A Separation Method And Reactor System For A Glycol-Water Mixture

Abstract

The separation method separates a polyalcohol compound from water, so as to obtain a purified product stream comprising the polyalcohol compound in an output concentration of at least 90 wt %. Thereto, a mixture of the polyalcohol compound and water is provided, said mixture having a polyalcohol concentration. The polyalcohol concentration of the mixture is increased in an evaporation stage. Subsequently, the mixture is treated in a distillation stage to deliver the purified product stream comprising the polyalcohol compound in the output concentration of at least 90 wt %. Herein, the distillation stage is operated to produce steam output, that is optionally compressed to a steam pressure, and is coupled to the evaporation stage. The maximum distillation pressure and/or said compressed steam pressure is not less than the maximum evaporation pressure. The reactor system is configured for performing the separation method.

Claims

1-29. (canceled)

30. A method of at least partially separating a polyalcohol compound from water, so as to obtain a purified product stream comprising the polyalcohol compound in an output concentration of at least 90 wt %, which method comprises the steps of: providing a mixture of the polyalcohol compound and water, said mixture having a polyalcohol concentration; increasing the polyalcohol concentration of the mixture in an evaporation stage, wherein the evaporation stage is operated at an evaporation pressure range comprising a maximum evaporation pressure at most; treating the mixture in a distillation stage to deliver the purified product stream comprising the polyalcohol compound in the output concentration of at least 90 wt %, which distillation stage is operated at a maximum distillation pressure at most, wherein the distillation stage is operated to produce steam output, that is optionally compressed to a steam pressure, which is coupled to the evaporation stage, wherein the maximum distillation pressure and/or said optional compressed steam pressure is not smaller than the maximum evaporation pressure; and wherein the maximum distillation pressure is at least 0.2 bar and less than 1.0 bar.

31. The method as claimed in claim 30, wherein the maximum distillation pressure is at least 0.4 bar, preferably at least 0.6 bar, more preferably at least 0.7 bar; and/or wherein the maximum distillation pressure is at most 0.95 bar, preferably at most 0.9 bar.

32. The method as claimed in claim 30, wherein the distillation stage is operated such that a distillation temperature within the distillation stage is at most 200° C., preferably at most 190° C., more preferably at most 180° C., even more preferably at most 170° C., even more preferably at most 160° C., and most preferably at most 150° C.

33. The method as claimed in claim 30, wherein the compressed steam pressure is higher than the maximum distillation pressure.

34. The method as claimed in claim 30, wherein the evaporation stage and the distillation stage are operated such that an evaporation temperature within the evaporation stage, as defined at atmospheric pressure, is at most 30° C. above the boiling point of pure water at atmospheric pressure.

35. The method as claimed in claim 30, wherein the evaporation stage comprises a plurality of vessels in series, each vessel working at a different pressure within the evaporation pressure range, wherein the steam output of the distillation stage is coupled to a most downstream vessel of the evaporation stage, wherein a most downstream vessel of the evaporation stage has a steam output that is coupled to a directly preceding vessel by means of heat-exchanging, and wherein the most downstream vessel is operated at a higher pressure than the directly preceding vessel.

36. The method as claimed in claim 30, wherein the polyalcohol concentration of the provided mixture is at least 40 wt %.

37. The method as claimed in claim 30, wherein the polyalcohol compound is a glycol compound, and more preferably is ethylene glycol.

38. The method as claimed in claim 30, wherein the mixture of the polyalcohol compound and water further comprises at least one of a monomer and an oligomer, each resulting from depolymerisation of a condensation polymer such as a polyester.

39. The method as claimed in claim 30, wherein the mixture is treated in a concentration stage after passing the evaporation stage, to further increase the polyalcohol concentration, wherein the mixture is heated in said concentration stage by means of waste heat supplied from a reactor.

40. The method as claimed in claim 30, wherein at least a part of the mixture is processed in a reboiler stage after passing the evaporation stage, and/or after passing the optional concentration stage, and/or after passing the distillation stage, to remove a contaminant fraction from said mixture, wherein optionally said contaminant fraction comprises components resulting from depolymerisation of a condensation polymer such as a polyester.

41. A reactor system for the separation of a polyalcohol compound from water, so as to obtain a purified product stream comprising the polyalcohol compound in an output concentration of at least 90 wt %, said reactor system comprising: an evaporation stage comprising an inlet for a mixture of the polyalcohol compound in water and an outlet for a stream enriched in the polyalcohol compound, said evaporation stage being configured for operation at an evaporation pressure range comprising a maximum evaporation pressure at most; a distillation stage comprising an inlet for the stream enriched in the polyalcohol compound arriving from the evaporation stage, an outlet for the purified product stream, and an outlet for a steam output, said distillation stage being configured for operation at a maximum distillation pressure at most, wherein the steam output is coupled to the evaporation stage, and wherein the steam output is optionally compressed to a steam pressure, such that the maximum distillation pressure and/or said optional compressed steam pressure is not less than the maximum evaporation pressure; and wherein the maximum distillation pressure is at least 0.2 bar and less than 1.0 bar.

