combined in one, transporting the solid material through the reactor column, without need for additional expensive or complex, air-tight equipment.
The cooling step may optionally be combined with a drying step. Suitably, herein a drying gas is fed into the cooling zone in one or more gas-inlet sections and the drying gas is removed via one or more gas-outlet sections. Since the process is highly efficient in letting off water vapor, the amount of drying gas needed in the cooling step can be kept rather limited, thereby saving costs. Suitably, the mass flow of drying gas fed into the cooling zone is equal or less than, more particular less than half of the mass flow of diammonium dicarboxylate salt fed into the reactor column.
For that purpose, the reactor column suitably comprises a cooling zone comprising a first cooling section comprising static heat exchangers, a gas-inlet section, and a second cooling section comprising heat exchangers, and the process comprises a cooling step, prior to the discharging step, comprising, in this order,
The solid diammonium dicarboxylate salt used in the process according to the invention and fed into the reactor column can be a particulate material having particle sizes and particle size distributions varying over a wide range. The salt can be for example, a powder, more particular a powder with a small particle size, or a granular material, more particular a granular material with medium or larger size of granules. Suitably, the solid diammonium dicarboxylate salt has a particle size distribution with a median particle size (d50), measured with laser granulometry by the method according to ISO 13320-1 at 20° C., in the range of 0.05-10 mm, preferably 0.1-5 mm, more preferably 0.2-3 mm. The advantages of a median particle size of at least 0.2 mm or higher are that the flow properties are better, bulk density of the powder is higher and that the powder has limited tendency to get entrained into the gas outlets. The advantage of a median particle size of at most 3 mm is in addition to the above, that the particles are still small enough to pass through relatively narrow heat exchanger passages inside the column in an even and undisturbed manner, and that they can easily be processed on an extruder afterwards.
For a granular material with a median particle size (d50), below 1 mm, the particle size distribution and median particle size are suitably measured with laser granulometry by the method according to ISO 13320-1 at 20° C. For a granular material with a median particle size (d50) of 1 mm or above, the particle size distribution and median particle size are suitably measured with the sieve method according to DIN 66165 (2016) Part 1&2.
The solid diammonium dicarboxylate salt used in the process according to the invention can in principle be any diammonium dicarboxylate salt that can be polymerized by direct solid-state polymerization. The process according to the invention can be applied for a wide range of polyamides, including aliphatic polyamides, semi-aromatic polyamides and fully aromatic polyamides. Herein, semi-aromatic polyamides and fully aromatic polyamides, more particularly the semi-aromatic polyamides are preferred. For aliphatic polyamides, the salt can be based on fully aliphatic components, i.e. aliphatic diamines and aliphatic dicarboxylic acids. Salts based on fully aromatic components, i.e. aromatic diamines and aromatic dicarboxylic acids, result in fully aromatic polyamides. Most preferably, the salt, as well as semi-aromatic polyamides derived thereof, are based on diamines and dicarboxylic acids comprising both aliphatic and aromatic monomers. For such semi-aromatic polyamides, the combination of aromatic components and aliphatic components may comprise, for example, aliphatic diamine and aromatic dicarboxylic acid, or aromatic diamine and aliphatic dicarboxylic acid, or any combination thereof. The polyamide prepared by the process suitably is a semi-crystalline polyamide. Such a polyamide comprises an amorphous phase and a crystalline phase next to each other.
In a particular embodiment of the process according to the invention, the polyamide produced in the process is a semi-aromatic polyamide, and the diammonium dicarboxylate salt used in the process is a salt of a diamine comprising an aliphatic diamine and a dicarboxylic acid comprising an aromatic dicarboxylic acid. In a preferred embodiment thereof, the solid diammonium dicarboxylate salt comprises an aliphatic diamine and an aromatic dicarboxylic acid, and the polyamide herein prepared is a semi-crystalline semi-aromatic polyamide having a melting temperature of at least 280° C., preferably at least 290° C. Herein, the melting temperature is measured by the DSC method according to ISO-11357-3.2, 2009, in a nitrogen atmosphere with heating rate of 20° C./min, in the first heating cycle.
Suitably, the diammonium dicarboxylate salt used in the process to prepare such semi-crystalline semi-aromatic polyamide is a salt of a diamine comprising at least 70 mole % of a linear aliphatic diamine with 4-12 carbon atoms, and a dicarboxylic acid comprising at least 70 mole % of an aromatic dicarboxylic acid selected from terephthalic acid, naphthalene dicarboxylic acid and 4,4′-biphenyl dicarboxylic acid. The process is in particular advantageous for these polyamides as these are more difficult to produce in a melt process.
