NL2035399B1 - Device and method for distillation - Google Patents
Device and method for distillation Download PDFInfo
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- NL2035399B1 NL2035399B1 NL2035399A NL2035399A NL2035399B1 NL 2035399 B1 NL2035399 B1 NL 2035399B1 NL 2035399 A NL2035399 A NL 2035399A NL 2035399 A NL2035399 A NL 2035399A NL 2035399 B1 NL2035399 B1 NL 2035399B1
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- 238000004821 distillation Methods 0.000 title claims abstract description 52
- 238000000034 method Methods 0.000 title claims abstract description 14
- 239000000203 mixture Substances 0.000 claims abstract description 96
- 230000003993 interaction Effects 0.000 claims abstract description 18
- 239000012530 fluid Substances 0.000 claims description 186
- 238000000926 separation method Methods 0.000 claims description 122
- 239000007788 liquid Substances 0.000 claims description 90
- 238000012856 packing Methods 0.000 claims description 77
- 238000009833 condensation Methods 0.000 claims description 21
- 230000005494 condensation Effects 0.000 claims description 19
- 238000010992 reflux Methods 0.000 claims description 19
- 238000001816 cooling Methods 0.000 claims description 12
- 238000001704 evaporation Methods 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 12
- 238000010438 heat treatment Methods 0.000 claims description 10
- 239000002184 metal Substances 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 description 9
- 230000009286 beneficial effect Effects 0.000 description 7
- 230000008901 benefit Effects 0.000 description 7
- 230000009993 protective function Effects 0.000 description 7
- 230000000694 effects Effects 0.000 description 6
- 230000008016 vaporization Effects 0.000 description 6
- 238000002156 mixing Methods 0.000 description 5
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000003321 amplification Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 238000003199 nucleic acid amplification method Methods 0.000 description 3
- 230000002441 reversible effect Effects 0.000 description 3
- 239000011800 void material Substances 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 230000021615 conjugation Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000001419 dependent effect Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000001965 increasing effect Effects 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000012808 vapor phase Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 241000446313 Lamella Species 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000014509 gene expression Effects 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/02—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in boilers or stills
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/26—Fractionating columns in which vapour and liquid flow past each other, or in which the fluid is sprayed into the vapour, or in which a two-phase mixture is passed in one direction
- B01D3/28—Fractionating columns with surface contact and vertical guides, e.g. film action
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/32—Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to a device and method for distillation of mixtures. The device and method are configured for providing heat exchanging interaction with at least a 5 fraction of the mixture to be distilled within the reboiling and condensing section in an efficient manner and for controlling the vapor equilibrium of the feed and/or the orientation of the flow of the feed.
Description
Device and method for distillation
The invention relates to a device for distillation of mixtures. The invention also relates to the use of a device according to the present invention. The invention further relates to a method for distillation of mixtures.
Despite the wide variety of known separation techniques available, distillation is nowadays still the most widely used. The proven technology of distillation has for example as a benefit that high purity products can be obtained and that it is capital wise relatively cheap. A drawback of distillation is that it is relatively energy consuming, in particular in case of binary mixtures having close boiling points. In addition to this, conventional distillation typically has a relatively low thermal efficiency, which may be in a range of 10 to 20%. Various distillation techniques have been developed over the years in order to attempt a reduction in energy consumption whereof secondary reflux and vaporization distillation (SRV) and the heat integrated distillation column (HIDIC) are examples. However, said technologies have not been applied for industrial application yet.
An improved device for distillation having an improved thermal efficiency and a reduced energy consumption is described in the applicants earlier application WO 2021180900 A1. Despite the promising results of this first horizontally oriented distillation device, a drawback which was experienced is that the isotherm representing the feed composition strongly depends on the vapor equilibrium of the feed (mixture). This has a negative impact upon the thermal efficiency of the device.
Hence, it is a goal of the invention to provide a device for distillation having a further improved thermal and/or thermodynamic efficiency.
The invention provides thereto a device for distillation of mixtures, comprising: - at least one inlet for feeding a mixture to be distilled to the device, - at least one housing comprising a: o at least one reboiling section wherein heat is provided to at least part of the liquid fraction of the mixture to be distilled such that at least part of said liquid fraction vaporizes,
o atleast one condensing section wherein at least part of the vapor fraction of the mixture is cooled such that at least part of said vapor fraction is condensed, and o atleast one separation section which is at least partially enclosed between the reboiling section and the condensing section, and wherein the separation section is in fluid connection with both the reboiling section and the condensing section, wherein the separation section is configured for providing vapor/liquid contact between at least part of the vapor fraction and part of the liquid fraction of the mixture to be distilled, - at least one vapor outlet and/or at least one liquid outlet, and - preferably at least one closed fluid circuit which is configured for providing heat exchanging interaction with at least a fraction of the mixture to be distilled within the reboiling section and within the condensing section, wherein the housing is in particular substantially horizontally oriented, and wherein at least part of the separation section comprises at least two different types of packings, wherein at least one packing is a structured packing which is in particular configured for enabling substantially vertically oriented fluid flow.
The distillation device according to the present invention benefits of an improved thermal efficiency due to the separation section comprising at least two different types of packings, wherein at least one packing is a structured packing which is in particular configured for enabling substantially vertically oriented fluid flow, in particular vertically oriented vapor flow. The structured packing enables further control of the vapor equilibrium of the feed. The separating section comprising a structured packing which is configured for enabling substantially vertically oriented fluid flow results in that a substantially vertical flow (y-direction) is initiated in at least part of the separation section. Correspondingly, there will be in this region a relatively low void fraction in the horizontal (x-direction), in particular below 10%, instead of a conventional relatively high void fraction in horizontal direction. The low void fraction in horizontal direction in combination with a relatively high pressure drop results in that there will be substantially now horizontal flow of fluid, in particular vapor. This results in that the isotherm of the feed composition is shifted towards a more beneficial position considering thermal efficiency. As a result, the device according to the present invention enables that higher concentrations for the light key can be obtained in a distillation process. This can also be at least partially explained by vertical vapor flow raising the L/V, at least in the condensing section, in particular on the condenser side, if applied. The L/V can be close to reflux conditions.