42. The reactor system as claimed in claim 41, further comprising a steam compressor so as to compress the steam output of the distillation stage to the compressed steam pressure, such that the compressed steam pressure is higher than the maximum evaporation pressure.

43. The reactor system as claimed in claim 41, wherein the steam output of the distillation stage is coupled to a most downstream vessel of the evaporation stage.

44. The reactor system as claimed in claim 43, wherein a most downstream vessel of the evaporation stage has a steam output that is coupled to a directly preceding vessel by means of heat-exchanging, and wherein the most downstream vessel is operated at a higher pressure than the directly preceding vessel.

45. The reactor system as claimed in claim 41, further comprising a concentration stage downstream of the evaporation stage and upstream of the distillation stage, said concentration stage being provided with a supply for a heated stream originating as waste heat supplied from a reactor.

46. The reactor system as claimed in claim 41, further comprising a reboiler stage arranged downstream of the evaporation stage and/or downstream of the optional concentration stage, and/or downstream of the distillation stage, wherein the reboiler stage is configured to process at least a part of the mixture arriving from the respective stage to remove a contaminant fraction from said mixture, wherein optionally said contaminant fraction comprises components resulting from depolymerisation of a condensation polymer such as a polyester.

Description

BRIEF INTRODUCTION OF THE FIGURES

[0034] These and other aspects of the invention will be further elucidated with reference to the Figures, wherein:

[0035] FIG. 1 schematically shows a first embodiment of the reactor system of the invention, comprising a evaporation stage with a flash vessel and two distillation columns in series;

[0036] FIG. 2 schematically shows a second embodiment of the reactor system of the invention, comprising an evaporation stage with a flash vessel;

[0037] FIG. 3 schematically shows a third embodiment of the reactor system of the invention, comprising an evaporation stage embodied as a multi-effect distillation installation;

[0038] FIGS. 4, 5 and 6 schematically show variations of the first embodiment, wherein use is made of a steam compressor;

[0039] FIGS. 7 and 8 schematically show variations of the second embodiment;

[0040] FIG. 9-11 schematically show variations of the third embodiment.

[0041] FIG. 12 schematically shows an embodiment of a reboiler stage usable in the embodiments of the invention.

DETAILED DISCUSSION OF ILLUSTRATED EMBODIMENTS

[0042] The figures are not drawn to scale. The same reference numerals in different figures refer to equal or corresponding elements. Where reference is made to bars, this refers to the absolute pressure. Thus 1 bar is 10.sup.5 Pa. Each figure shows the reactor system of the invention comprising a distillation stage 100 and an evaporation stage 200. The distillation stage is in the embodiments of FIG. 1-10 embodied as a distillation column. In the embodiment of FIG. 11, the distillation stage is an effect in a multi-effect distillation installation. The distillation stage 100 may be corresponding to a distillation column 220, 230 or effect in the evaporation stage 200, but that is not necessary. In any case, the distillation stage 100 is driven by power from outside the reactor system, such as high-pressure steam (not shown in the figures).

[0043] It is observed for clarity that the reactor system of the invention is suitably preceded by further reactor systems in which the mixture of polyalcohol compound, preferably glycol, for instance ethylene glycol, and water is generated. Typically, said mixture contains any further compound, which is removed from the mixture in one or more pre-treatments. For instance, a glycol such as ethylene glycol, is used for the catalysed depolymerisation of a polyester or polyamide or the like. One specific example is the catalysed depolymerisation of polyethylene terephthalate in ethylene glycol, wherein water is added for cooling and separation purposes, so as to remove catalyst and oligomers by means of a centrifuge treatment. The resulting mixture will comprise particulate contaminants to be filtered out and monomer and/or oligomer for the polyester, such as BHET (bis-hydroxyethyl terephthalate), which is to be separated via crystallisation and a solid-liquid separation.

[0044] As will be elaborated hereinafter, the catalysed depolymerisation may be carried out in a batch-mode and at a temperature close to the boiling point of the glycol (typically ethylene glycol), thus for instance in the range of 160-200° C., preferably at 180-200° C. The emptying of the depolymerisation reactor leads to liberation of heat. In specific implementations of the process and the reactor system of the invention, this heat is reused in the dehydration of the glycol.

[0045] Typically, the mixture of the polyalcohol compound and water has a concentration of the polyalcohol compound of at least 40 wt %, preferably at least 45 wt %, more preferably at least 50 wt %. If the concentration of the polyalcohol compound is lower, it can be increased in a suitable manner. This could be carried out by means of a flash vessel, membrane distillation, or any other known technique. It is not critical, as the boiling point of the mixture wherein the polyalcohol compound is lower than 40 wt % is not very sensitive to the concentration.

