Method for sustained thermal separation of multicomponent materials - Patents.com

Abstract

The present invention relates to a method for sustained thermal separation of a substance being delivered to a treatment chamber in a container. Besides the container, the apparatus comprises a heating device with an external heat source and a rotary mechanism with an external rotary drive. The heating device and the rotary drive are adapted to maintain the resulting operating temperature T op is the evaporation temperature T of at least one liquid that is part of the substance e The volume V near the inner surface of the container is equal to or higher than p are operated in a mutual manner so as to be acquired within.

Description

[Technical field]

[0001] The present invention is primarily directed to a method for sustained thermal separation of a multi-component material flowing into a treatment chamber.

[0002] The present invention particularly relates to a method, which is suitable for the utilization of waste heat as a major indirect energy contributor for the thermal separation of waste and by-products, the separation involving the removal of fluids from materials by heating. [Background technology]

[0003] A variety of substances, including both solid materials and vaporizable liquids, can be thermally separated by heating the substances to a temperature above the vaporization temperature of the liquid.

[0004] As a result of the heating, the liquid changes phase from liquid to gas phase, while the solid is dried. Equipment for such thermal separation processes is well known in the art and is commonly referred to as a "thermal desorption unit" (TDU) or dryer. During the thermal treatment, the liquid is usually condensed back to the liquid phase as a post-treatment or additional treatment step.

[0005] TDUs are used to treat many different materials that contain one or more evaporable liquids, such as waste and by-products from food production, municipal sludge, waste from refining processes or drilling, and a variety of other materials. The predominant thermal isolation techniques commercially available on the market today can be broadly divided into two categories. -Indirect heating thermal separation -Friction-based thermal isolation

[0006] Most existing TDU technologies are based on indirect heating: an external heat source heats the outer wall of the container, and the heat is transferred via the inner surface of the container onto the material to be heated.

[0007] The external heat source can in principle be anything capable of heating the substance to the required temperature to evaporate the relevant liquid in the substance inside the container. The most used heating sources are water steam, hot oil, flame, heated gas or exhaust, and electricity (cable, element, induction, etc.).

[0008] One example of an apparatus for drying materials using an indirect method is disclosed in patent publication GB1575576A. This publication particularly relates to the treatment of a mixture of wellbore drilling cuttings and drilling fluid to remove volatile materials from the drilling cuttings, and includes a heater for heating the cuttings in a heating chamber and vaporizing the volatile materials therein. Heating of the cuttings may involve an external electrical resistance element or may use a heat transfer fluid, which is in turn heated by an electrically energized auxiliary heat exchanger.

[0009] Other relevant publications disclosing relevant prior art indirect solutions for separating waste materials are US 5.375.343 A, which discloses an evaporator for drying sludge, and US 3.808.701 A, which discloses an apparatus for drying fluid materials.

[0010] The evaporator in US 5.375.343 essentially comprises a hollow cylindrical externally driven rotor equipped with vanes that extends the length of the evaporator. The device assumes gradual heating along the evaporator. Furthermore, the device in US 3.808.701 comprises a horizontally arranged cylindrical conduit and a rotor that rotates internally within the conduit. The rotor supports vane-like elements operatively associated with the inner wall of the conduit that serve to wipe, circulate, crush and scrape the flowing material.

[0011] All existing indirect (continuous) methods will have an internal transport mechanism where the mass will be slowly heated over time (and distance). The temperature will rise to approximately 100 degrees Celsius, which will take some time (and distance) since all the energy required for the evaporation of the water will therefore be transferred to the waste. If the material also contains liquids with higher evaporation temperatures, such as oil, most of such liquids will not evaporate prior to subsequent further heating of the material. In such situations, the internal transport mechanism is often 10-20 meters long and it may take up to 20 minutes before all the liquid in the waste is evaporated.

[0012] The main challenge of existing indirect methods is the heat transfer from the inside surface of the container into the material to be heated. From the start, the material or materials are "wet solids". The water, and possibly other liquids such as oil, are integral parts and are not "loose". The material will be influenced by gravity and will be located at or near the lower area (i.e., bottom) of the vessel / container. As the solids are heated, they will dry out and as a result the heat transfer rate will quickly decrease. The heat transfer rate from the steel to the liquid containing material will be higher initially, but the heat transfer will slowly reach a level equal to or similar to the heat transfer between the inner wall of the container and the dried solids in the material. Generally, for a typical drilling waste composition, i.e., oil, water, and mineral solids, a heat transfer rate of approximately 75 W / m2 in the indirect solution is required. 2 Achieving an average heat transfer better than K is regarded as difficult. One challenge relates to the fact that solids will build up an isolating layer on the heated surface, thereby reducing heat transfer efficiency. For protein containing solids, this is particularly challenging, since such solids have properties that make them highly affected by heat, leading to unnecessary degradation of potentially valuable solids.

[0013] Friction-based thermal separation, on the other hand, is based on a very different principle than indirect thermal separation, namely, the transfer of kinetic energy derived from a rotating drive to thermal energy (heat) by friction. In these friction-based processes, no internal surface of the material containing chamber is heated from the outside. Instead, in clear contrast to indirect solutions, the entire heat transfer surface, i.e., the solidified surface of all dried particles in the waste, is entirely located within the process chamber. This solidified surface area is very large compared to the corresponding heat transfer surface of the indirect solution, thereby making the internal transport mechanism irrelevant.

[0014] Friction-based solutions rely entirely on rotational energy and therefore do not utilize residual heat sources or other external indirect heat sources.

[0015] Also, energy losses in friction-based solutions are usually significant: for example, when a diesel engine is used to generate the required rotational energy and / or electrical power that comes from a diesel generator, losses of around 2 / 3 are typical.

[0016] The following patent publications disclose relevant examples of known friction-based dryers:

[0017] No. 4,869,810 (A) discloses a method for separating underwater oil and other evaporable liquids from drilling muds, bleaching earth, sludge from oil tanks, oil shale, or the like, whereby the mud is evaporated at a lower temperature than with conventional evaporation due to the fact that the capillary forces binding the separate fragments in the pores of the mud are destroyed in the friction evaporator.

[0018] WO02092187 (A1) discloses a method for separating oil, water, and other components that can be evaporated from an oil-containing material by evaporation. Evaporation is achieved below the atmospheric boiling point of the component due to the use of a gas phase established by the evaporation of the second component. A means for drying a fluid-containing material is also included, comprising a treatment chamber and a rotor mounted within the treatment chamber. The rotor comprises several fixed rotor arms that cannot swing, and the inner surface of the treatment chamber is smooth.

[0019] The operation of all known friction-based dryers relies on the extensive use of rotational energy, thus limiting the use of alternative energy sources such as surplus energy.

[0020] A common drawback with any of the known thermal techniques (both indirect and friction-based methods) is the consumption of large amounts of energy, both of which result in high operating and / or investment costs.

[0021] For that reason, cheaper, less efficient solutions such as landfilling or incineration are often chosen. These cheaper solutions are often problematic due to their environmental hazards and waste of potentially valuable resources.

[0022] In light of the above, it is an object of the present invention to provide a method that overcomes, or at least alleviates, one or more of the aforementioned problems associated with the use of prior art solutions.

[0023] A particular object of the present invention is to provide a method which allows the use of smaller equipment.

[0024] It is another object of the present invention to provide a method which provides more efficient separation of multi-component materials fed into the apparatus.

[0025] It is yet another object of the present invention to provide a method which provides more efficient mixing of multi-component materials fed into the apparatus.

[0026] Yet another object of the present invention is to provide a method for generating more favorable energy consumption during drying by utilizing waste heat sources. Utilizing unused (overflow) waste heat / surplus heat can significantly reduce operational costs.

[0027] Additionally or alternatively, the present invention has the objective of providing a method that allows for the efficient utilization of other surplus energy sources, including components separated in the process, with calorific value, such as oil or dried biomass. Examples of such waste materials are waste oil, waste solvents, refuse-derived fuels, carpet and textile waste, plastic or mixed plastic waste, automobile shredder residues, and meat and bone meal (MBM).

[0028] Excess heat and / or heat generating components from the waste may be used for thermal separation on-site, for example on an oil drilling platform.

[0029] Additionally, excess heat and / or heat generating components from the waste can partially or completely substitute for other energy contributors.