Generally, the arrangement of the reboiling section, separation section and condensing section within the housing provides a clever cooperation and/or mutual interaction between said sections. Therefore, the separation section can be in fluid connection with both the reboiling section and the condensing section, whilst maintaining a relatively space efficient configuration. The reboiling section, condensing section and separation section are typically positioned within the housing. A further advantage of the present device is that the thermodynamic efficiency and/or thermal efficiency can be significantly improved, up to levels of 80 to 90%. Typically, the thermodynamic and/or thermal efficiency is at least 50 to 60% improved by making use of the device according to the present invention. It is even conceivable that in practice the thermal efficiency will be higher than 90%. In particular, the amount of heat and work required to separate a mixture via a horizontally oriented distillation device according to the present invention is significantly lower than the heat and work required for conventional distillation. This can be at least partially explained by the horizontal orientation of the device, the efficient heat exchange between second and/or the efficient heat transfer by making use of at least one closed fluid circuit which is configured for providing heat exchanging interaction within the reboiling section and within the condensing section. The heat exchanging interaction between the closed fluid circuit and the reboiling section can be described as the closed fluid circuit providing heat to at least part of the liquid fraction of the mixture to be distilled which is present in the reboiling section such that at least part of said liquid fraction vaporizes. This will typically result in a reduction of the temperature of the fluid in the closed fluid circuit. Due to vaporization of at least part of the liquid fraction of the mixture and the fluid connection between the reboiling section and the separation section, at least part of the obtained vapor will rise into the separation section. The heat exchanging interaction between the closed fluid circuit and the condensing section can be described as the closed fluid circuit extracting heat from at least part of the vapor fraction of the mixture to be distilled which is present in the condensing section such that at least part if said vapor will be condensed. This will typically result in an increase of the temperature of the fluid in the closed fluid circuit. Where it is described that in the condensing section at least part of the vapor fraction of the mixture is cooled such that at least part of said vapor fraction is condensed, it can also be said that heat is extracted from at least part of the vapor fraction of the mixture such that at least part of said vapor fraction is condensed. Due to the condensation of at least part of the vapor fraction of the mixture and the fluid connection between the condensing section and the separation section, at least part of the obtained liquid will flow into the separation section. The condensation section thereto basically forms an internal reflux flow. As a consequence, and due to the separation section being configured for providing vapor/liquid (gas/liquid) contact, the vaporized liquid from the reboiling section can come into (direct) contact with the condensed vapor from the condensing section resulting in contribution to obtaining the desired separation of the mixture. The light key, or distillate, is thus typically separated via cross flow operation of vapor and liquid fractions in the separation section. Further, the effective vapor/liquid contact in at least part of the separation section in both vertical and horizontal direction may also contribute to the thermal efficiency. When it is referred to substantially vertical, a deviation of maximum 10% is meant. The device according to the present invention enables operation at a relatively low liquid load. Typically, there is vapor/liquid contact within the separation section in the x-, y- and/or z-direction. The device according to the present invention typically has a longitudinal configuration, resulting in a relatively small width (in the z-direction) of a typical device according to the present invention.
At least one closed fluid circuit is in particular configured for providing heat exchanging interaction with at least a fraction of the mixture to be distilled within the reboiling section and within the condensing section. In particular, the fluid of the closed fluid circuit is configured for heat exchanging interaction with at least a fraction of the mixture to be distilled within the reboiling section and within the condensing section. Due to the heat exchanging interaction between the fluid of the closed fluid circuit the temperature of the fluid within the closed fluid circuit typically differs per specific location of the device. The closed fluid circuit in fact enables a reversible energy cycle. Typically, there is a circular fluid flow in at least one closed fluid circuit. The fluid of the closed fluid circuit preferably circulates continuously.
Basically, at least one closed fluid circuit acts as a circular fluid flow channel. The use of the closed fluid circuit is also beneficial from energic point of view but also from economic point of view as significantly lower costs for heating and cooling compared to conventional distillation systems can be applied. This can also at least partially be explained due to the fact that the use of an external reflux can be omitted for the device according to the present invention. However, it is possible 5 that the device according to the present invention comprises at least one external reflux and/or at least one bypass. There is generally no direct contact between the fluid of the closed fluid circuit and the mixture to be distilled. The device according to the present invention can typically be operated as a balance system.
The device according to the present invention typically comprises at least one vapor outlet and/or at least one liquid outlet. The vapor outlet is typically present at or near the condensing section. It is for example possible that the liquid outlet is positioned at a position substantially before at least part of the vapor fraction is internally condensed. Preferably, at least one vapor outlet is present at an outer end and/or upper end of the housing. At least one liquid outlet is typically present at the reboiling section. Possibly, the device comprises a plurality of liquid outlets. The separation of the heavy key takes typically place in the reboiling section by evaporation in discrete stages. The vapor outlet can for example also be referred to as top outlet and/or the liquid outlet can be referred to as bottom outlet. Where the term vapor is used, also the term gas could be used and vice versa.
The feed mixture can for example be a liquid mixture and/or a gas mixture. The (feed) mixture may also comprises a vapor fraction and/or a liquid fraction. The mixture is typically a binary mixture. However, the mixture can also be a multicomponent mixture. The housing can also be referred to as a framework. The device according to the present invention is typically configured for industrial operation. The mixture is preferably entered (or introduced) in the reboiling section.
The mixture may for example be entered at bubbling point. A benzene/toluene mixture is a non-limiting example of a possible mixture which could be separated by making use of a device according to the present invention. It is conceivable that the mixture is supplied to the distillation device via multiple inlets.
The device according to the present invention can for example be operated at total reflux and/or at regular operation. The device for distillation can also be referred to as (horizontally oriented) distillation column. The reboiling section can also be referred to as reboiler section. The device is typically is operated under atmospheric pressure, or under relatively low pressures. However, the device may also be configured for operation under vacuum and/or under (high) pressure. The latter may for example be interesting when distilling cryogenic fluids.
The separation section is at least partially enclosed between the reboiling section and the condensing section, and wherein the separation section is in fluid connection with both the reboiling section and the condensing section. It is for example possible that the separation section is connected to the reboiling section via at least one support grid and/or that the separation section is connected to the condensing section via at least one distributor grid. Hence, the support grid and/or distributor grid may at least partially enable and/or enhance the fluid connection between the separation section and respectively the reboiling section and/or the condensing section. In a possible embodiment, the device comprises at least one support grid which is preferably configured for supporting at least part of the packing(s), if applied, of the separation section. Said support grid is typically substantially positioned between the reboiling section and the separation section. It is for example imaginable that at least one structured packing which is in particular configured for enabling substantially vertically oriented fluid flow is provided on at least part of the support grid. The support grid is typically at least partially permeable to fluids, in particular to vapour. The support grid may provide a protective function for the reboiling section and/or the separation section. The support grid may also provide a protective function for part of the closed fluid circuit. It is imaginable that at least part of the support grid comprising a step and/or offset over the length, which is preferably substantially located at or near at least one inlet.