In the embodiment wherein the polyamide prepared by the process according to the invention is a semi-crystalline semi-aromatic polyamide having a melting temperature of at least 290° C., the salt is suitably heated to a temperature of at most 230° C., preferably at most 220 in a first multifunctional zone, and to a temperature in the range of Tonset−265° C. in further multifunctional zones.
The polyamide produced in the process according to the invention may have a degree of polymerization varying over a wide range, as well as in connection with the degree of polymerization, have a viscosity varying over a wide range. Suitably, the polyamide discharged from the reactor column has a viscosity number of at least 20 ml/g, preferably at least 50 ml/g, measured in 96% sulphuric acid (0.005 g/ml) at 25° C. by the method according to ISO 307, fourth edition. Also suitably the polyamide has a conversion of carboxylic acid groups into amide groups of at least 90%, preferably at least 95%, more preferably at least 98%, relative to the carboxylic acid groups in the solid diammonium dicarboxylate salt. Herein the concentration of acid groups in the polyamide is determined by titration and expressed in mmol/kg polyamide, and the concentration of acid groups in the salt is calculated from the molecular weights of the diamine and the carboxylic acid in the salt and expressed in mmol/kg salt.
The current invention also relates to a reactor column, more particular to a reactor column for a continuous solid-state polycondensation process as described herein above. The process according to the invention is also suitably carried out in a reactor column as described herein below.
The reactor column according to the invention comprises at least three successive multifunctional zones each comprising a heating section comprising static heat exchangers and a gas-outlet section, and a downstream residence zone comprising at least one gas-inlet section.
The reactor column is suitable for use in a continuous solid-state polycondensation process, such as for preparing a polyamide from a diammonium dicarboxylate salt. Herein the multifunctional zones can be used for the polycondensation of the salt to prepare a polyamide and a first gas-inlet section inside the residence zone can be used for introducing a gaseous diamine into the residence zone, thereby allowing the diamine to react with the polyamide. By dividing the reactor column in multifunctional zones, each comprising a heating section and a gas-outlet section, thus alternating heating sections with gas-outlet sections, the amount of water vapor produced in a continuous solid-state polycondensation process in each heating section can be kept limited and the water vapor can simply be expelled from the heating sections and removed via nearby gas-outlet sections by overpressure resulting from the water vapor formed by the condensation reactions, without the need for a stream of inert gas to entrain and remove water vapor, while local exact temperature control and moderate pressures effectively prevent sticking and agglomeration. This enables employing a moving packed bed of solid state material moving through the column while the salt gets converted into polymer. Furthermore, by carrying out said process in the reactor column according to the invention, the loss of diamine during the polycondensation in the multifunctional zones is limited, while simultaneously introducing a relatively small amount of diamine in the residence zone positioned downstream the multifunctional zones, the monomer balance can be effectively maintained or adjusted without the risk of a significant loss of diamine or need for extensive recovery or work-up of exhaust streams.
Suitably, the at least three successive multifunctional zones in the reactor column do not comprise a gas inlet, i.e. neither in a heating section nor in a gas-outlet section, nor between any of the heating sections, nor between a heating section and a gas-outlet section in the multifunctional zones.
On the other hand, the residence zone in the reactor column according to the invention suitably comprises at least two gas-inlet sections. Herein, a first gas-inlet section inside the residence zone can be used for introducing a gaseous diamine into the residence zone, and a second gas-inlet section positioned downstream to the first gas-inlet section in the residence zone, optionally suitably positioned at the end of the residence zone, is used for introducing an inert gas into the residence zone while further transporting the polyamide as a moving packed bed through the residence zone.
The first gas-inlet section, and where applicable the second gas-inlet section, suitably comprise each an array of multiple gas-inlet devices to spread the gas or gases introduced evenly over the cross section of the residence zone. The gas-inlet devices in such array are preferably regularly spaced from one another and distributed uniformly over a cross-section of the gas-inlet section. Preferably, in a manner that promotes the even distribution of both the gases, and the solids.
As mentioned above, at least 3 successive multifunctional zones can be sufficient in case when pre-heating-and-drying are combined with some first condensation in the first multifunctional zone, and the further polycondensation is accomplished in the two successive multifunctional zones.