[0046] According to the invention, the purified mixture has a concentration of the polyalcohol compound of at least 90 wt %. The concentration may well be higher, such as at least 95% or at least 99% by weight. In case of the regeneration of a mixture originating from depolymerisation, the mixture will further comprise some dissolved compounds resulting from the depolymerisation, such as monomers, dimers and further oligomers. A concentration of the polyalcohol compound of 100% will then not be feasible. It is not excluded that the regenerated polyalcohol composition comprises some other additives, such as salts.

[0047] Turning to FIG. 1, a reactor system is shown with a distillation stage 100, embodied as a distillation column, and an evaporation stage 200, embodied with three substages: a flash vessel 210 and two further columns or vessels 220, 230. A feed stream 199, being a mixture of polyalcohol compound, water and any further additives with an initial concentration of polyalcohol compound, for instance between 40 and 50 wt %, enters the evaporation stage 200 at feed inlet 201. It then enters the first substage 210, which is a flash vessel in the shown embodiment. The flash vessel is boiling under reduced pressure and temperature, in the current embodiment for instance 0.2 bar and 60° C. Steam leaves the vessel 210 via steam outlet 213 and is led to a condenser 240 after passing a heat exchanger 241. The stream 219 enriched in the polyalcohol compound leaves the flash vessel at the bottom.

[0048] Part thereof 214 returns into the vessel 210 after passing a heat exchanger 215. This heat exchanger 215 is also known as a reboiler. Such reboiler may be implemented as being part of the flash vessel 210 (or any distillation column), or be a separate device. A pump may be present as part of the return branch 215, but this is not deemed strictly necessary. The mixture in said return branch 214 is heated in the reboiler/heat exchanger 214 with the steam 228 originating from the second substage 220. As a consequence, the temperature at the bottom of the first substage 210 will be equal or almost equal to that of the steam 228. The term ‘almost equal’ herein refers to any deviation resulting from heat losses in the transport and in the heat exchange. In one further implementation, distillation trays are present in the flash vessel 210 in between the feed inlet 199 and the inlet from the reboiler 214. The distillation trays below the feed inlet 199 leads to some distillation without requiring a reflux flow. That turns out to have a positive effect on the effective evaporation, which is beneficial for overall operation. Furthermore, it contributes to operation stability of the flash vessels at relative low pressures, such as pressures below 0.5 bar

[0049] The operation of the second substage 220 and the third substage 230 is essentially a repetition of that of the first substage 210. However, even if the first substage 210 does not comprise any distillation trays, it is preferred that the second and third substage 220, 230 include such distillation trays. These trays will be located between the feed inlet (from stream 219, 229) and the reboiled stream 224, 234. In comparison to the use of distillation columns for the second and third substage 220, 230 of the evaporation stage, no reflux is present. This is cost effective and allows operating the substages 220, 230 with top and bottom temperatures that deviate from the effective boiling points. Moreover, and even more importantly, the presence of distillation trays brings the advantage that any polyalcohol, such as ethylene glycol, evaporating with the water in a reboiler, will be washed out from the vapour, and flow back with the feed towards the outlet at the bottom. As a consequence, the water vapour leaving these substages 210, 220, 230 at their steam outlets 213, 223, 233 will contain less contamination with polyalcohol, i.e. have a higher grade of purity.

[0050] Furthermore, as will be understood, the pressure, temperature and concentration of polyalcohol compound are higher in the second and the third substage 220, 230 than in the first substage 210. The most downstream substage 230 receives its heat from the steam 192 from the distillation stage 100, which leaves the distillation stage 100 at steam output 103. For sake of efficiency, the embodiment illustrated in FIG. 1 but also the embodiments illustrated in other figures are designed so as to reduce the water content of the feed at the input 101.

[0051] The distillation stage 100 further has an inlet 101 for the enriched stream 239 originating from the evaporation stage 200, a product outlet 102 for the purified stream 191 and a heat exchanger 105 in a return branch 104. Although not indicated in FIG. 1, this heat exchanger 105 is suitably the feed into the distillation stage 100 for high-pressure steam. The remaining, low pressure steam may be led further as stream 193 (see FIG. 2) to transfer remaining heat to the evaporation stage 200. While not shown, the distillation stage 100 furthermore is provided with reflux means as known per se to the skilled person. Herein, the steam 192 leaving the distillation stage 100 at steam output 103 is split into a portion towards the reboiler 235 (or alternatively 215 as in FIG. 2) of the preceding stage, and a portion from refluxing. The refluxing involves condensing the steam, leading the condensed steam to a reflux drum and pumping the liquid from the reflux drum back into the top of the distillation stage 100. The exact implementation of the reflux means is open to variations, as the skilled person will understand.