It is also conceivable that the device comprises at least one distributor grid configured for distributing at least part of the liquid fraction present in the condensing section towards the separation section. The distributor grid is in particular configured to distribute at least part of the liquid which is condensed in the condenser section. The distributor grid should preferably also be configured to let vapor pass through. The distributor grid may further provide a protective function for the condensing section, closed fluid circuit and/or the separation section. The distributor grid is typically configured for liquid distribution. The distributor grid may in particular be configured for providing a substantially equal spread of condensed liquid from the condensing section which is to be distributed to the separation section. The distributor grid irrigate the separation section. The distributor grid may comprise multiple grid elements configured for distributing fluid, wherein the spacing of at least some grid elements is preferably below 500 mm, more preferably below 350, even more preferably below 200 mm. A non-limiting preferred embodiment of the distributor grid comprises multiple grid elements having a spacing of substantially 50 mm to 100 mm. If applied, the distributor grid and/or the support grid are positioned within the housing. The distributor grid and/or the support grid preferably extend substantially over the entire length and/or width of the housing. The grid elements are typically oriented in a direction which is substantially perpendicular to the longitudinal direction of the housing, in particular the z-direction. The distributor grid may for example comprise a plurality of substantially parallel positioned grid elements. It is preferred if at least one, and preferably all grid element(s) extend over substantially the entire width of the housing. It is also conceivable that at least one grid element is formed by a baffle.
In a further preferred embodiment of the device according to the present invention, at least part of the reboiling section is configured for fractional vaporization. The reboiling section may for example be divided in a liquid fraction and a vapor fraction. For such embodiment, typically, the bottom region of the reboiling section will comprise a liquid fraction whereas an upper region of the reboiling section will comprise a vapor fraction. The reboiling section may for example comprises at least one bottom region configured for receiving and/or comprising a liquid fraction and at least one upper region configured for receiving and/or comprising a vapor fraction.
It is a further preferred embodiment conceivable that the device, and in particular the reboiling section and/or the separation section, comprises multiple inlets, which inlets are in particular configured for feeding a mixture to be distilled to the device.
The multiple inlets may for example be vertically oriented with respect to another. It is also conceivable that the multiple inlets have an inclined orientation. It is conceivable that at least one inlet is located in the bottom region of the reboiling section in order to feed a mixture to the liquid fraction and/or wherein at least one inlet is located in the upper region of the reboiling section in order to feed a mixture to the vapor fraction. Preferably, the upper region of the reboiling section is provided with multiple inlets. It is also imaginable that the separation section comprises multiple inlets. The presence of multiple feed inlets may also positively contribute to the thermodynamic and/or thermal efficiency due to a lower vaporisation rate in the liquid phase of the reboiling section. The presence of multiple inlets further enables to supply mixtures with different feed temperatures.
Such preferred embodiment may reduce the required cross sectional area and such embodiment may also positively contribute to the thermal efficiency of the distillation device. It is also conceivable that at least part of the condensing section is configured for fractional condensation. In yet a further embodiment, substantially the entire condensing section may be configured for fractional condensation. The device can be configured to operate in split flow and/or the device may be configured for distilling a mixture in a single vaporization-condensation cycle.
However, the device according to the present invention can also be configured to separate the mixture to be distilled by multiple (repeated) vaporization- condensation cycles. It is imaginable that the device comprises multiple inlets, in particular multiple vapor inlets, wherein at least part of the inlets is distributed over the height of the device. At least two of the (vapor) inlets can for example be present in the separation sections.
In a preferred embodiment, the separation section comprises at least two different types of packings, wherein at least one packing is a structured packing which is in particular configured for enabling substantially vertically oriented fluid flow. It is also conceivable that the separation section comprises at least two different types of packings, preferably two different types of structured packings. At least one further packing, in particular at least one further structured packing, may be configured for enabling vertically and/or horizontally oriented fluid flow.
The device according to the present invention, and in particular the housing thereof, comprises at least one stripping section, at least one feeding section and at least one rectifying section. Said at least one stripping section, at least one feeding section and at least one rectifying section are in particular adjacently defined such that each of the stripping section, feeding section and rectifying section overlaps with the reboiling section, the separation section and the condensing section.
Hence, the at least one stripping section, at least one feeding section and at least one rectifying section are in particular adjacently defined seen from a horizontal orientation. In relation to this, the reboiling section, the separation section and the condensing section are adjacently defined seen from a vertical orientation. The feeding section represents in particular the section between the feed point vertical and the condenser vertical both identified by the isotherm of the feed composition.
The feeding section can also be referred to as middle section. Preferably, at least part of the separation section which overlaps with the feeding section comprises at least one structured packing which is in particular configured for enabling substantially vertically oriented fluid flow. This embodiment will have a positive influence on the feed composition, and in particular on the isotherm of the feed composition eventually resulting in higher obtainable concentrations for the light key. At least part of the feeding section is configured to operate close to total reflux or at total reflux. It is also imaginable that at least one structured packing is configured to enable operation close to total reflux or at total reflux. The stripping section and/or the rectifying section are typically provided with an internal split flow cycle. Their duty is mainly defined by the a-value. The condensing part of the cycle has to balance the vaporisation part. At least one split flow cycle, and preferably each split flow cycle can be integrated with the overall cycle. This can be beneficial for the performance of the separation section which overlaps with the feeding section.