In a preferred embodiment, the reactor column comprises at least 4 successive multifunctional zones comprising heating sections and gas-outlet sections, more preferably at least 5, still more preferably at least 6 and even more preferably at least 7 of the multifunctional zones.
As mentioned herein above, the advantage of more successive multifunctional zones is that the polycondensation of a solid starting material for preparing a polymer, for example for preparing a polyamide from a diammonium dicarboxylate salt, can be done in the reactor column in and split over more successive multifunctional zones, thereby allowing a higher through-put through the column without increasing the risk of sticking and agglomeration of solid material or increasing the risk of entrainment of solid material comprising the starting material or the polymer, such as the salt and the polyamide, in a moving packed bed in the reactor column.
In a preferred embodiment of the reactor column according to the invention, the static heat exchangers are selected from vertically or essentially vertically oriented tubular heat exchangers and vertically or essentially vertically oriented plate heat exchangers. The reactor column with such static heat exchangers is advantageously used in the process according to the invention, as it allows for highly efficient heat transfer and in addition allows a moving packed bed of solid material to be transported through the reactor column by gravitational forces while minimizing hindrance for such transport. A further advantage is that such tubular heat exchangers and plate heat exchangers can be regularly spaced from one another and distributed uniformly over a cross section of the heating sections and, where applicable, one or more cooling sections.
In a particular embodiment thereof, the tubular heat exchangers have an inner diameter in the range of 0.5-5 cm and a core-to-core distance in the range of 1-8 cm. Herein the solid material is flowing through the tubes, while the solid material can be heated via the tubes by hot oil flowing in an interstitial space surrounding the tubes.
In another particular embodiment, the plate heat exchangers have
Plate heat exchangers with a smaller thickness have the advantage that there is more space in the reactor column for the moving packed bed flowing downwardly, while a smaller plate-to-plate distance between the plates allows for a better heat transfer between the plate heat exchangers and the moving packed bed flowing downward in the heating sections. A close proximity of heating plates (small passages) has the advantage that the risk of particles sticking together is further reduced. A further advantage of using thin plates with a small distance results in larger heat transfer surface, thereby further enhancing heat transfer and productivity per unit of reactor volume, while still preventing the particles from overheating and sticking. Meanwhile, the temperature of the wall can remain relatively low and quite close to that of the reacting mass, thereby prevent overheating and sticking to the wall.
Preferably, at least one of the heating sections, and preferably each of the heating sections, comprises one or more arrays of plate heat exchange elements regularly spaced from one another and distributed uniformly over a cross-section of the heating section. The advantages thereof are more uniform heating of the solid material and a more uniform flow of the moving packed bed over the cross-section of the heating section with a reduced variation in residence time in the column.
With one or more arrays is meant here that the heating section can comprise one array, or two arrays, or three arrays, or more, for which each array comprises planar heat exchange elements, regularly spaced from one another and distributed uniformly over a cross-section of the heating section. These planar heat exchange elements can be parallel and vertically positioned, or essentially so. This implies that such arrays are positioned in sequential order in the column and a moving packed bed of solid material being transported through the reactor column is transported through one such array after another. It further implies that the arrays belonging to the same heating section are not separated from each other by a gas-outlet section or an array of gas-outlet devices positioned in-between two of these heat exchanger arrays.
The gas-outlet sections in the reactor column according to invention suitably comprise one or more arrays of gas-outlet devices, more particular wherein the devices in each array are substantially evenly spread over a cross-section of the column at the gas-outlet section. Each gas-outlet section may comprise, independently from one another, one or two, or even more of such arrays.
With one or more arrays is meant here that the gas-outlet section can comprise one array, or two arrays, or eventually more than two, for which each array comprises gas-outlet devices regularly spaced from one another and distributed uniformly over a cross-section of the gas-outlet section. This implies that such arrays are positioned in sequential order in the column and a moving packed bed of solid material being transported through the reactor column will be transported passing one such an array after another. It further implies that the arrays belonging to the same gas-outlet section are not separated from each other by a heating section or an array of heat-exchangers positioned in-between two of these arrays of gas-outlet devices.