[0030] Some existing solutions are capable of utilizing the surplus heat as the main energy supply for thermal isolation. However, these solutions have limited heat transfer capacity and would necessarily require large heating surfaces and long internal transport mechanisms. As a result, they are large with higher energy losses and the relatively larger heating surfaces need to be protected / insulated to both avoid heat losses and reduce hazards. Summary of the Invention [Means for solving the problem]

[0031] The present invention is set forth and characterized in the independent claims, while the dependent claims describe further characteristics of the invention.

[0032] In one aspect, the present invention relates to a method for thermally sustained separation of a material flowing into a treatment chamber, preferably through the use of a separation device.

[0033] The separation device has a length l c The present invention relates to a container having a container wall with an inner surface enclosing a treatment chamber of height H and width W, the containers each having at least one substance inlet, at least one first outlet for a non-vaporizable component, and at least one second outlet for a vaporizable component, the heating device being arranged outside the treatment chamber, e.g., at the outer surface and / or in the container wall, and the rotary mechanism being arranged to rotate the treatment chamber over the length l of the treatment chamber. c The rotary mechanism further comprises a rotatable shaft arranged within the treatment chamber, oriented along the L direction (hereinafter referred to as the L direction). The rotary mechanism further comprises a rotatable shaft arranged within the treatment chamber, oriented along the L direction (hereinafter referred to as the L direction), at a significant distance, preferably at a central axis C of the treatment chamber. TC and the inner wall, and fixed to the rotatable shaft so as to extend over at least 80%, and even more preferably at least 90%, of the linear distance between the md and axial length l md The mixing device may comprise a mixing device of at least one of the above-mentioned types. The radially outermost portion of the mixing device, for example up to 20% of the radial extent of the mixing device, or up to 10% of the radial extent of the mixing device, may include axial sets of radially separated mixing protrusions, the sets being axially offset with respect to each other. The mixing protrusions allow for intense mixing of at least a portion of the material, preferably all of the evaporated material, at the inner surface.

[0034] central axis C TC is defined as the axis oriented along the L direction and located midway between the average width W and average height H of the treatment chamber.

[0035] In one embodiment, the mixing protrusions may be in the form of rods that protrude radially from the outermost boundary of the remainder of the mixing device and are distributed with intervals along at least 80% of the length of the rotatable shaft.

[0036] In another embodiment, the protrusion extends continuously across the length of the mixing device parallel to the rotatable axis. The method comprises the following steps (in any sequence):

[0037] A. The minimum peripheral volume V of the treatment chamber that can be heated by use of a heating device to heat the inner surface and transmit thermal energy from the heating device through the inner surface by direct contact between the mixing device (including the mixing protrusions) and the inner surface. p a step of transferring onto the vapor cloud, if present, heat energy being transferred to the vapor cloud generated therein (see step D below); B. By use of a rotary drive operably fixed to the rotatable shaft, the rotary mechanism is rotated at a minimum peripheral rotational speed v of 5 meters per second, measured at the radially outer boundary of the mixing device (i.e., the radially outer boundary of the mixing protrusion). p,min The peripheral rotation speed v exceeds p Rotating until C. Using a feeding device, preferably an automatic feeding device, feeding the substance through at least one substance inlet into the treatment chamber, the substance being heated to a temperature at least one of the components above a vaporization temperature T e (e.g., below 200° C.), and D. - the input power of the heating device; - a flow of material into the treatment chamber, i.e. through at least one of the at least one material inlet; the input power of the rotary drive; an output flow of a non-vaporized portion of the substance discharged from the at least one first outlet; and At least one of the minimum peripheral volume V p The total heat transfer energy to at least a portion of the vaporization temperature T during operation e Operating temperature T exceeds op wherein the heating device adjusts the heating temperature to provide a minimum peripheral volume V p the amount of heat energy transferred in said portion constitutes more than 60%, preferably at least 65%, more preferably at least 70%, e.g. 75%, of the total transferred heat energy.

[0038] The total transferred heat energy combined with the intense mixing produces a vapor cloud that includes an evaporated portion, i.e., a mixture of components in a fluid state (gas or liquid), and a non-evaporated portion, such as a dry solid.

[0039] The result is the minimum peripheral volume V p , i.e., near instantaneous heating and evaporation on or near the interior surface.

[0040] The outermost radial portion of the mixing device preferably comprises a plurality of radially separated mixing protrusions.

[0041] Further, the plurality of radially separated mixing protrusions may be spaced apart from each other along the axial length l of the mixing device. md The number of mixing protrusions in each set is defined as the number of axially nearest mixing protrusions in a perfect circle around the rotatable shaft when viewed along the direction of the rotatable shaft at an axial position directly in front of the set. Also, the minimum peripheral rotation speed of the rotary mechanism v p,min is further defined as follows: v p,min =C(d md / # mp ) During the ceremony, C is a constant greater than or equal to 12π, # mpis the number of radially separated mixing lobes in each set.

[0042] d md [m] is the radial diameter of the mixing device (i.e. including the mixing protrusions).

[0043] The radially separated mixing protrusions may be aligned with a plurality of axial planes, for example having a radial offset from one another, all of which are aligned with the central axis C. TC It intersects with.

[0044] If the mixing protrusions in each set are in the form of radial rods, and these rods are not substantially axially displaced relative to one another, maximum mixing of the non-vaporized and vaporized portions of the substance at the inner surface occurs at or near one radial plane within the treatment chamber. In such a configuration, the mixing device comprises a plurality of such radial disks of mixing protrusions. If the mixing protrusions are in the form of axial rods that form the radially outermost portion of the mixing device, there may be only a single set.

[0045] In a preferred configuration, the mixing protrusions of each set are aligned with five radially separated axial planes, i.e., the central axis C TC When viewed along the mixed device length l md There are a total of 100 mixed lobes across the board, and 10 mixed lobes in each set (# mp In a particular configuration with axial offset radial planes (=10), there will be an additional 9 sets aligned in the axially offset radial planes.

[0046] In another embodiment of the invention, each or some of the mixing protrusions in each set may be axially offset. Thus, the axial length l of the mixing device md Rather than having maximum mixing in distinct radial planes along the inner surface, maximum mixing occurs in one or more swept areas around the circumference of the inner surface.

[0047] In one version of the latter embodiment, the mixing protrusions are spaced apart from each other by an axial length l of the mixing device. md Across the entirety, it is continuously shifted in the axial direction.

[0048] In certain embodiments, the input power of the rotary drive and / or the input power of the heating device is controlled by the output flow emitted from the at least one first outlet.

[0049] Minimum peripheral volume V p The definition of is to be interpreted as the volume between the inner wall of the vessel and the outside of the outer boundary of the mixing device (in all spatial directions). Thus, any free space of the radially separated mixing protrusions is limited to the minimum peripheral volume V p For example, if a container has an internal length l c and its inner diameter d c The mixing device is a container, the mixing device being fixed to a rotatable shaft, the mixing device extending in the radial direction on average 0.95 meters and in the axial direction on average 0.90 meters in length l, both of which are 1 meter. md Extends, diameter d md If there is a minimum peripheral volume V p is as follows: [ka] In the formula, d c = 1 meter, l c = 1 meter, d md = 0.95 meters, and l md = 0.90 meters.

[0050] Therefore, in this embodiment, V p constitutes approximately 20% of the total internal volume of the container.

[0051] The minimum peripheral rotational speed v as defined above p,min A peripheral rotation speed v that is equal to or exceeds pBy maintaining a constant inner surface area, it is ensured that all or most of the inner surface is utilized during heat transfer since the effects of gravity are avoided or nearly avoided. Additionally, the inner surface is kept clean or nearly clean, thereby keeping heat transfer higher than with existing indirect solutions.

[0052] For example, for a mixing device with a diameter of 1.1 meters and a set of eight mixing lobes arranged at its radially outermost portion (the mixing lobes in each set are mutually aligned in a common axial plane), the above relationship (v p,min =C(d md / # mp ) the minimum peripheral rotation speed v of the mixing device p,min is approximately 5 meters per second (m / s). At the inner surface, the peripheral rotation speed v p is the centripetal force F on the material. c Such a centripetal force F c The basic formula is as follows: F c =2mv p 2 / d md During the ceremony, m [kg] is the mass affected at the outermost end of the mixing lobe, v p [m / s] is the peripheral rotation speed.