It is conceivable that a lower part of the separation section which overlaps with the feeding section comprises at least one structured packing which is in particular configured for enabling substantially vertically oriented fluid flow and wherein a further part of the separation section comprises at least one further type of packing, in particular at least one further type of structured packing. The further type of packing can for example be configured for enabling substantially vertically and/or horizontally oriented fluid flow. In a possible embodiment, a lower part of the separation section which overlaps with the feeding section comprises at least one first type of structured packing which is in particular configured for enabling substantially vertically oriented fluid flow and wherein an upper part of the separation section which overlaps with the feeding section comprises at least one further type of structured packing. It is imaginable that a lower part of the separation section which overlaps with the stripping section, the feeding section and/or the rectifying section comprises at least one structured packing which is in particular configured for enabling substantially vertically oriented fluid flow. When it is referred to an upper part and a lower part of the separation section, it is imaginable that the lower part is defined by a height of at most 60% of the total height of the separation section, preferably at most 40% more preferably at most 30% in particular calculated from the support grid, if applied. It is also imaginable that the lower part of the separation section is defined by a height in the range of between 0 and 20% or 25% of the total height of the separation section, in particular calculated from the support grid, if applied. At least part of the separation section which overlaps with the stripping section and/or rectifying section may also comprise a further type of structured packed, for example the same as present in an upper part of the separation section which overlaps with the feeding section. It is also conceivable that at least part of the separation section which overlaps with the stripping section and/or rectifying section comprises at least one further type of structured packing.
The device according to the present invention comprises at least one closed fluid circuit. In a preferred embodiment, the device according to the invention comprises at least two closed fluid circuits, wherein each closed fluid circuit is configured for providing heat exchanging interaction with at least a fraction of the mixture to be distilled at least within the reboiling section and within the condensing section. The presence of a plurality of closed fluid circuits may be beneficial for the heat exchanging capacity of the closed fluid circuits, and thus for the efficiency of the device as such. It is for example imaginable that at least one closed fluid circuit is substantially located in the stripping section and that at least one further closed fluid circuit is substantially located in the rectifying section. It is for example also imaginable that at least one closed fluid circuit is substantially located in the stripping section and/or the feeding section and that at least one further closed fluid circuit is substantially located in the rectifying section and/or the feeding section.
Each closed fluid circuit may overlap with the feeding section. Preferably, at least one closed fluid circuit is received within the housing of the device. However, it is also possible that at least part of at least one closed fluid circuit is positioned outside the housing. It is also conceivable that the closed fluid circuits comprises a plurality of ducts. Such embodiment may also enhance the efficiency of the device.
Itis for example conceivable that at least one closed fluid circuits comprises a plurality ducts which are substantially parallel oriented with respect to each other. It is also conceivable that the closed fluid circuit comprises at least one manifold, or possibly multiple manifolds. At least one manifold may be configured to connect a plurality of ducts of the closed fluid circuit which are present in the reboiling section and/or the condensing section to a combined (parallel oriented} connection channel. In case multiple closed fluid circuits are applied, it is imaginable that at least one closed fluid circuit, and preferably each closed fluid circuit, comprises a plurality of mutually connected ducts. At least two ducts may be positioned substantially parallel. At least one closed fluid circuit may also comprises at least one bypass duct which is preferably configured for bypassing at least part of the fluid in the closed fluid circuit. The bypass duct may act as reflux. Preferably, the at least one bypass duct is positioned upstream of the inlet(s). At least one bypass duct is preferably configured for providing an extra cooling effort for the condensing section. It is conceivable that the closed fluid circuit comprises multiple bypass ducts. It is also conceivable that in case the device comprises a plurality of closed fluid circuits, preferably each closed fluid circuit comprises a bypass duct. At least part of at least one closed fluid circuit can be positioned inside the housing. More preferably, at least part of at least one closed fluid circuit is positioned inside the reboiling section and/or at least part of at least one closed fluid circuit is positioned inside the condenser section. In this manner, the heat exchanging interaction between the fluid of the closed fluid circuit and the mixture to be distilled can be enabled in a relatively easy manner and/or can be improved. Preferably at least one closed fluid circuit is positioned such that it does not (negatively) affect the vapor/liquid contact in the separation section. Hence, at least one closed fluid circuit may be positioned at a predetermined distance from the separation section.
It is also possible that at least one closed fluid circuit is substantially entirely positioned inside the housing. In this way, the housing may provide a protective function for the closed fluid circuit(s).
Preferably, at least one inlet of the device is located in the reboiling section which overlaps with the feeding section. For example in an upper part of the reboiling section which is adjacent to the separation section. At least one inlet is located in the bottom region of the reboiling section in order to feed a mixture to the liquid fraction and/or at least one inlet is located in the upper region of the reboiling section in order to feed a mixture to the vapor fraction. It is possible that the reboiling section comprises multiple inlets, which inlets are in particular configured for feeding a mixture to be distilled to the device. The multiple inlets may for example be parallel oriented with respect to another. It is also conceivable that the multiple inlets have an inclined orientation. It is conceivable that at least one inlet is located in the bottom region of the reboiling section in order to feed a mixture to the liquid fraction and/or wherein at least one inlet is located in the upper region of the reboiling section in order to feed a mixture to the vapor fraction. Preferably, the upper region of the reboiling section is provided with multiple inlets. The presence of multiple feed inlets may also positively contribute to the thermodynamic and/or thermal efficiency due to a lower vaporisation rate in the liquid phase of the reboiling section. The presence of multiple inlets further enables to supply mixtures with different feed temperatures. Such preferred embodiment may reduce the required cross sectional area and such embodiment may also positively contribute to the thermal efficiency of the distillation device. It is also conceivable that at least part of the condensing section is configured for fractional condensation. In yet a further embodiment, substantially the entire condensing section may be configured for fractional condensation. The device can be configured to operate in split flow and/or the device may be configured for distilling a mixture in a single vaporization- condensation cycle. However, the device according to the present invention can also be configured to separate the mixture to be distilled by multiple (repeated) vaporization-condensation cycles.
The separation section typically comprises at least one type of structured packing and preferably at least two types of structured packings. A non-limiting example is a high density structured packing. At least one structured packing may for example be a lamella-type packing. The desired cross sectional area in order to obtain a desired vapor flow can be defined by the y- and z-direction of the (packing of) the separation section, i.e. the height and width. In particular, there can be a horizontally oriented vapor flow in the condensing section, the separation section and/or the reboiling section. A vertically oriented vapor flow is desired in at least part of the separation section, in particular which overlaps with the feeding section.