[0052] By means of this sequence, wherein the pressure gradually increases, the mixture can be enriched in the polyalcohol compound stepwise, wherein the liberated water is roughly equal in each of the steps (roughly equal implying within a margin of at most 50%, suitably at most 30%). Furthermore, it is achieved herein, that the boiling temperature does not increase too much. As will be visible from Table 1, the steam 228 leaving the distillation stage 100 at steam output 103 has a temperature of 92° C. only and the maximum distillation temperature is 150° C.

TABLE-US-00001 TABLE 1 operation of multistage reactor system shown in FIG. 1. stage Evaporation stage Substage Distillation Feed 1.sup.st substage 2.sup.nd substage 3.sup.rd substage stage Glycol (ton/hr) 5 5 5 5 5 Water (ton/hr) 5 3.8 2.6 1.4 0.2 Glycol concentration (wt %) 50 57 66 78 96 Evaporated water 1.2 1.2 1.2 1.2 temperature at top of stage (° C.) 54 63 74 92 Pressure at top of stage (bar) 0.15 0.22 0.37 0.75 temperature at bottom of stage (° C.) 63 74 92 150 Pressure at bottom of stage (bar) 0.16 0.23 0.38 0.76 Required steam pressure (bar) 0.22 0.37 0.75 4.9

[0053] FIG. 2 schematically shows the reactor system of the invention according to a second embodiment. In this second embodiment, the evaporation stage 200 comprises a flash vessel 210 only. Such a system benefits less from the stepwise pressure decrease to arrive at a balanced evaporation per stage. However, the operation of the system is feasible and energetically efficient, in the reuse of heat. The principles shown in relation to this figure could also be applied to a reactor system comprising an evaporation stage 200 with a plurality of distillation columns. In the shown system, the high-pressure steam is used for heating the distillation stage 100 via heat exchanger 105 to a return branch 104. Thereafter, the steam 193 can still be applied to pre-heat the enriched stream 219 that will enter the distillation stage at its inlet 101. Still, the rest-steam is useful, as it can be used for heating the feed 199 that will enter the flash vessel 210 at its inlet 201. The increased temperature of the feed 199 will lead to evaporation under the reduced pressure conditions in the evaporation stage 200, such as in the flash vessel 210. This is particularly effective in the method of the invention, wherein the flash vessel operates at a lower pressure than the distillation stage, as the lower pressure results in a lower boiling temperature in the flash vessel 210. Hence, it becomes feasible to evaporate a significant portion of the water in the water-alcohol mixture in the flash vessel, which is clearly beneficial to achieve the desired result of an alcoholic solvent with at most minor parts of water therein.

[0054] In the context of the second embodiment, the pressure of the distillation stage is preferably in the range of at least 0.4 and less than 1.0 bar, and the pressure at the flash vessel is suitably 20-60% thereof, for instance at most less than 1.0 bar and preferably 0.1-0.6 bar.

[0055] Additionally, as shown in this FIG. 2, the steam 192 produced in the distillation stage 100 is led via heat exchanger 205 to a condenser 140. In this manner, the heat of the distillation stage 100 is effectively transferred to the evaporation stage 200. Furthermore, the distillation stage 100 may be charged via an additional inlet 109 with an additional, predominantly liquid stream. Such additional stream suitably originates from another part of the process, such as a centrifuge. It is typically a hot stream upon entry of the distillation stage 100, so as that its temperature would not disturb operation of the distillation stage 100. It is deemed preferable to add such predominantly liquid stream 109 only in the distillation stage 100, in order to prevent contamination of the preceding stages. While a variety of liquid streams could be used with different degree of purities, it is not excluded that such predominantly liquid stream contains specific contaminants in the form of particles or solutes. One example of a particulate contaminants is for instance a heterogeneous catalyst.

[0056] FIG. 3 schematically shows the reactor system of the invention according to a third embodiment. Herein, the evaporation stage 200 is embodied as a multi-effect distillation (MED) installation 280. While the first effect 280A of the multi-effect distillation installation may operate at the same low pressure (or even below that pressure) as the first substage 210 of the evaporation stage 200 according to the first embodiment, the volume of the first effect 280A does not need to be as large as that of the flash vessel of the first substage 210 in the first embodiment. In fact, if the capacity of a single first effect 280A would be insufficient, it is feasible to add an extra effect or extra MED installation 280.

[0057] The MED installation 280 shown in FIG. 3 comprises three effects 280A, 280B, 280C. Feed 199 enters the evaporation stage 200 and thus the MED installation 280 at inlet 201. It then passes a feed distributor 282, which divides the stream into a plurality of droplets, so as to spray the feed onto individual levels of the first effect 280A. Heat is provided into this first stage 280A by means of a heating channel 281. Additionally, the steam 912 from the distillation stage is led to the MED-installation 280. An effect 280A,B,C leads to separation of the water vapor from remaining liquid through a membrane. The water vapour is condensed against a wall. Liberated heat is transmitted through the wall to the adjacent effect. The resulting condensate is removed via a condensate outlet 288. The remaining and concentrated liquid, leaves an effect 280A, 280B, 280C via a second outlet 286, and is thereafter pumped to a corresponding inlet 287 of the subsequent effect, or for the most downstream effect 280C to the distillation stage 100. A pump is needed herein between each stage, so as to achieve that the liquid mixture flows from low pressure to higher pressure. Steam remaining in the most upstream effect 280A is led to a condenser 240.