Preferably, the gas-outlet section positioned between a heating section in the corresponding multifunctional zone and a nearby heating section in the successive multifunctional zone comprises two of said arrays. The advantage of having two of such arrays, instead of one, is that capacity of the reactor column in a continuous solid-state polymerization process is increased by a large amount, or even essentially doubled, without the need of increasing the size of the reactor column, and still avoiding solid material being entrained with the water vapor being removed from the reactor column via the gas-outlet sections, or alternatively significantly reducing the risk of solid material from being entrained with the flow of gas or vapor and being removed from the reactor column via the gas-outlet sections. Furthermore, the risk of water vapor produced in one section being carried over to other sections is further reduced, thereby reducing the risk of water being carried over to upstream sections wherein the salt is still relatively cold, where it could jeopardize the granular material from being retained in the solid state, is thus further reduced.
The gas-outlet section may comprise three or more of such arrays, as this would increase the capacity in a further but small extend, far less than by going from one to two.
The gas-outlet devices may in principle be any device and have any form, shape or structure that is suitable for removing water vapor via these devices from the reactor column. Such devices suitably comprise openings for receiving gases or vapors and channels for leading the gases or vapors to an exit or to exits and removal of the gases or vapors via the exit or exits from the reactor column.
The gas-outlet sections comprising arrays of gas-outlet devices substantially evenly spread over a cross-section of the gas-outlet section (i.e. “evenly spread” means herein that the arrays of gas-outlet devices are located at approximately equal distance from each other) favor an evenly spread out-flow of gas or vapor from a nearby heating section or two nearby heating sections and have the advantage that vapors produced in a polycondensation process in the heating sections in the reactor column are removed more uniformly, thereby preventing formation of channels in the moving packed bed in the adjacent heating section or sections and reducing the risk of solid material from being entrained with the flow of gas or vapor and being removed from the reactor column via the gas-outlet sections.
Preferably, the gas-outlet devices consist of elongated elements protruding essentially transversely with respect to the length-direction of the column into the gas-outlet sections, and wherein the elongated elements each comprise a gas-flow channel in length-direction of the elongated elements and a groove-opening or a slit-opening over the length of the elongated elements or a series of openings distributed over the length of the elongated elements.
In case the gas-outlet devices are used in combination with plate heat exchangers, they are advantageously placed perpendicular to the direction of the plates, to enhance plug flow of the solid material in the moving packed bed.
More preferably, the elongated elements have a v-shaped cross-section, a u-shaped cross-section, a semi-oblong cross-section, a semi-circular cross-section or a semi-ellipsoid cross-section, or any other cross-section, and wherein the opening or openings are facing in flow direction towards a solids discharge section. The advantages of such elongated elements with said shape is that the flow of the solid material as a moving packed bed is hampered less, while at the same time the risk of solid material from being entrained with the flow of gas or vapor and being removed from the reactor column via the gas-outlet sections is reduced.
The reactor column according to the invention can be shaped in various ways, and can be tailored, for example, to further technical requirements or in combination with specific embodiments. The space inside the reactor column is confined by the reactor wall, wherein the multifunctional zones therein are confined by sections of the reactor wall.
For example, the reactor column may have a tubular shape, or at least a main part thereof. Suitably, the multifunctional zones are confined by circular wall sections. In one embodiment, the multifunctional zones are confined by wall sections with a circular cross section. The advantage of such circular wall sections confining the multifunctional zones is that the reactor is better pressure resistant. Moreover, such circular wall sections are preferably combined with heating sections comprising vertically or essentially vertically oriented tubular heat exchangers. This has the advantage that the tubular heat exchange elements can more easily be regularly spaced from one another and distributed uniformly over a cross-section of the heating section.
In another embodiment, the multifunctional zones are confined by four wall sections comprising two essentially parallel opposite wall sections, preferably comprising two pairs of two essentially parallel opposite wall sections. This embodiment is preferably combined with essentially vertically oriented plate heat exchangers.
More preferably, the multifunctional zones are confined by four wall sections constituting an essentially rectangular cross-section. The combination of this embodiment with essentially vertically oriented plate heat exchangers has the advantage that heat exchange elements of the same size can be used and that the heat exchange elements can more easily be regularly spaced from one another and distributed uniformly over a cross-section of the heating section.
Even more preferable, the reactor column with such a rectangular cross-section is combined with a polycondensation process carried out at low pressure, for example 0.9-1.5 bara, or at a pressure in the range of −0.1 BarG and +0.5 BarG. The advantage is that the reactor column with such rectangular cross-section can be constructed relatively easily.