For the present invention, the required cross sectional area is smaller compared to conventional distillation where the cross sectional area is typically defined by the reflux ratio and distillate. However, this is also dependent of the relatively volatility (a) of the mixture which is to be separated. In practice, the required cross sectional area is expected to be larger in case the relatively volatility is higher than 2.5. The desired cross sectional area may also be at least partially dependent of the type of packing applied. The design parameters for distillation according to the present invention provide flexibility in design for, for example, a relatively low pressure drop of vapor flow in the x-direction. A low pressure drop can be favourable for its impact on the hydraulic gradient. Another reason for a low vapor velocity in the x-direction is necessary for efficiency in separation due to the mixing with the vapor flow of the internal reflux. Although pressure drop has an increasing effect on the temperature in the lower area of the device it may contribute positively on the amplification factor. The amplification factor can be described by the temperature differential of the low key (LK) and the heavy key (HK) divided by the (pinching) temperature differential of the heater. Where it is referred to the lower area of the device, it is in particular referred to the area where the temperature is relatively high or at highest.
The area may for example be defined by (the lower part of) the condensing section, separation section and/or the reboiling section, wherein the temperature typically increases in longitudinal direction. This may be of relevance for the distillation of mixtures having a close boiling points (for example alpha <1.1) and/or for operating under vacuum conditions. The cross sectional area required for the internal reflux can be defined by the x- and z-direction. Non-limiting examples of packings which could be used for the separation section are a Rombopak packing and/or modified wire mesh. At least one structured packing configured for enabling substantially vertically oriented fluid flow preferably comprises at least one modified wire mesh.
In addition to this, it is also conceivable that at least one random packing is used.
Hence, at least part of the separation section may comprise at least one random packing. At least one packing can also be a gauze packing. Gauze packings are known for their high separation efficiency. At least one packing can for example be a strip type of packing and/or a lamella type of packing. At least one packing can also be a high density packing. At least one structured packing can comprise a plurality of channels. Preferably, the diameter of the channels of at least one structured packing are smaller than 10 cm, preferably smaller than 7 cm and/or larger than 2 cm, preferably larger than 4 cm. At least part of the diameter of the channels of at least one structured packing is preferably about 5 cm. At least one packing preferably has a pressure drop per theoretical stage in the range of 0.1 to 0.5 mbar. Preferably, at least one packing comprises metal. It is also conceivable that at least one packing is made of metal.
The separation section is typically at least partially enclosed between the reboiling section and the condensing section, and the separation section is preferably in fluid connection with both the reboiling section and the condensing section. It is for example possible that the separation section is connected to the reboiling section via at least one support grid and/or that the separation section is connected to the condensing section via at least one distributor grid. Hence, the support grid and/or distributor grid may at least partially enable and/or enhance the fluid connection between the separation section and respectively the reboiling section and/or the condensing section. The device may thus comprise at least one support grid located between the reboiling section and the separation section and/or at least one distributor grid configured for distributing at least part of the liquid fraction present in the condensing section towards the separation section. The support grid may also comprise at least one support packing. It is for example possible that the separation section is connected to the reboiling section via at least one support grid and/or that the separation section is connected to the condensing section via at least one distributor grid. In a possible embodiment, the device comprises at least one support grid which is preferably configured for supporting at least part of the packing, if applied, of the separation section. Said support grid is typically substantially positioned between the reboiling section and the separation section.
The support grid is typically at least partially permeable to fluids, in particular to vapour. The support grid may provide a protective function for the reboiling section and/or the separation section. The support grid may also provide a protective function for part of the closed fluid circuit. It is also conceivable that the device comprises at least one distributor grid configured for distributing at least part of the liquid fraction present in the condensing section towards the separation section.
The distributor grid is in particular configured to distribute at least part of the liquid which is condensed in the condenser section. The distributor grid should preferably also be configured to let vapor pass through. The distributor grid may further provide a protective function for the condensing section, closed fluid circuit and/or the separation section. The distributor grid is typically configured for liquid distribution. The distributor grid may in particular be configured for providing a substantially equal spread of condensed liquid from the condensing section which is to be distributed to the separation section. The distributor grid irrigate the separation section. The distributor grid may comprise multiple grid elements configured for distributing fluid, wherein the spacing of at least some grid elements is preferably below 500 mm, more preferably below 350, even more preferably below 200 mm. A non-limiting preferred embodiment of the distributor grid comprises multiple grid elements having a spacing of substantially 50 to 100 mm. If applied, the distributor grid and/or the support grid are positioned within the housing. The distributor grid and/or the support grid preferably extend substantially over the entire length and/or width of the housing. The grid elements are typically oriented in a direction which is substantially perpendicular to the longitudinal direction of the housing, in particular the z-direction. The distributor grid may for example comprise a plurality of substantially parallel positioned grid elements. It is preferred if at least one, and preferably all grid element(s) extend over substantially the entire width of the housing. It is also conceivable that at least one grid element is formed by a baffle.
Atleast part of the separation section focusses on vertically oriented fluid flow.
However, preferably, at least part of the separation section is configured such that at least vapor can flow through the separation section in both horizontal and vertical direction. More preferably, at least part of the separation section is configured such that both vapor and liquid can flow (or pass) through the separation section in both horizontal and vertical direction. This embodiment can benefit of a relatively large vapor/liquid contact surface, which is desired for the distillation process. Preferably, in at least part of the separation section the fraction of vapor flowing in horizontal direction is larger than the fraction of vapor flowing in vertical direction whilst in a further part the fraction of vapor flowing in vertical direction is larger than the fraction of vapor flowing in horizontal direction .
In a further beneficial embodiment, the device comprises at least one cooler configured for cooling at least one closed fluid circuit, in particular the fluid of at least one closed fluid circuit, preferably wherein the cooler is positioned substantially prior to the condensing section. In this embodiment, the cooler can contribute to obtaining a desired temperature for (fluid of) the closed fluid circuit in order to enable condensation in the condensation section in a more controlled manner. The cooler may be positioned at least partially inside the housing and/or at least partially outside the housing. The cooler is preferably configured to provide cooling of the closed fluid circuit, in particular the fluid thereof to a predetermined temperature. The cooler may for example be configured to provide cooling up to several dozen degrees Celsius. The temperature to be reached may for example be in the range of -200 to 300 degrees Celsius, preferably in the range of-100 to 200 degrees Celsius. However, typically, due to the efficiency of the closed fluid circuit, in practice, the cooler provides a cooling effect for the fluid of the closed fluid circuit of only a few degrees Celsius, for example in the range of 1 to 5 degrees Celsius, preferably in the range of 1 to 3 degrees Celsius. This can be explained by energy recovery of the integrated heating system achieved by the use of a closed fluid circuit. The cooler may be configured to overcome the temperature difference of the fluid based upon pinch analysis. The cooler can be positioned in the region of a pinch point of the closed fluid circuit, in particular before the fluid enters the condensing section.