[0058] FIG. 4-6 shows variations of the first embodiment, wherein use is made of a steam condenser 160, 260. The use of a steam condenser 160, 260 is deemed advantageous in the context of the invention, as it allows to limit the effective range between the lowest pressure and the highest pressure in the reactor system when applying the method. Still, the number of substages in the evaporation stage can be sufficiently high or even be optimal.

[0059] In the embodiment schematically shown in FIG. 4, a steam condenser 160—also indicated with SC—is arranged between the steam outlet 103 of the distillation stage 100 and a heat exchanger of the evaporation stage 200, and more particularly, the heat exchanger 235 of the substage 230 that is arranged most downstream within the evaporation stage 200, thus at the highest pressure. It would not be impossible to lead to the steam compressed stream 192 to the heat exchanger of another substage 210, 220. This is particularly feasible if the heat exchanger 235 can be fed with heat from another heat source. Although not indicated in this figure, it is feasible that the steam applied to the heat exchanger 105 of the distillation stage 100 is reused thereafter to heat the enriched mixture 239 being fed to the distillation stage 100 and/or to heat (or pre-heat) the mixture of polyalcohol compound and water at another location within the reactor system.

[0060] The effect of the steam compressor can be understood from Table 2 and the comparison with Table 1. While the flow rates, and the rate of evaporation of water, are the same in the embodiments without and with steam compressor (FIG. 1 and FIG. 4 respectively), the pressure in the first substage is 50% higher in the embodiment with steam compressor than without (0.22-0.23 vs 0.15-0.16 bar). As a consequence, the volume of the 1.sup.st substage (suitably a flash vessel) can be reduced significantly. Corresponding thereto, the temperatures are higher in the substages of the evaporation stage, i.e. between 63 and 112° C., rather than between 54 and 92° C. When looking at the required steam pressure, the minimum pressure is 0.37 bar, rather than 0.22 bar. This simplifies handling and construction of the reactor system.

TABLE-US-00002 TABLE 2 settings for the operation of the reactor system shown in FIG. 4 stage Evaporation stage Substage Distillation Feed 1.sup.st substage 2.sup.nd substage 3.sup.rd substage stage Glycol (ton/hr) 5 5 5 5 5 Water (ton/hr) 5 3.8 2.6 1.4 0.2 Glycol concentration (wt %) 50 57 66 78 96 Evaporated water (ton/hr) 1.2 1.2 1.2 1.2 temperature at top of stage (° C.) 63 74 92 92 Pressure at top of stage (bar) 0.22 0.37 0.75 0.75 temperature at bottom of stage (° C.) 74 92 112 150 Pressure at bottom of stage (bar) 0.23 0.38 0.76 0.76 Required steam pressure (bar) 0.37 0.75 1.5 4.9

[0061] It is observed that the present example uses steam compression from 0.75 to 1.5 bar, which is known to provide sufficient power so that the temperature in the 3.sup.rd substage can be 92° C. at 0.75 bar. It is clearly not excluded that the steam compressor would compress the steam less strongly, for instance to increase the pressure with 50% (or 0.37 bar), rather than 100% (0.75 bar) relative to the pressure in the distillation stage. Less pressure increase facilitates a simpler steam compressor, with the effect that the pressure in the first substage will be reduced in corresponding manner. Evidently, one could additionally choose to increase the pressure in the distillation stage 100 and reduce the steam compression ratio (=output pressure versus input pressure) relative to the ratio of 2 indicated in Table 2.

[0062] In the embodiments shown in FIG. 5 and FIG. 6, a steam compressor 260 is arranged in the steam line 218 at the steam output 213 of the first substage 210 of the evaporation stage 200. The substages are embodied as flash vessel provided with a reboiler 215, 225, 235 and preferably some distillation trays between the feed inlet 199 and the inlet from the reboiler 215. The resulting stream of compressed steam 217 is merged with the steam that leaves the steam outlet from a substage that is arranged more downstream. It appears preferred, though not necessary, that said substage is the second substage 220, which is indicated in FIG. 5 and FIG. 6. The resulting stream of steam 228 will be more or less at the outlet pressure of the second substage 220. This steam is then strong enough to maintain the first substage 210 at appropriate pressure and temperature, which are in the example of FIGS. 5 and 6, 0.16 bar and 63° C. for the steam at the outlet 103, and 73° C. and 0.23 bar for the enriched liquid mixture 219.

[0063] In the embodiment of FIG. 5, the distillation stage is operated at a pressure of 0.75 bar. It will be understood by the skilled person, that one may alternatively operate this distillation stage at a lower pressure, down to 0.2 bar, and then apply another steam compressor to the steam 192, as shown in FIG. 4.