[0053] d md [m] is the diameter of the mixing device. Furthermore, the prevailing gravity F g becomes: F g =mg During the ceremony, g[m / sec 2 ] is the gravitational constant = 9.8.

[0054] m [kg] is the affected mass as stated above. Centripetal force F c and gravity F gThe ratio between is therefore: [ka]

[0055] Centripetal force F c is the peripheral rotation speed v p Since the mixing speed is proportional to the square of md But the ratio is almost 5 c / F g , i.e., giving a value significantly higher than 1.

[0056] Therefore, to avoid undesirable effects from gravity during separation, the peripheral rotation speed v p can be as low as 5 m / sec (with such a configuration).

[0057] Additionally, there are 8 sets of mixing lobes per radial plane / swept area (# mp = 8) and a mixing device diameter of 2 meters (d md = 2) the mixing device has a minimum peripheral rotation speed v of 9.4 m / s p,min Similar results can be seen in mp =13 and d md = 3.25 m. Hence, the minimum speed required to avoid significant effects of gravity during operation is taken as the mixing device diameter (d md ), or the number of mixed lobes (# mp ), or any combination thereof.

[0058] It should be noted that the term "radial" hereinafter refers to a direction perpendicular to the L direction.

[0059] In favorable operation, the peripheral rotation speed of the rotary mechanism v p is the minimum peripheral volume (in the form of a vapor cloud) V pThe flow path of the gas is adjusted so that some or all of any evaporated or vaporized components / portions of material within the gas acquires turbulent properties, i.e., a movement pattern characterized by internal conditions of chaotic variations in pressure and flow velocity (as opposed to laminar flow).

[0060] The presence of such turbulent flow characteristics can be detected by measuring the temperature difference ΔT between the vessel wall and the vapor cloud. When a significant drop in ΔT is measured and / or a minimum ΔT is found, for example, down to about 50 K, the amount of fluid flow directed towards the inner wall is high, indicative of a turbulent velocity pattern.

[0061] Minimum peripheral volume V p In order to generate a high degree of turbulence within the rotor, the peripheral rotation speed of the rotary mechanism is v p However, the minimum peripheral rotation speed v p,min may be set to a speed exceeding v p,min =C(d md / # mp ), and C ≥ 45π

[0062] That is, this is at least 3.75 times the speed criteria stated above to avoid significant influence from gravity effects during operation.

[0063] The same exemplary configuration as above, i.e., a mixing device with a set of eight mixing lobes arranged on its radially outermost portion and a diameter d of 1.1 meters md When using a mixing device with a minimum peripheral rotation speed v p,min is approximately 19.4 m / sec in this preferred operation. To ensure a higher degree of turbulence and heat transfer efficiency, more favorable operation requires a minimum peripheral rotational speed v p,min has. v p,min =C(d md / # mp ) where C≧60π, or, better yet, C≧80π.

[0064] By using the above exemplary configuration, v p,min would be about 25.9 m / s or about 34.5 m / s, respectively. The peripheral rotational speed v p An increase in φ results in a desired increase in heat transfer efficiency.

[0065] 24 mixed lobes (# mp = 24) set and mixing device diameter d of 1.1m md Using a 11.5 m / s swirl nozzle, the same intense mixing (producing turbulent flow characteristics) can be obtained at velocities in excess of 11.5 m / s. However, because higher velocities contribute not only to an increased number of sweeps across the mixing volume, but also to more violent material impingement (the "winding effect"), the heat transfer efficiency will be reduced compared to the same number of passes but at higher peripheral velocities.

[0066] These embodiments are based on the length l of the mixing device. md Note that we assume a set of blending protrusions aligned in a common axial plane along

[0067] Other possible minimum peripheral rotational speeds v for this particular configuration p,min may be greater than 20 m / s, greater than 25 m / s, or greater than 30 m / s. The peripheral rotational speed v p A specific example of this may be 40 m / sec.

[0068] If the solids in the material have a low specific gravity (SG) (e.g., from biomass) compared to materials with higher SG (e.g., solids in drilling waste), turbulent flow characteristics will be achieved at lower peripheral rotation speeds.

[0069] Furthermore, if the set of mixing lobes deviates significantly from axial alignment (i.e., intersects a common axial plane), the relationship set forth above may be adjusted by adjusting the following factor f mp can be corrected by v p,min=f mp C(d md / # mp )

[0070] Wherein, the adjustment coefficient f mp is a phenomenological coefficient that depends on the degree of deviation from axial alignment along the length of the mixing device. A low degree of axial alignment results in a high f mp For example, the length of the mixing device l md uniformly distributed in both the radial and axial directions along the md = 1.1, v p.min =34.5m / sec, and # mp If f = 100, mp =12.5.

[0071] In an exemplary configuration of the separation device, the rotatable axis of the rotary mechanism is aligned with the central axis C of the chamber. TC are aligned in a consistent manner.

[0072] In another exemplary configuration, the rotatable axis extends through a center point of at least one end wall of the container.

[0073] In yet another exemplary configuration, the treatment chamber has a radial diameter d c (or, if not constant, the mean radial diameter d c ) and having a cylindrical shape with a length l c and radial diameter d c The ratio between (L / d c ) is equal to or less than 4.0, more preferably equal to or less than 2.5, even more preferably equal to or less than 2.0, even more preferably equal to or less than 1.5, e.g., 1.

[0074] In addition to or as an alternative to the above exemplary configurations, the mixing device may be arranged and designed such that it does not contribute to the net transport of material along the L direction from the inlet to the outlet. For example, the shape of the disturbance means and / or the elongated body may be such that no amount of material is pushed along the L direction, or that only an insignificant amount of material is pushed along the L direction.

[0075] In yet another exemplary configuration, the mixing device comprises a plurality of rotary disks fixed with an axial offset relative to a rotatable axis with a radially symmetric preferred orientation around the rotation axis, and a plurality of elongated bodies interconnecting the plurality of rotary disks. At least one of the plurality of rotary disks may present at least one through-opening for allowing the evaporated portion of the substance to flow therethrough during operation. At least one of these through-openings may be designed radially symmetrically around the rotation axis. Also, the at least one through-opening may be arranged in the radial half of each rotary disk located closest to the rotatable axis. In this particular configuration, the maximum peripheral volume may be defined as the volume between the inner wall of the container and the outer boundary of the rotary disk.

[0076] In yet another exemplary configuration, the rotary disk located closest to the end of the container with the substance inlet (i.e. the end opposite the second outlet 5) is small, i.e. without any through openings, while the remaining disks present such openings. Thereby, it is ensured that the non-evaporated parts, such as dried matter in the treatment chamber, present on the inner surface due to centrifugal forces, are not guided into the mixing device, i.e. the section of the chamber where gas or gaseous components will constitute the most predominant proportion of the substance. Thus, if the rotary disk at the end is not closed, there is a possibility that the non-evaporated parts will be guided through the openings of the disk into the flow of the evaporated parts of the substance near the rotatable axis. Such a flow of the non-evaporated parts increases the risk of undesired release of the non-evaporated parts from the second outlet.

[0077] In yet another exemplary configuration, the container is further disposed on at least a portion of the inner surface, thereby increasing the surface area of ​​the treatment chamber and reducing the minimum peripheral volume V p The treatment chamber may further comprise a plurality of inner auxiliary members each protruding radially into the treatment chamber. The plurality of auxiliary members are preferably distributed with an offset around the circumference of the inner surface, in particular on the inner wall oriented along the L direction. However, the plurality of auxiliary members may also each be arranged along the circumference of the inner surface at right angles to the L direction and distributed with an offset along the L direction.

[0078] In yet another exemplary configuration, the heating device comprises an enclosure arranged around the container such that a gap is created between the outer surface of the container wall and the inner surface of the enclosure. The enclosure comprises a thermal inlet for feeding a heated fluid into the gap and a thermal outlet for discharging a cooled fluid out of the gap for the purpose of transferring heat through the container wall to the treatment chamber. At least a portion of the gap may also comprise a number of protruding elements, such as fins, thereby increasing the surface area of ​​the outer wall and allowing heat to be transferred more efficiently into the container wall. The protruding elements / fins are fixed to the outer surface of the container wall and possibly also to the inner surface of the enclosure. Furthermore, the fins may extend in the L direction.