The device may also comprise at least one heater configured for heating at least one closed fluid circuit, in particular the fluid of at least one closed fluid circuit, preferably wherein the heater is positioned substantially prior to the reboiling section. In this embodiment, the heater can contribute to obtaining a desired temperature for (fluid of) the closed fluid circuit in order to enable vaporization in the reboiling section in a more controlled manner. The heater may be positioned at least partially inside the housing and/or at least partially outside the housing. The heater is preferably configured to provide heating of at least one closed fluid circuit, in particular the fluid thereof to a predetermined temperature. The heater may for example be configured to provide heater up to several dozen degrees Celsius. The temperature to be reached may for example be in the range of -200 to 300 degrees
Celsius, preferably in the range of-100 to 200 degrees Celsius. However, typically, due to the (energetic) efficiency of the closed fluid circuit, in practice, the heater provides a heating effect to the fluid of the closed fluid circuit of only a few degrees
Celsius, for example in the range of substantially 1 to 5 degrees Celsius, preferably in the range of 1 to 3 degrees Celsius. The heater may be configured to overcome the temperature difference of the fluid based upon pinch analysis. The heater can be positioned in the region of a pinch point of the closed fluid circuit, in particular before the fluid enters the reboiling section. A substantial amplification of the internal reflux can be achieved by pinching temperatures of the heater.
The device may further comprise at least one expansion vessel. In particular, at least one closed fluid circuit may be connected with at least one expansion vessel.
Such expansion vessel is typically configured to protect the closed fluid circuit from excessive pressure. The expansion vessel can be any known, suitable expansion vessel. Typically, if applied, the expansion vessel is positioned in a region of the closed fluid circuit wherein the temperature is relatively low.
Abovementioned optional heater and cooler are in particular configured for obtaining a desired temperature in or for the closed fluid circuit. The heater and cooling can be any conventional heater or cooling useable for industrial application.
The fluid in the closed fluid circuit is preferably substantially liquid and/or substantially in vapor phase. Non-limiting examples of fluids to be used in the closed fluid circuit are water, hydrogen and/or helium.
Itis also possible that the device comprises at least one secondary heater configured for heating at least part of the liquid fraction in the reboiling section.
More in particular, at least one secondary heater may be configured for the provision of distillate. At least one secondary heater is preferably positioned between at least one inlet and at least one liquid outlet. If applied, at least one secondary heater is typically positioned within the liquid phase of the mixture present in the reboiling section. Said secondary heater is typically configured to enhance the vaporization of liquid fraction in the reboiling section. At least one secondary heater may for example be a heat exchanger.
Itis further possible that the device comprises at least one secondary heat exchanger, for example a secondary cooler, configured for cooling at least part of the vapor fraction in the condensing section. The presence of at least one of said secondary heat exchanger may for example be beneficial in case the mixture to be distilled is a vapor mixture. If applied, at least one secondary heat exchanger is typically positioned within the vapor phase of the mixture present in the condensing section and configured to enhance the condensation of the vapor fraction in the condensing section. The secondary heat exchanger may also be position in the condensing section between an inlet for feeding a vapor mixture to be distilled to the device and the vapor outlet. It is also conceivable that the device according to the present invention comprises both at least one secondary heat exchanger present in the reboiling section, and at least one secondary heat exchanger present in the condensing section.
The reboiling section and/or the condensing section may be provided with at least one baffle and preferably a plurality baffles. The presence of at least one baffle in the reboiling section may prevent back mixing of at least part of the liquid fraction in the reboiling section. Back mixing is undesirable as this may negatively affect the distillation process. Preferably, at least one baffle is present in the region of the inlet. At least one baffle can comprise a wire mesh. At least one baffle, or possibly multiple baffles, can be present in the reboiling section up to height of the closed fluid circuit(s). It is also conceivable that at least one baffle, or possibly multiple baffles, are present in the reboiling section wherein the baffle(s) overlap with the closed fluid circuit(s). Further, the presence of at least one baffle in the reboiling section may also enable obtaining of discrete separation stages. At least one baffle in the condensing section may prevent condensed liquid affected the output of the device near the vapor outlet. It is conceivable that at least one baffle is connected to the distributor grid, if applied. At least one baffle may also form integral part of the distributor grid. It is also conceivable that at least one baffle is connected to the support grid, if applied. At least one baffle may also form integral part of the support grid. It is also conceivable that at least one baffle is present in the vapor disengaging space of the reboiling section, in particular located between the support grid and an upper part of the closed fluid circuit, to enable discrete separation stages. If multiple baffles are applied, either in the reboiling section and/or the condensing section, adjacent baffles are typically positioned at a spacing inthe range of 100 and 500 mm. The spacing is preferably below 400m, more preferably below 300 mm and even more preferably below 200 mm.
It is also conceivable that at least part of the housing and/or at least part of the reboiling section is positioned under a predetermined angle. The housing and/or the reboiling section may for example be slightly tilted, in particular with respect to the substantially horizontal ground surface. The predetermined angle may for example be between 0.01% and 10%, preferably between 0.01% and 0.1%. An embodiment having at least part of the housing and/or at least part of the reboiling section is positioned under a predetermined angle may contribute to more controlled flow of at least part of the liquid fraction in the reboiling section. It may further be used to at least partially drain the reboiling section and/or for a positive effect on the liquid level in the reboiling section (hydraulic gradient) and/or to enhance liquid collection and redistribution of the liquid in the reboiling section, in particular in the support grid, if applied. A (liquid) level controller may also be present in the reboiling section. It is also imaginable that there is a level difference over the length of the housing, and in particular over the length and/or in the bottom of the bottom section. This is in particular beneficial for relatively elongated housings, having a relatively large (horizontal) length which can be explained by the hydraulic gradient. Applying a level difference over the length of the housing can positively contribute to obtaining a substantially vertical fluid flow, preferably in the separation section. At least part of the support grid, if applied, can be adapted based upon the level difference over the length of the housing. It is for example imaginable that at least part of the support grid is configured to achieve overflow in at least part of the bottom section. At least part of the support grid can have a level difference. The level difference of the support grid and/or of the housing can have a slope, step and/or offset over the length, which is preferably substantially located at or near at least one inlet.