In a further embodiment, the reactor column is assembled from multiple column elements, comprising column elements comprising heat exchangers and column elements comprising gas-outlet devices. The advantage thereof is that the column can be easier disassembled and cleaned.
The invention also relates to an installation (which may also be referred herein to as a process installation) for a continuous solid-state polymerization process for preparing a polyamide derived from diamine and dicarboxylic acid. The installation comprises a reactor column according to the invention or any particular or preferred embodiment thereof as described herein above.
Herein the reactor column is suitably positioned vertically, or essentially vertically. This has the advantage that solid material is more easily moving as a moving packed bed through the reactor column while being transported by gravity.
With vertical is herein understood that the column is positioned upright at right angles (90°) to the horizon. With essentially vertical is herein understood that the column can be slightly tilted or inclined relative to the upright position. Herein the tilt angle or inclination angle is suitably at most 10°, preferably at most 5°, relative to the right angles of 90° relative to the horizon.
In a particular embodiment, the installation suitably comprises the reactor column according to the present invention or any particular or preferred embodiment thereof, at least one exhaust gas recovery unit and a diamine supply unit, wherein the gas-outlet sections in the multifunctional zones comprise a gas-outlet connected to an exhaust gas recovery unit, and wherein the first gas-inlet section in the residence zone comprises a gas inlet connected to the diamine supply unit. Preferably, the reactor column comprises a second gas-inlet section in the residence zone downstream relative to the first gas-inlet section, wherein the second gas-inlet section comprises a gas inlet connected to an inert gas supply unit. Herein the exhaust gas recovery unit suitably comprises a condenser. The condenser can be used to liquefy the water vapor expelled from the reactor during use of the installation in a continuous solid-state polycondensation process for preparing a polyamide from a diammonium dicarboxylate salt as described herein above.
The invention also relates to the use of the installation according to the invention in a polycondensation process, more particular in a continuous solid-state polymerization process for preparing a polyamide derived from diamine and dicarboxylic acid.
A continuous, solid-state polymerization process according to the invention was implemented in a vertically positioned reactor column according to the invention. The total equipment height is about 11 m (including transport, and charging sections), whereas the column used for the process has a height of about 7 m (including discharging section), and a virtually square cross-section of about 0.15 m2. The reactor column comprises three multifunctional zones, each comprising a heating section followed by a gas-outlet section comprising two arrays of gas outlet devices. Following the third multifunctional zone in the downward direction, there is an amine dosing section, comprising a heat exchanger, a residence section and an amine inlet device, which is followed by a residence zone, another heat exchange section, a drying section and a final cooling section.
The residence zone that is located below the amine dosing section has one gas inlet section positioned just above the heat exchange section. The function of the residence zone is to allow sufficient time to increase the molecular weight of the product on its way down the column, before reaching the next (cooling) heat exchanger, followed by the drying and final cooling sections. The latter sections are in the bottom of the column and have an additional gas inlet and an additional gas outlet to allow nitrogen to pass through the product and dry off residual water. Drying is enhanced by the relatively high temperature of around 170° C. of the product in this zone. The product temperature in the drying zone can be tuned with the heat exchanger located above the drying zone, so that drying is sufficient, and (water forming) reactions are stopped.
The column further comprises a charging section at the top of the column with a nitrogen inlet to ensure that no air enters into the reactor column and a discharge section at the bottom of the column fitted with a nitrogen inlet to ensure gases formed in the column do not leave with the product.
For the process, a salt made of a mixture of butane diamine (DAB), hexane diamine (HMDA) and terephthalic acid (TPA), in the form of a solid granular material was used. The salt granules had a particle size in the range of 0.1-0.5 mm. Before starting the polymerization, the column was filled with already reacted polymer granules, of the same particle size and shape as the salt particles, obtained previously by reacting the same salt granules in a batch reactor facility.
All viscosity numbers obtained in Examples 1-3 herein below were measured in 96% sulphuric acid (0.005 g/ml) at 25° C. by the method according to ISO 307(2019).
All levels of water content in Examples 1-3 given in ppm (or mg/kg) are on a mass basis, and were determined using Karl-Fischer coulometric titration, based on ISO 15512 (2019).
All end-group concentration values in Examples 1-3 (mEq/kg, or mmol_end_groups/kg) were determined by using 1H NMR measurements in dry, deuterated sulphuric acid. 1H NMR measurements were performed as described by C. D. Papaspyrides, A. D. Porfyris, R. Rulkens, E. Grolman, A. J. Kolkman in Journal of Polymer Science. Part A. Polymer Chemistry, vol. 54, issue 16, 2016, pages 2493-2506.