[0079] The heated fluid that travels through the gap via the thermal inlet and thermal outlet may be at least one of steam, hot steam, melt, heated liquid, or exhaust from an engine, turbine, or incinerator.

[0080] Alternatively or in addition, the heating device may comprise at least one heating element, e.g. at least one electric heating element, e.g. in the form of a heating rod inserted into a channel extending along the L direction, arranged in the container wall. Such heating rods may be distributed with an offset around the circumference of the vessel.

[0081] Alternatively, or in addition, the heating device may comprise an electric heating system, a microwave heating system, and / or an induction heating system arranged around the exterior surface of the container.

[0082] The separator further comprises a flow rate S i a delivery device for delivering the flow of material into the treatment chamber at, a clarifier for removing fine solids from the evaporated portion of the material discharged from the second outlet during operation, and a solids discharge system for discharging and collecting the non-evaporated portion discharged from the first outlet during operation.

[0083] flow rate S i may be measured as the mass flow rate in kg / hr when averaged over a suitable period, for example 1 minute, or 10 minutes, or 30 minutes, or 1 hour, or 3 hours.

[0084] Referring to step D, the input power to the heating device and / or the input power to the rotary drive may be set at a constant level and the flow rate S i is the minimum peripheral volume V p Operating temperature T within at least a portion of op is achieved and adjusted to be maintained.

[0085] Alternatively, the flow rate S i may be set at a constant rate, while the input power to the heating device and / or the input power to the rotary drive may be set at a minimum peripheral volume V p Operating temperature T within at least a portion of op is achieved and adjusted to be maintained.

[0086] In yet another exemplary configuration, the separation apparatus further comprises a temperature sensor, a control system in signal communication with the temperature sensor, a feed device, a heating device, and / or a rotary drive arranged such that the temperature in and / or at the treatment chamber can be measured directly or indirectly. The temperature can be described, for example, at the inner surface of the treatment chamber, and / or at the second outlet, and / or at the first outlet, and / or within the vessel wall, and / or anywhere on the outer surface of the vessel wall. The temperature measured in or at the treatment chamber will be defined herein as the material temperature.

[0087] The control system regulates the flow rate S based on the material temperature measured by the temperature sensor. i , the input power to the thermal device, and the input power to the rotary drive motor. The temperature measurements may be performed at time intervals, or continuously, or a combination thereof. The location of such measurements may be anywhere inside the treatment chamber, in the treatment chamber, or adjacent thereto, such as at or near the first output, and / or at or near the substance input. For example, step D may include the following partial steps: - measuring the temperature of the material by use of a temperature sensor; - new flow rate S as a function of material temperature n transmitting the material temperature to a control system which recalculates

[0088] - by transmitting a signal to the feeding device, a new flow rate S n For flow rate S i A step of adjusting.

[0089] These partial steps are typically performed while keeping the input power to the heating device and the input power to the rotary drive constant or nearly constant at set operating parameters.

[0090] When thermal energy is derived from surplus sources, the present invention may allow for the substitution or reduction of other energy inputs, such as electricity, thereby significantly reducing overall energy costs and / or consumption and / or causing a substantial reduction in CO2 equivalent emissions.

[0091] In another aspect, the invention relates to a separation device suitable for sustained thermal separation of a substance being fed into a treatment chamber. The substance is heated to a temperature above the evaporation temperature T e The composition comprises two or more components that can be evaporated at 0.5° C.

[0092] The separation device has a length l c and a height H of the treatment chamber, the treatment chamber having a vessel wall with an inner surface and an outer surface. c and height H, respectively, are the average length l across the extension of the chamber perpendicular to and along the length of the chamber. c and the average height H.

[0093] The container further includes a material inlet for delivering the material into the treatment chamber, a first outlet for discharging a non-evaporated portion of the material, such as solid particles, from the treatment chamber, a second outlet for discharging an evaporated portion of the material, such as gas and / or vapor, from the treatment chamber, and a rotary mechanism.

[0094] The rotary mechanism is adapted to rotate at least partially over the length l of the treatment chamber. c The mixing device includes a rotatable shaft arranged in the treatment chamber along a direction L (hereinafter abbreviated as L direction), and a mixing device fixed to the rotatable shaft and extending perpendicularly therefrom. The rotatable shaft is preferably aligned with a central axis C of the treatment chamber along the L direction. TC (midpoint of height H and width W). Furthermore, the rotatable shaft preferably extends through a center point of at least one of the ends of the container along direction L, with at least one of the ends of the rotatable shaft located outside the outer surface of the container.

[0095] The separation apparatus further comprises a rotary drive operatively connected to or near an end of the rotatable shaft, and a heating device arranged outside the treatment chamber, e.g., at the outer surface and / or at an inner surface within the vessel wall. The heating device is adapted to deliver thermal energy through the inner surface to a minimum peripheral volume V within the treatment chamber. p The method is configured to transmit the

[0096] Minimum peripheral volume V p The definition is the same as that of the first aspect.

[0097] The rotary drive may be at least one of an electric motor, a combustion engine, and a turbine.

[0098] The mixing device comprises a plurality of rotary discs fixed with an axial offset relative to a rotatable shaft with a radially symmetric preferred orientation about the axis of rotation, and a plurality of elongated bodies interconnecting the plurality of rotary discs.

[0099] The heating device and the rotary drive are both connected to each other via their respective operating input power P hd and P rm When operated at op is the evaporation temperature T e A minimum peripheral volume V equal to or greater than p At least a portion of the minimum peripheral volume V p It is configured to be acquired within.

[0100] By using this particular configuration, the separation device has a heat transfer rate that is significantly higher than the average transfer rate of the material initially fed into the treatment chamber, T e The vaporizable component is allowed to evaporate into a vapor cloud at the

[0101] It may also be envisaged that the rotatable shaft may also be connected to more than one rotary drive unit, such as, for example, two electric motors, an electric motor and a combustion engine, etc.

[0102] The mixing device may further comprise a plurality of radially protruding elements distributed with an offset along the L direction. The term "radially protruding element" is defined herein as an element, preferably an elongate element such as a rod, that is oriented with a significant radial component. The radial component preferably comprises more than 50%, e.g., 100%, of the total length of the element.

[0103] A plurality of radially projecting elements, such as rods, may be connected, most preferably displaceably connected, to a plurality of elongate bodies, for example by use of threads.

[0104] Additionally, the plurality of radially protruding elements may be arranged radially symmetrically around the rotatable axis.

[0105] At least one of the plurality of radially projecting elements may comprise, at or near the end closest to the inner surface, a disrupting means or structure designed to improve mixing of the materials. The disrupting means may take the form of, for example, sharp edges, disks, hammer shapes, airfoils, etc. At least the latter two exemplary shapes should be oriented with a head or leading edge pointing towards the direction of rotation of the rotating mechanism.

[0106] In a preferred embodiment, the rotary drive is configured to generate a peripheral rotation speed exceeding 5 meters per second, more preferably 20 meters per second or higher. The peripheral rotation speed is measured at the outside, preferably at the outermost radial boundary, of the mixing device. Thus, if the mixing device comprises radially protruding elements, the outermost radial boundary may be the disturbance means. Alternatively or additionally, such a boundary may be an elongated body of the mixing device.

[0107] At peripheral rotation speeds of 20 meters per second or higher, the turbulent characteristics are such that the minimum peripheral volume V p When the goal is to generate turbulent flow characteristics, the main purpose of the mixing device is not to convert kinetic energy into frictional heat, but to reach and maintain a turbulent vapor cloud inside the treatment chamber, and (at the same time) to ensure continuous heat transfer from the vapor cloud onto the inflowing material by stirring the material inside the treatment chamber such that solids contained in the inflowing material are continuously suspended within the generated vapor cloud.

[0108] The heating device has a minimum peripheral volume V p At least a part of the operating temperature T op The remaining portion of the total heat energy is thus generated by the rotational movement of the rotary mechanism.

[0109] In one exemplary configuration of the separation device, the treatment chamber has a radial diameter d c (or, if not constant, the mean radial diameter d c ) and having a cylindrical shape with a length l c and radial diameter d c The ratio between (l c / d c ) is equal to or less than 4.0, even more preferably equal to or less than 2.5, even more preferably equal to or less than 2.0, even more preferably equal to or less than 1.5, e.g., 1. This configuration is considered advantageous due to reduced cost and greater compactness, and the separation device has a minimum peripheral volume V p Because the separation process allows for instantaneous or near instantaneous heating and evaporation within the chamber (and thereby evaporation as well), there is no need to exceed a certain chamber length to complete the separation process.