At least part of the liquid fraction in the reboiling section should typically flow from a lower temperature region (i.e. the light key region) to the higher temperature region (i.e. the high key region). Practically, it can also be said that the liquid has to flow from a lower pressure to a higher one. In order to minimise the difference in liquid level is preferred to avoid impact on the efficiency of the reboiling section, an example thereof is back mixing. In general, it is preferred that the device according tothe invention operates using relatively low liquid velocities.
The housing of the device is in a preferred embodiment substantially horizontally oriented. Advantages of a substantially horizontally oriented housing compared to a vertically oriented distillation column are for example easier construction, operation, and/or maintenance. It is for example possible that the length of the housing (x- direction) is larger than the height (y-direction) and the width (z-direction) of said housing. In a further preferred embodiment, the length of the housing is at least two times the height of the housing. It is also conceivable that the length of the housing is at least two and preferably at least 2.5 times the height of the housing, or preferably the length of the housing is substantially 3 times the height of the housing. However, it is also conceivable that the housing has a substantially vertically orientation. Preferably, the housing is substantially longitudinal.
The length of the housing can for example be at least 5 meter, in particular at least 7 meter, more in particular at least 10 meter. Typically, the length of the housing is at least 20 meter, preferably at least 30 meter, and more preferably at least 40 meter. Further non-limiting examples are the length of the housing being substantially between 5 and 100 meter, for example between 6 and 90 meter or between 10 and 70 meter. The housing may for example be in the range of 50 to 60 meter. The width of the housing is preferably less than 5 meter, preferably less than 4 meter, more preferably less than 3 meter. It is also conceivable that the width of the housing is between 2 and 4 meters. A relatively small width of the housing contributes to the longitudinal character of the device, which may have above mentioned advantages of easier construction, operation and/or maintenance in particular if applied in horizontal orientation.
In a preferred embodiment, the device comprises at least one pump for controlling fluid flow in the closed fluid circuit. Hence, the pump can be configured for pumping the fluid within the closed fluid circuit, preferably in a controlled manner. The pump is preferably configured to provide a circulating fluid flow within the closed fluid circuit. The pump may for example be configured to control the fluid flow in anti- clockwise direction. However, it is also conceivable that the fluid is pumped in clockwise direction. The pump may be configured to control the fluid counter currently and/or co-currently with respect to the mixture to be distilled. Typically, the fluid of the closed fluid circuit is controlled such that the fluid flow is in the reboiling section guided substantially a forward direction seen from inlet to at least one vapor outlet. This means that the fluid in the condensing section is guided substantially in a forward direction seen from the vapor outlet towards the inlet. The fluid of the closed fluid circuit flows continuously through the reboiling section and condensing section, wherein the temperature is typically relatively high when it enters the reboiling section and is substantially lowered when the fluid leaves the reboiling section. The opposite applies for the condensing section, where the temperature of the fluid relatively low when it enters the condensing section and wherein said temperature is increased over the length (or distance travelled) of the condensing section.
The invention also relates to a system comprising multiple devices according to the present invention. The devices can for example be configured to be connected and/or operated in series. Such system may for example be configured for desalination of (sea)water.
The invention also relates to the use of a device according to the present invention.
The invention further relates to a housing for use in a device according to the present invention. The invention also related to the use of a closed fluid circuit as described for the present invention for use in distillation processes.
The invention also relates to a method for distillation of mixtures, preferably by making use of a device according to the present invention, comprising a substantially vertically oriented fluid flow in at least part of the separation section. In a preferred embodiment, heating at least part of the liquid fraction of the mixture to be distilled such that at least part of said liquid fraction vaporizes is realized via heat exchanging interaction between said liquid fraction and at least one closed fluid circuit, and wherein cooling at least part of the vapor fraction of said mixture is cooled such that at least part of said vapor fraction is condensed via heat exchanging interaction between said vapor fractions and said closed fluid circuit.
The method according to the present invention can also be referred to as reversible separation.
The method according to the present invention, and use of the device according to the present invention, enables that a higher efficiency can be obtained for the same heat requirement and a lower requirement for the amount of thermodynamic work, when compared to conventional distillation. This can be at least partially explained by the effect of the entropy of mixing. The effect of the achieved vertical flow which is obtained by the at least one structured packing which is configured for enabling substantially vertically oriented fluid flow versus a mixed flow in horizontal and vertical orientation for conventional distillation. The operational difference between the method for distillation according to the present invention, or reversive separation, and conventional distillation can at least partially be explained by vertical flow in at least part of the separation section versus mixed flow (i.e. horizontal and vertical flow). Further efficiency of the method according to the invention can for example be obtained when the feed composition is adjusted such that a relatively large vapor fraction is present. The distillation can for example performed at total reflux operation or close to total reflux.
The invention will be further elucidated by means of non-limiting exemplary embodiments illustrated in the following figure, in which: - figure 1 shows a schematic representation of a possible embodiment of a device according to the present invention; - figures 2a, 2b and 2c show the thermal and thermodynamical effect of the device according to the present invention compared to a conventional distillation device.
Within these figures, similar reference number refer to similar or equivalent technical features or elements.
Figure 1 shows a schematic representation of a possible embodiment of a device 100 according to the present invention. The figure shows a side view of the device 100. The device 100 is configured for distillation of mixtures, for example liquid and/or vapor mixtures. In the shown embodiment, the device 100 comprises a inlet 102 for feeding a mixture to be distilled to the device 100 and a housing 101. The housing 101 comprises a reboiling section 103, a condensing section 104 and a separation section 105. The device 100, and in particular the housing 101, comprises further a stripping section S, a feeding section F and a rectifying section
R. Each of the stripping section S, feeding section F and rectifying section R overlaps with the reboiling section 103, the separation section 105 and the condensing section 104. The separation sections 105 comprises at least one structured packing. In the shown embodiment, a lower part of the separation section 105 which overlaps with the feeding section F comprises at least one structured packing S1 which is in particular configured for enabling substantially vertically oriented fluid flow. This will have a positive influence on the feed composition, and in particular on the isotherm of the feed composition eventually resulting in higher obtainable concentrations for the light key. It can be seen in figure 1 that the slope of isotherm is influences by the structured packing S1. A further part of the separation section 105 comprises at least one further type of packing S2, S3 in particular at least one further type of structured packing. The reboiling section 103 is present at a lower region of the housing 101. Within the reboiling section 103, heat is providing to at least part of the liquid fraction of the mixture to be distilled such that at least part of said liquid fraction vaporizes.