[0064] In the embodiment of FIG. 6, a concentration stage 500 is present upstream of the distillation stage 100 and downstream of the evaporation stage 200. This concentration stage is heated by means of a stream of heat 534, typically steam, originating from an external heat source, more particularly waste heat, such as waste heat from an emptied reactor. Therefore, the steam 192 from the distillation stage 100 is led directly to the most downstream vessel 220 in the evaporation stage 200, passing over the concentration stage 500.

[0065] The concentration stage 500 comprises in this embodiment two substages 510, 520, each of which is embodied, in the illustrated embodiment, corresponding to the substages 210, 220 of the evaporation stage 200. Hence the vessels 510, 520 are each provided with feed inlet, steam outlet 513, 523, reboilers 515, 525. The mixture flows from the second substage 220 as a stream 229 enriched in polyalcohol to the inlet of the third substage 510. The further enriched mixture 519 flows or is flown (by means of a pump, if needed) to the fourth substage 520. The again further enriched mixture 529 flows to the inlet 101 of the distillation stage 100. In the illustrated embodiment, the heat stream 534 has a temperature of more than 190° C. and its volume is set so as to allow heating the fourth substage 520 to achieve a temperature of 120° C. at 2 bar pressure at its steam outlet 523. In the third substage 510, the temperature at the steam outlet 513 is 97° C. at a pressure of 0.9 bar. The temperature of the mixture 519 is about 120° C. and that of the mixture 529 even 160° C. In view of the chosen pressures, there is no need to apply steam compression to the steam 192 originating from the distillation stage 100.

[0066] Rather than choosing that the evaporation rate is equal in all substages 210, 220 of the evaporation stage 200, 510, 520 of the concentration stage and in the distillation stage 100, it is feasible and may well be useful, to set the evaporation rates in a manner which would minimize overall reactor sizes. For instance, one may choose to reduce the evaporation rate in the first substage 210, while another substage could be increased. For instance, the second substage 220 could be larger and/or could be embodied as two vessels in parallel.

[0067] FIG. 7-8 shows variants of the second embodiment of the invention as schematically shown in FIG. 2. FIG. 7 shows an option to enable further reuse of heat. This is done by means of heat exchange on a stream 409. Additionally, a predominantly liquid stream 109 may be added into the distillation stage 100. The stream 409 and the liquid stream 109 originate for instance from a reactor, such as a depolymerisation reactor which operates at a temperature higher than the temperatures used in the operation of the method of the present invention. The stream 409 originates from a buffer tank 400, designed to as to convert temporal batches 401 originating from a batch reactor into a continuous stream 409. Heat exchanging occurs in heat exchanger 410. The receiving stream 411 is for instance water and/or steam, but could be any type of heat transfer medium, including oil. The receiving stream 411 can thereafter be heat exchanged with the feed 199, but is alternatively applied to heat the flash vessel 210 directly, for instance as a jacket around the vessel 210. In the embodiment shown in FIG. 8, steam compression is applied to the steam output 218 of the first (and only) substage 210 of the evaporation stage 200. This occurs by means of steam compressor 260. The compressed stream 217 is merged with a stream of steam originating from a downstream stage, in this example the steam 192 originating from the distillation stage 100. It is furthermore shown in this FIG. 8, that the stream 409 (originating from a reactor) is heat-exchanged in heat exchanger 399 with the feed 199. In order to match the available heat in stream 409 with the heat needed for the feed 199, the feed is herein split into a first feedline 199A, which does not pass the heat exchanger 399 and a second feedline 199B, which passes the heat exchanger 399. The first feedline 199A thus constitutes a bypass. By controlling the flow rates in the first and the second feedline 199A, 199B, the feed heating can be tuned so as to be efficient without obtaining a too vigorous boiling in the flash vessel 210. Instead of a heat exchanger 399, a kettle boiler may be used. Such kettle boiler will operate under the vacuum of the distillation stage 100. It is not excluded that some glycol, such as ethylene glycol is added, so as to ensure that the viscosity of the enriched mixture remains correct.

[0068] FIG. 9-11 show three variants on the third embodiment using a multi-effect distillation (MED) installation 280. In the embodiment schematically shown in FIG. 9, the MED-installation 280 comprises four effects 280A-280D. In the embodiment of FIG. 10, the MED-installation 280 comprises five effects 280A-280E. In the embodiment of FIG. 11, the MED-installation 280 comprises six effects 280A-280F. Notwithstanding the integration into a single MED-installation 280, there is a conceptual distinction between the first three stages 280A-C and the remaining stages 280D, 280E, 280F. The first three stages 280A-C constitute the evaporation stage as has been discussed hereinabove. This evaporation stage 200 is heated by means of the steam 192 originating from the distillation stage 100. As in the implementation with separate vessels and columns 210, 220, 230, each effect operated at a separate pressure, wherein the pressure increases from the first effect 280A towards the third effect 280C.