[0110] In addition to or as an alternative to the above exemplary configurations, the mixing device may be arranged and designed such that it does not contribute to the net transport of material along the L direction from the inlet to the outlet. For example, the shape of the disturbance means and / or the elongated body may be such that no amount of material is pushed along the L direction, or that only an insignificant amount of material is pushed along the L direction.

[0111] In another exemplary configuration, at least one of the rotary disks exhibits at least one through-opening for allowing the evaporated portion of the substance to flow therethrough during operation. At least one of these through-openings may be designed radially symmetrically around the axis of rotation. Also, the at least one through-opening may be arranged in the radial half of each rotary disk located closest to the rotatable axis.

[0112] In a specific configuration, the rotary disk located closest to the end of the container with the substance inlet is small, i.e. without any through openings, while the remaining disks present such openings, thereby ensuring that no amount of non-evaporated part of the substance is allowed to flow out of the container at the second outlet, or only a small amount of non-evaporated part of the substance is allowed to flow out of the container at the second outlet.

[0113] The container is further disposed on at least a portion of the inner surface, thereby enlarging the surface area of ​​the treatment chamber and minimizing the minimum peripheral volume V p The treatment chamber may further comprise a plurality of inner auxiliary members each protruding radially into the treatment chamber to increase the generation of turbulence of the material within the treatment chamber. The inner auxiliary members are preferably distributed with an offset around the circumference of the inner surface, particularly on the inner wall oriented along the L direction.

[0114] In yet another exemplary configuration, the heating device further comprises an enclosure arranged around the vessel such that a gap is created between the outer surface of the vessel wall and the inner surface of the enclosure. The enclosure comprises a heat inlet and a heat outlet for feeding heated fluid into the gap and discharging heated fluid out of the gap, respectively. At least a portion of the gap may also comprise a plurality of outer fins extending in a direction perpendicular to the L direction, thereby increasing the surface area of ​​the outer wall and transferring heat more efficiently into the vessel wall. An outer support material may be fixed to the outer surface of the vessel wall and / or on the inner surface of the enclosure.

[0115] The heated fluid that travels through the gap via the thermal inlet and thermal outlet may be at least one of water vapor, hot steam, melt, heated liquid, excess exhaust from the generator, and excess exhaust from an engine, turbine, and / or incinerator.

[0116] Alternatively or in addition, the heating device may comprise at least one heating element, e.g. at least one electric heating element, e.g. in the form of a heating rod inserted into a heating channel extending along the L direction, arranged in the container wall. Such heating rods may be distributed with an offset around the circumference of the vessel.

[0117] Alternatively, or in addition, the heating device may comprise electric heating elements, microwave heaters, and / or induction heaters arranged around the exterior surface of the container.

[0118] The separator further comprises a flow rate S i The treatment chamber may include a delivery device for delivering a flow of the substance into the treatment chamber at, a purifier for purifying an evaporated portion of the substance discharged from the second outlet during operation, and a solids discharge tank for collecting a non-evaporated portion discharged from the first outlet during operation.

[0119] flow rate S imay be measured as the flow rate in kg / hour when averaged over a suitable period, for example 1 minute, or 10 minutes, or 30 minutes, or 1 hour, or 3 hours.

[0120] When thermal energy is derived from surplus sources, the present invention may enable substitution of other energy inputs, thereby significantly reducing operating energy costs and / or causing a substantial reduction in CO2 equivalent emissions.

[0121] The conceptual idea of ​​the present invention is to generate sufficient heat transfer from an external heat source onto the material to be evaporated inside a closed container such that evaporation occurs instantaneously or nearly instantaneously, in sharp contrast to traditional indirect methods where evaporation occurs more slowly.

[0122] Such instantaneous or near instantaneous evaporation is achieved by the separation apparatus of the present invention because heat from an external heat source is not transferred primarily to solids within the material (e.g., waste material), but instead to a "vapor cloud" containing the evaporated liquid and the (already) dried solid particles. If the material injected into the vessel contains moisture, the "vapor cloud" will typically contain a large amount of water vapor.

[0123] Heat is then transferred from this heated vapor cloud onto the inflowing material being mixed by the mixing device. To ensure high heat transfer, the mixing should advantageously be very intense, to the point where the components making up the vapor cloud experience turbulent flow characteristics, high internal velocities with rapid acceleration / directional changes.

[0124] As described above, intense mixing / turbulence is achieved by inserting a rotary mechanism into the treatment chamber. One purpose of the rotary mechanism is to ensure optimal mixing and, together with the heating system described above, to ensure optimal heat exchange from the vessel walls onto the various components of the vapor cloud that generate the vapor cloud. Thus, instantaneous or near instantaneous evaporation of vaporizable components within the material is achieved.

[0125] As a result, in at least one preferred embodiment, the vessel contains a vapor cloud with optimal heat transfer capability, both from the interior walls and also onto the inflowing material, at all times during operation.

[0126] The solid particles move around the container (i.e., the minimum peripheral volume V mentioned above) due to centrifugal force. p In the V direction, the continuous evaporation of the evaporable components such as water creates strong internal forces in all internal directions, which also p To ensure a high proportion of evaporated liquid in

[0127] By creating and maintaining intense mixing / turbulence against the inside walls of the vessel, the inside surfaces are kept clean. This cleaning process further aids in the goal of achieving sustained optimal heat transfer capacity during operation. Due to the mixing, solid particles will not be able to build up a layer on the inside surfaces as these surfaces are continually "washed" by the vapor cloud containing both evaporated liquid and solid particles. The intense mixing also counters gravity and further ensures that the entire inside surface can be used for the transfer of heat.

[0128] As a result of the instantaneous evaporation and intense mixing / turbulence, the separator can operate sustainably without internal transport mechanisms that would slowly heat the material.

[0129] According to one exemplary embodiment of the present invention, the container may be arranged in a generally horizontal position, however, one skilled in the art will appreciate that the container may also be arranged in a generally vertical position, or any position between a generally horizontal position and a generally vertical position.

[0130] The combination of the heating device and the rotary mechanism creates a thermal desorption unit that will ensure significantly more efficient heat transfer than known indirect thermal solutions. The mixing device will disperse and agitate the material through its rotation, thereby providing a "vapor cloud effect" inside the treatment chamber.

[0131] The intense mixing of the "steam cloud" inside the treatment chamber will result in primarily water vapor and other evaporated liquids, but also waste solids and particles, being brought into contact with the inner surfaces of the treatment chamber for a very short period of time, after which the steam and particles will transition out of contact with the inner surfaces and be continually replaced by other new steam and particles. In at least one embodiment of the invention, heat transfer from the inner surface of the treatment chamber occurs as follows.

[0132] - A mixing device creates intense mixing (preferably turbulence) within the material components present in the treatment chamber, thereby providing (in addition to the heating device) a vapor cloud, which may include vapors (e.g., water vapor and vapors from other vaporized liquids such as oil) and solids / particles.

[0133] This intense mixing on the inner surface provides high heat transfer from the inner surface and to the vapor cloud.

[0134] - Heat (thermal energy) exchanged from the inner surfaces of the treatment chamber will be instantly or nearly instantly dispersed throughout the vapor cloud due to the intense mixing.

[0135] As mentioned above, the intense mixing, in combination with the solids and particles in the vapor cloud, will keep the heated surfaces clean at all times, thereby improving heat transfer from the inner surfaces of the treatment chamber and to the vapor cloud. The intense agitation of the vapor cloud will ensure that all or nearly all of the material present inside the treatment chamber contains dried solids and vapors with nearly the same composition (i.e., ratio between different components) and temperature.

[0136] Moreover, at least the inner surface along the L direction is heated and in contact with the vapor cloud. It is thus avoided that only the bottom area of ​​the container is active in transferring heat to the substance, as would be the case in other known indirect methods. A larger effective heating surface is thus obtained compared to prior art solutions, since heat will be transferred to the vapor cloud and the vapor cloud resulting from the mixing will be in contact with the entire heating surface of the treatment chamber.