The condensing section 104 is present at an upper region of the housing 101. Within the condensing section 104, at least part of the vapor fraction of the mixture is cooled such that at least part of said vapor fraction is condensed.
The separation section 105 is partially enclosed between the reboiling section 103 and the condensing section 104 and in fluid connection therewith.
The separation section 105 connects to the reboiling section 103 and condensing section 104 via respectively a support grid 106 and a distributor grid 107. The separation section 105 is configured for providing vapor/liquid contact between at least part of the vapor fraction and part of the liquid fraction of the mixture to be distilled.
The device 100 further comprises a vapor outlet 108 and a liquid outlet 109. The liquid outlet 109 is the heavy key outlet 109 and is provided in the reboiling section 103. The vapor outlet 108 is the light key outlet 108 and is provided in the condensing section 104. The shown embodiment of the device 100 comprises multiple closed fluid circuits 110 which are configured for providing heat exchanging interaction with at least a fraction of the mixture to be distilled within the reboiling section 103 and/or within the condensing section 104. At least one closed fluid circuit 110 circuit is located in the stripping section S and at least one closed fluid circuit 110 is located in the rectifying section R.
At least one closed fluid circuit 110 comprises at least one bypass duct configured for bypassing at least part of the fluid in the closed fluid circuit 110. In the shown embodiment, the device 100 has a substantially horizontal orientation.
In particular, the housing 101 is substantially horizontally oriented.
The device 100 comprises multiple pumps 111 for controlling fluid flow in the closed fluid circuit 110. Optionally, a cooler 113 is present in order to cool art of a closed fluid circuit 110, in particular the fluid of the closed fluid circuit 110. It conceivable that the housing 101 comprises a section configured for fractional condensation prior to the cooler 113. A heater 114 is present for heating a closed fluid circuit 110, in particular the fluid of the closed fluid circuit 110. It is conceivable that the housing 101 comprises a section configured for fractional vaporization prior to the heater 114. Secondary heaters 115 can be provided for heating at least part of the liquid fraction in the reboiling section 103. An external condenser 116 is present for condensing of at least part of the vapor fraction which is removed via at least one vapor outlet 108. The light key (LK) and heavy key (HK)
are indicated as well in the figure. The closed fluid circuit 110 can be provided with, optional, expansion vessels 119.
Figures 2a, 2b and 2c show the thermal and thermodynamical effect of the device according to the present invention compared to a conventional distillation device.
Figure 2a shows a vertically oriented distillation column configured for conventional distillation. Figure 2b shows a first example of a horizontally oriented device for distillation. Figure 2c shows a second example of a horizontally oriented device for distillation wherein at least part of the separation section comprises at least two different types of packings such that the fluid flow is influenced. Figures 2b and 2c show an example of reversible separation in distillation. The device as shown in figure 2c equals the device as shown in figure 1.
For the distillation column of figure 2a, the heat Q and the amount of work W required to separate the mixture are defined according to the following formulas:
Qk” = Qp + Qrr +05 + Qh and
Wep = 73 eK)
For example 1 of figure 2b, the heat Q and the amount of work W required to separate the mixture are defined according to the following formulas:
Q1 = Opi + Qrri and
Ww, = |p - 2) 0,
BLF(AVG)
For example 2 of figure 2c, the heat Q and the amount of work W required to separate the mixture are defined according to the following formulas:
Q2 = Qp2 + YQrr2 and
TsTe AVG) T Tp
We = | Fo Je.
In these formulas, W= work in J, Q is heat requirement in kW, T= temperature in degrees Celsius, and factor y=0.1.
The distillation device as shown in figure 2c benefits of an improved thermal efficiency due to the separation section comprising at least two different types of packings, wherein at least one packing is a structured packing which is in particular configured for enabling substantially vertically oriented fluid flow.
Calculations results in the following results for the thermal efficiency based on the required heat Q:
QR > >
For the thermodynamic efficiency, the required amount of work is:
Wp > W>W,
It follows from the formulas that the amount of heat Q and work W required to separate the mixture via a horizontally oriented distillation column (examples 1 and 2 corresponding to figures 2b and 2c) is lower than the heat Q and work W required for conventional distillation (prior art, figure 2a). This results in a higher thermodynamic efficiency. In practice, the device of figure 2b would require a very higher number of trays which is undesirable. The separation can be further optimized by making use of a device according to the present invention, as it can be observed that the use of at least two different types of packings in the separation section results in a shift of the isotherm. This will have a positive influence on the feed composition, and in particular on the isotherm of the feed composition eventually resulting in higher obtainable concentrations for the light key. It can be seen in figure 2c that the slope of isotherm is shifted compared to the isotherm as shown in figure 2b.
It will be clear that the invention is not limited to the exemplary embodiments which are illustrated and described here, but that countless variants are possible within the framework of the attached claims, which will be obvious to the person skilled in the art. In this case, it is conceivable for different inventive concepts and/or technical measures of the above-described variant embodiments to be completely or partly combined without departing from the inventive idea described in the attached claims.
The verb 'comprise' and its conjugations as used in this patent document are understood to mean not only ‘comprise’, but to also include the expressions ‘contain’, ‘substantially contain’, ‘formed by' and conjugations thereof.
Claims (32)
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL2035399A NL2035399B1 (en) | 2023-07-17 | 2023-07-17 | Device and method for distillation |
| PCT/NL2024/050384 WO2025018881A1 (en) | 2023-07-17 | 2024-07-12 | Device and method for distillation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL2035399A NL2035399B1 (en) | 2023-07-17 | 2023-07-17 | Device and method for distillation |
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| NL2035399B1 true NL2035399B1 (en) | 2025-01-28 |
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| NL2035399A NL2035399B1 (en) | 2023-07-17 | 2023-07-17 | Device and method for distillation |
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| WO (1) | WO2025018881A1 (en) |
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- 2023-07-17 NL NL2035399A patent/NL2035399B1/en active
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| US4843828A (en) * | 1985-10-04 | 1989-07-04 | The Boc Group, Plc | Liquid-vapor contact method and apparatus |
| DE4431546A1 (en) * | 1994-09-05 | 1996-03-07 | Jakob Dr Ing Hois | Process and device for desalination of sea water |
| US5964986A (en) * | 1996-10-09 | 1999-10-12 | Sulzer Chemtech Ag | Distillation plant |
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|---|---|
| WO2025018881A1 (en) | 2025-01-23 |
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