[0069] The remaining effects 280D, 280E, 280F are part of a concentration stage 500. No use is made of steam evaporation herein. Rather, the effects are embodied as heat exchangers, wherein another liquid or gas flows through channels or tubes and does not get into contact with the feed stream of the said effects. The liquid or gas typically originates from an external heat source. That may be a stream from a reactor, or alternatively based on waste heat. More particularly a heat stream 534 is supplied and is circulated via tubes 541 through the effect 280D (in FIG. 9) of the effects 280D and 280E (FIGS. 10 and 11). It leaves the stage as stream 535, and is then discarded as waste (although it is not excluded that the stream 535 would be reused). The tubes can be embodied according to any suitable shape, include trays with holes. The resulting mixture concentrated 519 is led to the inlet of the distillation stage 100

[0070] In the FIGS. 10 and 11, the heat stream 534 is led from the fifth effect 280E to the fourth effect 280D via extension 536. It is observed that merely heat exchange occurs in these effects 280D, 280E. As a consequence, the pressure is equal in both effects 280D, 280E and a separation barrier 281 is not needed between the two effects 280D, 280E.

[0071] In FIG. 11, the concentration stage 500 comprises a sixth effect 280F, which is fed by a heat stream 537, extending through the effect by means of a circulation system 543. This sixth effect 280F is held at the same pressure as the preceding effects 280D, 280E of the concentration stage 500. In the embodiment shown in FIG. 11, a further recycle 289 of steam is provided. This is recycle from the second substage or effect 280B back to the distillation stage 100. Hence, steam 192 is provided from the distillation stage 100 to the top of the second effect 280B, and is after passing this second effect 280B returned to the distillation stage 100 via recycle 289. As will be understood, the recycle may be either steam or liquid or a mixture of both.

[0072] Although not shown, it is not excluded that part of the steam 192 originating from the distillation stage 100 is led to the first effect 280A, or that the steam/liquid from the second effect 280B is further led to the first effect 280A. Typically, in multi-effect distillation, heat will be transmitted via the separation wall or barrier 281 between the effects. Although merely shown diagrammatically in the FIGS. 9-11, each effect is preferably designed in corresponding manner so as to allow integration. The construction of a multi-effect distillation installation is known per se and feasible for an expert on multi-effect distillation installations.

[0073] In one example of operating the installation shown in FIG. 9. the enriched stream leaving the first effect 280A at the output 286 towards the entry 287 of the second effect 280B, has a temperature of 70° C. (with about 57 wt % glycol). At the bottom of the second effect 280B, the temperature is 80° C. (with about 67% glycol). At the bottom of the third effect, the temperature becomes 97° C. (with about 78% glycol). The fourth effect 280D, that is heated with a separate heat stream 534, for instance entering the fourth effect at a temperature of 195-200° C. results in a temperature of 135° C. for the enriched mixture 219 and a glycol concentration with would arrive at 90 wt %. FIG. 9 shows additionally the use of a steam compressor 260, which compresses steam from the first effect 280A to a higher pressure, herein about 1 bar, rather than (or optionally in addition to) transferring said steam to a condenser. The increased flow of steam into the third effect 280C is effective to boost the evaporation. As a consequence, it becomes feasible to reduce the size of the distillation column in the distillation stage 100. It is observed for sake of clarity that the steam 192 originating from the distillation stage 100 as well as the compressed stream 217 would enter into the heating channel 281 of the MED-installation 280.

[0074] FIG. 12 shows an embodiment of a reboiler stage, which is usable in the embodiments of the invention. In the embodiment, a mixture stream 239 enriched in polyalcohol compound, which arrives from an evaporation stage 200, is divided into a mixture stream 239a, which is supplied to the distillation stage 100 at the inlet 101 for the stream 239a enriched in the polyalcohol compound and arriving from the evaporation stage 200, and a mixture stream 601, which is supplied to the reboiler stage 600. The volume ratio between the mixture stream 239a supplied to the distillation stage 100 and the mixture stream 601 supplied to the reboiler stage 600 may be suitably controlled. In an example, the mixture stream 601 supplied to the reboiler stage 600 is selected within the range 0-100 volume-%, preferably 0-20 volume-%, of the mixture stream 239 arriving from an evaporation stage 200.

[0075] The reboiler stage 600 is configured to process the mixture stream 601 by forming an evaporation stream 602 at a top outlet of the reboiler stage 600. In this embodiment, said evaporation stream 602 is supplied to the distillation stage 100. The distillation stage 100 comprises an inlet 106 for said stream 602, which is arranged at any position of the distillation stage 100, for instance close to the inlet 101 for the stream 239.