The melting temperature is measured by the DSC method according to ISO-11357-3.2 (2009), in a nitrogen atmosphere with heating rate of 20° C./min, in the first heating cycle.
At first, the heat exchangers of the multifunctional zones were heated to their respective set points and after 2 hours the solids flow rate was slowly increased to 4 kg/h, which was maintained until the polymer granules inside and in-between the multifunctional zones were heated to a temperature that was about the temperature of the heat exchanger located at nearest location, as was detected by temperature sensors positioned below each multifunctional zone. Further, heating elements in the form of electrical tracing were switched on to heat the outside of the column, which together with suitable mineral-wool insulation prevented cooling from the outside. Polymer granules were added to the hopper at the top of the column in the same manner as described for the salt herein below.
The solid granular salt material was fed from 20 kg bags into a discharge cabinet at ground level, and transported with nitrogen gas from the bottom discharge point of the cabinet to a receiving vessel at the top of the column by pneumatic transport, using nitrogen as transport gas. From the receiving vessel, the salt intermittently flowed by gravity through a valve, into a feeding hopper that was connected to the top of the reactor column. Nitrogen purged into the charge hopper of the column ensured an inert atmosphere around the granular salt material before entrance to the reactor. The feed rate of the granular salt material was gradually increased from zero to 8 kg/h within one hour time, by gradually increasing the rotational speed of the previously calibrated transport screw at the bottom of the reactor.
After entering the reactor column, the solid material passed through the first multifunctional zone wherein it was heated by the first heat exchanger, which was set to a temperature of 228° C. After the first heat exchanger, the solids passed the first gas-outlet section, where nitrogen and water vapor left the column via the first array of gas outlet devices. Passing further down, the solids passed the next array of gas outlet devices in the same gas-outlet section of the first multifunctional zone. Here, water vapor from below could flow counter-currently to the solids and leave the reactor via this second array of gas outlet devices. Progressing further downward, the solids passed the second multifunctional zone, set to a temperature of 244° C. On passing through the second heat exchanger, the solids (part salt and part polymer at this stage) were heated further, and the endothermic condensation reaction proceeded, releasing water vapor from the condensation reaction into the granule bed, which then circulated to the gas-outlet sections by means of the slight overpressure in the (superheated) steam generated under said conditions of high temperature and close-to-atmospheric pressure. After the second heat exchanger, the material passed through the second gas-outlet section, through which gases coming from above and below left the reactor column. Then, the solids passed the third multifunctional zone, wherein the solid granular material was heated further by the third heat exchanger, set to a temperature of 259° C. and water vapor produced upon further polycondensation was again removed via the gas-outlet sections located above and below the third heat exchanger. For Example 1, the granules passed through the next heating and amine dosing sections essentially unaltered, i.e. without further reaction or significant changes in composition, because the polymer was already acid-end-group terminated at this stage (all amine end-groups were used up, as shown by end-group analysis of the product herein below).
Progressing further down, the solids passed via the cooling heat exchanger into the drying section at a temperature of about 170° C. Nitrogen gas was introduced via a gas inlet in the drying section and removed via two gas-outlet sections, one above and one below the gas inlet, to evaporate residual water. After passing the drying section, the solid granular material passed through the final cooling section, wherein the solids were further cooled to a temperature below 60° C. The solids were discharged via the discharge section, comprising a hopper and a discharge screw, while a nitrogen gas was fed to the nitrogen inlet just above the discharge screw to create a counter-current upward flow of nitrogen in the bottom part of the column. The amount of nitrogen at this point was tuned so as to maintain a slight overpressure relative to the column's vapor-outlet pressure at this position. The latter was to ensure that gases formed in the column did not evaporate from the product. It took around 3 days to completely fill the column with fresh material and another 2 days to reach a steady state. A dry polymer granulate material was obtained with a relative viscosity (VN) of 52 to 55 ml/g. The column was operated at essentially atmospheric pressure in all Examples 1-3.
Thus, the polycondensation reaction from salt to polymer was completed, ending in an acid-end-group terminated polymer and the water formed during reaction was effectively removed in the three multifunctional zones. The drying section further reduced the water level to between 1000 and 1500 ppm in the final product.