[0137] The treatment chamber may be set at atmospheric pressure. Alternatively, the treatment chamber pressure may be below atmospheric pressure, for example at or below 0.3 bar. For example, the present application provides the following: (Item 1) A method for thermal separation of a material (12) flowing into a treatment chamber (2) by use of a separation device (100), comprising: The separation device (100) comprises: Length l c a container (1) having a container wall with an inner surface (1a) enclosing a treatment chamber (2) of length, height H and width W, said container (1) comprising at least one substance inlet (3) and at least one first outlet (4) and at least one second outlet (5) for the non-evaporable and evaporable portions (12a, 12b), respectively; a heating device (6) arranged outside the treatment chamber (2); The length l of the treatment chamber (2) c a rotatable shaft (7a) arranged within said treatment chamber (2) oriented along a radial direction d md and axial length l md A rotary mechanism (7) having a mixing device (7b-d) of The method comprises: A. Heating the inner surface (1a) by using the heating device (6) and distributing thermal energy to the minimum peripheral volume (V p ) B. By use of a rotary drive (10) operatively fixed to said rotatable shaft (7a), said rotary mechanism (7) is driven to a minimum peripheral rotational speed (v p,min ) p ) and C. Using a delivery device (20), delivering the substance (12) through the at least one substance inlet (3) into the treatment chamber (2), the substance (12) comprising two or more components, at least one of the components having a vaporization temperature (T e ) in which the mixture is evaporated; D. The input power of the heating device (6); a flow of said material (12) fed into at least one of said at least one material inlet (3); The input power of the rotary drive unit (10) an output flow of a non-vaporized portion (12a) of said substance (12) discharged from said at least one first outlet (4); and At least one of the minimum peripheral volumes (V p ) during operation, the total heat energy transferred to at least a portion of the vaporization temperature (T e Operating temperature (T op ) by the heating device (6), p the amount of heat energy transferred into the portion of said heating element comprises more than 60% of said total heat energy transferred; A method comprising: (Item 2) 2. The separating apparatus (100) according to item 1, wherein the outermost radial portion of said mixing device (7b-d) comprises a plurality of radially separated mixing protrusions (7c, 7d). (Item 3) The plurality of radially separated mixing protrusions (7c, 7d) are spaced apart along the axial length (l) of the mixing device (7b-d). md ) into one or more sets distributed axially along said rotatable shaft (7a), the number of mixing protrusions (7c, 7d) in each set being defined as the number of said mixing protrusions (7c, 7d) in a perfect circle around said rotatable shaft (7a) as viewed along the direction of said rotatable shaft (7a); The minimum peripheral rotation speed (v p,min ) is further defined as follows: v p,min =C(d md / # mp ) During the ceremony, C is a constant greater than or equal to 12π, # mp is the number of said radially separated mixing lobes (7c, d) in each set, d md [m] is the radial diameter of the mixing device (7b-d); Item 3. A separation device (100) according to item 2. (Item 4) The radial diameter (d md ) and the radial diameter (d c ) is 0.8 to 1.0. (Item 5) The peripheral rotation speed (v p ) is the minimum peripheral volume (V p 4. The method according to any one of the preceding claims, wherein the evaporated portion (12b) of the material (12) present in the vaporizer (12b) is adjusted to acquire turbulent characteristics. (Item 6) The plurality of radially separated mixing protrusions (7c, 7d) are spaced apart along the axial length (l) of the mixing device (7b-d). md ) into one or more sets distributed axially along said rotatable shaft (7a), the number of mixing protrusions (7c, 7d) in each set being defined as the number of said mixing protrusions (7c, 7d) in a perfect circle around said rotatable shaft (7a) as viewed along the direction of said rotatable shaft (7a); The minimum peripheral rotation speed (v p,min ) is further defined as follows: v p,min =C(d md / # mp ) During the ceremony, C is a constant greater than or equal to 45π; # mp is the number of said radially separated mixing lobes (7c, d) in each set, d md [m] is the radial diameter of the mixing device (7b-d); The method according to any one of the above items. (Item 7) The rotatable shaft (7a) is aligned with the central axis (C TC ) is aligned in accordance with the method of any one of the preceding items. (Item 8) The heating device (6) is arranged to extend over the length l of the treatment chamber (2). c The method according to any one of the preceding items, wherein the substrate is oriented in the direction of (Item 9) The heating device (6) further comprises: An enclosure (13), arranged around the container (1) such that a gap (14) is created between an outer surface (1b) of the container wall and an inner surface of the enclosure (13), the enclosure (13) comprising an enclosure inlet (13a) allowing the feeding of a heating means (6') into the gap (14). 3. The method according to any one of the preceding items, comprising: (Item 10) 2. The method according to any one of the preceding claims, wherein at least a portion of the outer surface (1b) of the vessel wall is provided with a plurality of outer fins (16). (Item 11) 2. The method according to any one of the preceding claims, wherein the heating device (6) is arranged at least partially within the vessel wall. (Item 12) Flow rate (S i ) is set at a constant rate, the input power to the heating device (6) and the input power to the rotary drive (10) are p ) at least a portion of the operating temperature (T op The method according to any one of the preceding items, wherein the above-mentioned three methods are mutually adjusted so as to achieve the above-mentioned: (Item 13) The input power to the rotary drive (10) and the input power to the heating device (6) are set at a constant level and the flow rate (S i ) is the minimum peripheral volume (V p The operating temperature (T op The method according to any one of items 1 to 12, wherein the above-mentioned formula (1) is adjusted so as to achieve the above-mentioned formula (1). (Item 14) The separation device (100) further comprises: a temperature sensor (19) arranged such that the temperature in or at the treatment chamber (2) can be monitored; A control system in signal communication with the temperature sensor (19), the feeding device (20), the rotary drive (10), and the heating device (6), the control system controlling a flow rate (S) based on the temperature measured by the temperature sensor (19). i a control system configured to automatically adjust at least one of the input power of the rotary drive (10) and the input power of the heating device (6); 3. The method according to any one of the preceding items, comprising: (Item 15) The separation device (100) further comprises: A temperature sensor (19) arranged so that the temperature in or at the treatment chamber (2) can be monitored. Equipped with The separation device further comprises: A control system in signal communication with the temperature sensor (19) and the delivery device (20), the control system controlling the flow rate (S) from the delivery device (20) based on the temperature measured by the temperature sensor (19). i a control system configured to automatically adjust Equipped with Step D is measuring the temperature in or at the treatment chamber (2); The new flow rate (S n transmitting said temperature to said control system which calculates The new flow rate (S n ) for the above flow rate (S i ) adjusting the The method according to any one of the preceding items, comprising: (Item 16) The mixing device (7b-c) is a plurality of rotary discs (7b) fixed to the rotatable shaft (7a) with an axial offset; a plurality of axially oriented elongate bodies (7c) interconnecting said plurality of rotary discs (7b); 3. The method according to any one of the preceding items, comprising: (Item 17) 17. The method according to claim 16, wherein each of the plurality of rotary discs (7b) exhibits at least one through opening (7b1) for allowing the evaporation portion (12b) to flow therethrough during operation. (Item 18) 2. The method according to any one of the preceding claims, wherein the mixing device (7b-c) comprises a plurality of radially protruding elements (7d) distributed with an offset along the length of the rotatable shaft (7a). (Item 19) 19. The method according to claim 18, wherein the mixing device (7b-c) comprises a plurality of rotary discs (7b) fixed with an axial offset relative to the rotatable shaft (7a) and a plurality of axially oriented elongated bodies (7c) interconnecting the plurality of rotary discs (7b), and the plurality of radially protruding elements (7d) are displaceably connected to the plurality of axially oriented elongated bodies (7c). (Item 20) The container (1) has an inner axial length l c and the inner radial diameter d c and the inner axial length d c and the inner radial diameter d c The method according to any one of the preceding items, wherein the ratio between is less than or equal to 4.0. [Brief description of the drawings]

[0138] The following drawings are included to facilitate an understanding of the invention. The drawings illustrate embodiments of the invention which will now be described by way of example only. [Figure 1]FIG. 1 is a schematic side view of a separation apparatus according to the present invention.

[0139] [Diagram 2] FIG. 2 is a schematic side view of a separation assembly in accordance with the present invention.

[0140] [Diagram 3] FIG. 3 is a perspective cutaway side view of a first embodiment of a separation device according to the present invention.