[0076] The reboiler stage 600 is further configured to remove a contaminant fraction as a contaminant stream 603 from said mixture stream 601 arriving from the evaporation stage 200. Said contaminant fraction or contaminant stream 603 has a higher boiling temperature than the evaporation stream 602. The contaminant fraction is enriched in dissolved reaction components resulting from depolymerisation of a condensation polymer, such as a polyester or a polyamide. Said reaction components may typically comprise monomer and/or oligomer derived of said condensation polymer. Said dissolved reaction components increase the boiling temperature of the polyalcohol mixture.

[0077] Said reboiler stage maybe heated by any heat stream, such as originating from an external heat source, more particularly waste heat, such as waste heat from an emptied reactor.

[0078] In alternative or additional embodiments, the reboiler stage may be arranged downstream of a concentration stage 500 or downstream of a distillation stage 100 to process a mixture stream arriving 602 from the concentration stage 500 or the distillation stage 100 by forming an evaporation stream at a top outlet of the reboiler stage 600 and to remove a contaminant fraction as a contaminant stream 603 from said mixture stream.

[0079] The reboiler stage according to any of these embodiments may be used in combination with any of the embodiments of the invention, as shown in FIG. 1-11.

LIST OF REFERENCE NUMERALS

[0080] 100 distillation stage [0081] 101 inlet for a stream (239, 219) enriched in the polyalcohol compound and arriving from the evaporation stage 200 [0082] 102 outlet for the purified product stream 191 [0083] 103 outlet for a steam output 192 [0084] 104 return branch [0085] 105 heat exchanger [0086] 106 inlet for a evaporation stream 602 arriving from the reboiler stage 600 [0087] 109 inlet for predominantly liquid rest stream [0088] 125 heat exchanger in the feed stream [0089] 140 condensor [0090] 160 steam compressor [0091] 191 purified product stream [0092] 192 steam output stream [0093] 193 heat stream (for instance steam) from the distillation stage 100 to the evaporation stage 200 [0094] 199 feed stream [0095] 199A feed stream shortcut [0096] 199B feed stream passing heat exchanger 420 with hot outlet stream [0097] 200 evaporation stage [0098] 201 feed inlet [0099] 210 first substage of evaporation stage 200 (for instance embodied as flash vessel) [0100] 213 steam outlet of the first substage 210 [0101] 214 return branch (from enriched stream 219) [0102] 215 heat exchanger [0103] 218 steam outlet stream [0104] 217 stream of compressed steam [0105] 219 mixture stream enriched in polyalcohol compound [0106] 220 second substage of evaporation stage 200 (for instance embodied as distillation column) [0107] 223 steam outlet of the substage 220 [0108] 224 return branch (from enriched stream 229) [0109] 225 heat exchanger [0110] 228 stem output stream being led to heat exchanger 215, 315 of preceding substage 210, 310 [0111] 229 mixture stream enriched in polyalcohol compound [0112] 230 third substage of evaporation stage 200 (for instance embodied as distillation column) [0113] 233 steam outlet of the substage 230 [0114] 234 return branch (from enriched stream 239) [0115] 235 heat exchanger [0116] 238 stem output stream being led to heat exchanger 225 of preceding substage 220 [0117] 239, 239a mixture stream enriched in polyalcohol compound [0118] 240 condenser (coupled to the first substage 210 when embodied as flash vessel) [0119] 241 heat exchanger [0120] 260 steam compressor [0121] 280 multi-effect distillation installation [0122] 280A,B,C,D,E,F individual effects of the multi-effect distillation installation 280 [0123] 281 heating channels between individual effects 280A,B,C [0124] 282 feed distributor [0125] 286 outlet for stream enriched in the polyalcohol compound [0126] 287 inlet for stream enriched in the polyalcohol compound [0127] 288 outlet for condensate [0128] 289 channel leading stream enriched in the polyalcohol compound from the effect inlet 287 to the distributor 282 [0129] 310 further substage of evaporation stage 200 [0130] 314 return branch (from enriched stream 319) [0131] 315 heat exchanger [0132] 318 stem output stream being led to heat exchanger 215 of preceding substage 210 [0133] 319 mixture stream enriched in polyalcohol compound [0134] 399 heat exchanger between hot outlet stream 409 and feed stream 199B [0135] 400 buffer tank [0136] 401 inlet for buffer tank [0137] 409 hot outlet stream [0138] 410 heat exchanger for outlet stream [0139] 411 heat stream between heat exchanger 410 and substage (210) of evaporation stage [0140] 416 outlet for heat stream after heating multieffect distillation installation 280 [0141] 417 connection for heat stream between effects D, E in multi-effect distillation installation 280 [0142] 418, 419, 420 heat stream for heating effects D, E, F of multieffect distillation installation 280 [0143] 434 waste heat stream [0144] 500 concentration stage [0145] 600 reboiler stage [0146] 601 mixture stream supplied from the evaporation stage 200 to the reboiler stage 600 [0147] 602 evaporation stream [0148] 603 contaminant stream