The fact that the product was a loose powdery material in Examples 1-3, and that the process could proceed for days, also shows that stickiness and lumping have been avoided by the measures taken, i.e. water vapor was released and removed in the multifunctional zones, while avoiding condensation of water onto colder surfaces and cold product. In the multifunctional zones where the main conversion took place, nitrogen was not applied. In these zones, water vapor escaped as superheated steam, and was collected in the exhaust gas collecting channels that were connected to the gas outlets of the column.
The relatively low molecular weight (VN) obtained in Example 1 was due to the loss of volatile diamines that evaporated from the product together with the water vapor, as described herein above. This was verified by determining the end-group concentration of the product, thereby obtaining a concentration of less than 40 mEq/kg of residual amine end-groups (below the detection limit of the NMR method used), compared to a concentration of 260 mEq/kg of acid end-groups. The acid-to-amine balance was further controlled by applying the process as described in Example 2 and Example 3 herein below.
By applying the same conditions of temperature and flow rate as in Example 1, the amine dosing was switched on and a concentrated aqueous solution of HMDA and DAB was fed to an array of gas distributor devices via a heater-evaporator, adjusted to match the temperature of the polymer bed and the heat exchanger located just above it, thereby preheating and vaporizing the aqueous solution. The diamine containing vapor mixture was led into the amine dosing section of the reactor via the amine inlet device. The diamine-water-nitrogen vapor mixture was forced to flow upward, counter-current to the granular bed, by the nitrogen from the nitrogen inlet located below the amine feed point. Thus, the diamine was absorbed effectively by the polymer granulate in a counter-current contacting pattern. Any non-absorbed diamine, nitrogen and water vapor were led out of the column via the gas outlet section positioned above the amine dosing section. Progressing further down, the solids passed through the same drying and cooling sections as described in Example 1. The viscosity of the material obtained slightly varied over time, as the amine dosing rate was adjusted to the correct value, reaching a reasonably steady state around 30 hours after starting the amine dosing.
A loose and free-flowing polyamide polymer powder with a VN between 65 and 80 ml/g was obtained, with the concentration of amine end-groups between 90 and 110 mEq/kg and the concentration of acid end-groups between 110 and 130 mEq/kg. Water levels ranged from 1000 to 1500 ppm and the melting point (Tm) of the polymer was 346° C.
Example 2 shows that the current invention allows end group content and molecular weight to be controlled to reach a commercially relevant range useful for commercial applications as it is important to be able to steer the process to obtain products with different molecular weights to match the requirements set for different applications. Further, the process according to the present invention enables obtaining polymer specifications to be reached in a single-pass apparatus, thus saving on cost and energy, since alternative methods require re-heating, amine addition and cooling in an (costly) additional process step.
For carrying out Example 3, the solids flow rate was increased further, from 8 kg/h to 14 kg/h in 3 hours. The amine dosing amounts were gradually increased to match, i.e. to maintain the same amine to solids ratio as described in Example 2. The temperatures of the heating sections were gradually increased to match the increased heat load required for pre-heating and reaction, i.e. zone one was increased to a final set point of 230° C., the second zone to 246° C. and the third zone to 265° C. The temperature sensors in each multifunctional zone were used to monitor the local granule temperatures and heater temperatures were adjusted to maintain reasonably stable granule temperatures. 24 hours after adjusting the solids flow rate, samples taken at 2 hour intervals showed a stable VN.
The product obtained by the process as described in Example 3 was a semi-crystalline semi-aromatic polyamide in the form of a free-flowing solid granular material. The shape of the particles in the solid granular material was the same to the shape of the salt material fed into the column. The polyamide product had a melting temperature (Tm) of 345° C., measured by DSC, a viscosity number (VN) of 70-72 ml/g, amine end-groups concentration between 93 and 97 mEq/kg and acid end-groups concentration between 118 and 222 mEq/kg, with water levels ranging from 1200 to 1800 ppm.
Example 3 shows that with stable operation, VN and the level of end-groups concentration can be kept stable within a narrow range, that a higher production rate can be reached by tuning the temperature of the heat exchangers in the multifunctional zones and that the end-groups concentration level and VN can be controlled by tuning the amount of amine dosing to match the flow rate of the salt.
| Number | Date | Country | Kind |
|---|---|---|---|
| 19218085.9 | Dec 2019 | EP | regional |
| 20166164.2 | Mar 2020 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2020/087099 | 12/18/2020 | WO |