[0141] [Figure 4] FIG. 4 is a perspective cutaway side view of the separation device of FIG. 3, in which the inner support is disposed on an inner surface of the container.

[0142] [Diagram 5] FIG. 5 is a perspective cutaway front view of the separation device of FIG. 3 with the cutting plane located further into the container of the device.

[0143] [Figure 6] FIG. 6 is a perspective cutaway side view of a peripheral portion of the separation device shown in FIG. 3, with one radially protruding element shown in greater detail in a separate drawing.

[0144] [Figure 7] FIG. 7 is a perspective side view of the separation device of FIGS. 3-5.

[0145] [Figure 8] FIG. 8 is a perspective cutaway side view of a second embodiment of a separation device according to the present invention, in which one turbulence-generating elongate body is shown in greater detail in a separate drawing.

[0146] [Figure 9] FIG. 9 is a perspective cutaway side view of the separation device of FIG. 8, in which the inner support is disposed on an inner surface of the container.

[0147] [Figure 10] FIG. 10 is a perspective side view of a rotary mechanism of a separating apparatus according to the present invention. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0148] Detailed Description of the Invention In the following, embodiments of the invention will be discussed in more detail with reference to the accompanying drawings, in which it will be understood, however, that the drawings are not intended to limit the invention to the subject matter depicted therein.

[0149] It should be understood that certain features of the invention that are, for clarity, described in the context of separate embodiments, may also be provided in combination in a single embodiment. Conversely, various features of the invention that are, for brevity, described in the context of a single embodiment, may also be provided separately or in any suitable subcombination. In particular, it should be understood that features described in relation to one particular embodiment may be interchangeable with features described in relation to other embodiments.

[0150] In particular, referring to FIG. 1, which shows a first embodiment of the present invention, a separation device 100 is configured to perform continuous thermal separation of a substance 12 flowing into a treatment chamber 2 inside a cylindrical container 1 having an inner surface 1a and an outer surface 1b. The container has a length l c and a cylindrical wall of diameter d c and two circular (or alternatively, elliptical, or rectangular, or square, with height H and width W) end walls.

[0151] The substance 12 delivered into the substance inlet 3 by use of a delivery device 20 (FIG. 2) is a multi-component (A n , n>1) consisting of one or more of these components 12b (A e m , m≦n) have distinct evaporation temperatures (T e i , i = 1...m). Therefore, a part 12a (A n-m ) is the set operating temperature (Top ≧T e i ), which may be considered non-evaporable within the container 1. The non-evaporable and evaporable portions 12a, 12b are discharged from the container 1 through the first and second outlets 4, 5, respectively. During operation, a vapor cloud 12c is formed, which includes a mixture of the non-evaporable portion 12a and the evaporable portion 12b. The vapor cloud 12c includes both fluids (gas and / or liquid) and solids / particles.

[0152] The container 1 is arranged along a central longitudinal axis C of the container 1. TC The container 1 includes a rotary mechanism 7 having a rotatable shaft 7a aligned with the container 1. The shaft 7a extends along the length l of the container 1. c and through at least one, and preferably both, of the end walls.

[0153] The rotary mechanism 7 further includes mixing devices 7b-d fixed to the rotatable shaft 7a inside the treatment chamber 2. The mixing devices 7b-d comprise at least one, preferably at least two rotary pulleys or disks 7b fixed firmly on the shaft 7a at right angles and a plurality of mixing protrusions / protrusion elements 7d fixed to the outer radial ends of the disks 7b. In case of a plurality of disks 7b, these are arranged with a spacing / offset along the longitudinal direction (i.e., the longitudinal axis C) of the shaft 7a. In FIG. 1, a total of seven spaced disks 7b are shown, all disks except the leftmost disk presenting an opening 7b1 in the vicinity of the shaft 7a, thereby allowing the vaporized component 12b to flow through it. The main purpose of the single closed disk 7b, arranged closest to the end wall presenting the material inlet 3 (see Figure 7), is to prevent solids from the vapor cloud 12c from entering the volume between the rotatable shaft 7a and the protruding element 7d, thereby avoiding them mixing with the evaporated portion 12b and being discharged through the second outlet 5.

[0154] Further, to prevent solids from escaping through the second outlet 5, narrow slits consisting of two circumferentially extending plates 23 are fixed to the disc 7b nearest the second outlet 5 and to the adjacent inner wall 1a, respectively.

[0155] The mixing device 7b-d further comprises a number of bars 7c fixed to or near the outer edge 7b2 of the disks 7b, each of the bars 7c having a length and a length extending in a direction perpendicular to the central axis C of the container 1, allowing the interconnection of two or more of the disks 7b, preferably all of the disks 7b. TC and an orientation oriented along (parallel to)

[0156] 1-6, the mixing devices 7b-d are also arranged radially toward the inner surface 1a of the cylindrical wall of the vessel 1, i.e., toward the central axis C of the vessel 1. TC 1 and 2. The inner wall 1a is provided with a number of rods 7d displaceably connected to each bar 7c so as to project perpendicularly to the inner wall 1a. The main purpose of the rods 7d is to generate intense mixing of the vapor cloud 12c and improve heat transfer from the inner wall 1a.

[0157] Using the particular configuration shown in FIG. 1, experiments have demonstrated that intense mixing of the vapor cloud 12c occurs at a peripheral velocity v of 34.5 m / s measured at the end of rod 7d closest to the inner vessel wall. p During the experiment, eight rods were mp = 8) with a set of mixed devices 7a-d, each with a mixed device length l md The eight rods 7d of each set are further distributed at intervals along the entire circumference of the mixing device 7b-d. The mixing device 7b-d has a diameter d md and the inner vessel diameter d c was 1.2m.

[0158] A peripheral speed of 34.5 m / s using this particular configuration corresponds to a rotation speed ω of 600 revolutions per minute (rpm). revBy using eight rods 7d around the circumference of the mixing device, this corresponds to 4,800 sweeps per minute (spm) across the specific area of ​​the inner vessel wall 11a.

[0159] If the number of sweeps is determined to be constant, the minimum peripheral rotational speed v at the outer radial boundary of the rod / mixing protrusion p,min It can be deduced that can be formulated as follows: v p,min =80π(d md / # mp ) In the formula, d md is the diameter of the mixing device, # mp is the number of blending lobes.

[0160] Further experiments indicate that a vapor cloud with turbulent characteristics can be achieved at a number of spm significantly lower than 4,800, at least as low as 2,700 spm, which corresponds to a certain minimum peripheral rotational speed.

[0161] It is v p,min =45π(d md / # mp ).

[0162] With particular reference to FIG. 6, the shape of the end 7d1 of each rod 7d mounted closest to the inner surface 1a is varied to define a minimum peripheral volume V p As shown in the detailed view in the oval frame of FIG. 6, the ends of the rods 7d may be flat or nearly flat with respect to the facing front inner surface 1a. However, the ends 7d1 may be spaced apart from the minimum peripheral volume V pThe end 7d1 may be of any shape, so long as it contributes to the mixing of the vapor cloud 12c present within the vessel 1. The detailed drawings within the oval frame of FIG. 1 show various examples of possible shapes of the end 7d1. Note that all of the exemplary rods 7d within the oval frame of FIG. 1 are turned 90° counterclockwise relative to the rods 7d shown within the vessel 1.

[0163] To ensure the rotation of the rotary mechanism 7 and thereby also of the mixing devices 7b-d, the end section 7a1 of the shaft 7a is connected to a rotary drive 10. As shown in Fig. 2, the latter is powered by an internal and / or external rotary motor 10a. In the exemplary configuration shown in Fig. 2, the rotary drive 10 comprises a rotary motor 10a, a transmission belt 10b and two transmission pulleys 10c arranged around the rotatable axes of the end section 7a1 and the rotary motor 10a, respectively.

[0164] The first outlet 4 is dedicated to emitting solid particles (non-evaporated portion) 12a, while the second outlet 5 is dedicated to emitting evaporated portion 12b. To avoid the emission of vapor out of the treatment chamber 2 through the first outlet 4, a rotary valve 22 (FIG. 1) is fixed to the first outlet 4, thereby discharging the non-evaporated portion 12a from the first outlet 4.

[0165] After being discharged from the first outlet 4 through the rotary valve 22, the non-evaporated portion 12a may be collected by a dedicated solids dispensing container 40 arranged below or partially below the vessel 1 (FIG. 2).

[0166] To monitor the temperature inside the vessel 1, one or more temperature sensors 19 at various locations may be positioned in or near the treatment chamber 2, for example, outside or in the vessel wall and / or in the first outlet 4. The latter location is depicted in FIG. The vapor 12b may be fed into a condensation system 30. The latter may be carried out in three steps.

[0167] The steam 12b flows into the gas purifier, cleaning the steam 12b for small amounts of solid particulates. Small amounts of the first liquid, such as oil, may also condense in the gas purifier.

[0168] The cleaned steam 12b further flows into a liquid condenser, for example an oil condenser, to condense the first liquid from the steam 12b.

[0169] - Finally, the cleaned steam, which does not have any amount of the first liquid (e.g. lighter oil) or has a reduced amount of the first liquid (e.g. lighter oil), flows into a water steam condenser, which condenses at least a second type of liquid, such as water, and, if applicable, the reduced amount of the first liquid.

[0170] In FIG. 1, the first outlet 4 and the second outlet 5 are seen to be arranged adjacent to the distal end wall of the rotary drive 10, and their openings out of the container 1 are respectively aligned along the central axis C. TC oriented along the central axis C TC 3-5 and 7 of the first embodiment and FIGS. 8-9 of the second embodiment show an alternative configuration of the first outlet 4, having a vertical opening out from the treatment chamber 2 at the base of the container 1.

[0171] Total radial diameter d of the rotary mechanism 7 / mixing device 7b-d md That is, the central axis C TC The total radial length from the radial boundary of the rotary mechanism 7 to the diameter d c For example, the inner diameter d c is 2 metres, the average distance between the end 7d1 of each of the plurality of rods 7d and the inner surface 1a should preferably be less than 10cm, for example 3 or 4cm. In all of the example configurations of FIGS. 1 and 3-9, the heating device 6 is depicted as an assembly comprising both: central axis C TC a plurality of resistive heating elements in the form of poles / rods 6″ arranged within the vessel wall along (i.e., parallel to)

[0172] A high temperature fluid system arranged around a cylindrical wall, comprising an enclosure 13 forming a gap 14 between an inner surface of the enclosure 13 and an outer surface 1b of the vessel 1. The enclosure 13 further comprises a heat inlet 13a for feeding a heated fluid 6' into the gap 14 and a heat outlet 13b for discharging the heated fluid 6' out of the gap 14.

[0173] However, it should be noted that the heating device 6 may comprise any type and any number of heating mechanisms capable of heating the inner wall 1a of the vessel 1. For example, in alternative embodiments, the heating device 6 may consist only of one or more resistive heating elements in and / or on the outside of the container wall, or only of the hot fluid system. The heating device 6 may alternatively or additionally comprise a microwave heater system and / or an inductive heater system arranged on or near the outer surface 1b of the vessel 1 and / or inside the treatment chamber 2.

[0174] FIG. 7 shows a separation device 100, in which one of the end walls of the vessel 1 presents two material inlets 3, an opening for the rotatable shaft 7a and an inspection / service hatch 18. However, it is understood that this end wall may comprise any number of material inlets 3 and any number of hatches 18. For the particular configuration shown in FIG. 7, only one of the two material inlets 3 is used during operation. The other may be closed, for example, by the same material as the rest of the vessel 1 or with transparent glass. Alternatively, material 12 may be fed through both inlets 3 during operation.

[0175] Black arrows 6' pointing into the heat inlet 13a and out from the heat outlet 13b, respectively, represent the flow of hot fluid.

[0176] 8 and 9 show a second embodiment of the separation device 100. In comparison with the first embodiment, the rods 7d are omitted. The rotary mechanism 7 thus comprises a rotatable shaft 7a and a mixing device 7c-d, the latter being constructed by a number of disks 7b and interconnecting bars 7c. The minimum peripheral volume V p The desired mixing of the substance 12 within is then ensured primarily by the longitudinally oriented bars 7c.

[0177] To allow for maximized mixing, the vapor cloud 12c is preferably V p As long as the turbulent flow characteristics are experienced within the bar 7c, the shape of the bar 7c can be optimized, for example, through repeated testing in which bars 7c of various shapes are inserted and operated, and heat transfer is measured during each operation. Figures 8-9 show an exemplary configuration of bars 7c whose longitudinal cross-sectional area exhibits a triangular shape. The sharp edges 7c1 of the triangular bars 7c can induce additional turbulence and intense mixing of the vapor cloud 12c within the smallest peripheral volume.

[0178] The above described separation apparatus 100 allows for the effective removal of liquids and / or gases from the material 12 by thermal separation, for example using waste heat 6' as the main indirect energy for the separation of waste and by-products. Due to the combined external heating of the vessel 1 and the intense mixing of the material components / vapor cloud 12c, the separation apparatus 100 can operate sustainably without the presence of a net internal transport mechanism that would cause gradual heating of the material 12 (as is required in currently known indirect separation methods).

[0179] By using the above described apparatus 100, heat is not transferred primarily to the solids in the waste, as is the case for indirect separation methods. Instead, heat is transferred to the vapor cloud 12c, which has a much higher heat transfer coefficient. This vapor cloud 12c is composed primarily of evaporated liquid / gas (by volume) and also hot non-evaporated particles. If water is present in the influent material 12, the "evaporated" vapor cloud 12c will necessarily contain water vapor. During operation, the following process steps occur:

[0180] A heating device 6 and a rotary mechanism 7 transform the inflowing material 12 into a vapor cloud 12c.

[0181] - Thermal energy from the heating device 6 is transferred from the inner surface 1a of the vessel 1 to the generated vapour cloud 12c.

[0182] - Thermal energy is then transferred from this heated vapor cloud 12c onto the inflowing material 12 by the intense mixing / turbulence from the rotary mechanism 7.

[0183] The heat transfer from the steel to the dried solids found in prior art indirectly heated separators is typically around 75 W / m 2 In comparison, heat transfer from steel to water vapor (which would typically be the main component of the vapor cloud 12c during thermal separation of waste) is significantly higher, typically around 6,000 W / m 2 It's K.

[0184] Thus, by heating the material 12 via the heating steps described above, the device of the present invention can achieve a thermal energy of 75 W / m 2 Significantly higher than K (but 6,000 W / m 2 K).

[0185] The final heat transfer will depend, among other things, on the moisture content. For example, 1,000 W / m 2 K and 1,200 W / m 2The heat transfer coefficient between 0.25 and 1.0 K has been verified when thermal separation tests were performed on a material containing (by weight) approximately 15% water, 15% oil, and 70% non-evaporable materials, the latter being a typical composition for cuttings after a drilling operation.

[0186] As mentioned above, the intense mixing / turbulence mechanism ensures optimal mixing and heat exchange from the vapor cloud 12c onto the substance 12 being continuously pumped through the substance inlet 3, and the various components in the substance will thereby cause, in particular, almost instantaneous evaporation of the liquid within the substance 12. The vessel 1 will thereby contain the vapor cloud 12c with optimal heat transfer capacity both from the inner surface 1a and onto the incoming substance 12 at all times.

[0187] Any generated vapor cloud particles will inevitably be pushed to the periphery of the treatment chamber by centrifugal forces, but the continued evaporation of the liquid (such as water) will generate strong internal forces in all internal directions, thereby ensuring a high proportion of vapor (water vapor) at the periphery.

[0188] Tests with the separation device of the present invention have been carried out while treating waste material (cuttings from drilling operations) containing, by weight, 70% mineral solids, 15% water and 15% oil. Tests have demonstrated a maximum energy dissipation rate of approximately 1,000 W / m 2 K and 1,200 W / m 2 A heat transfer coefficient between 0.25 and 1.0 K was demonstrated. Even higher heat transfer coefficients are expected for materials with higher water content.

[0189] In the preceding description, various aspects of the method and apparatus according to the present invention have been described with reference to illustrative embodiments. For purposes of explanation, specific values, systems, and configurations have been set forth to provide a thorough understanding of the apparatus and its operation. However, this description is not intended to be construed in a limiting sense. Various modifications and variations of the illustrative embodiments, and other embodiments of the method and apparatus, that are apparent to those skilled in the art to which the disclosed subject matter pertains, are deemed to be within the scope of the present invention.

Claims

1. A method for thermal separation of a material (12) flowing into a treatment chamber (2) by use of a separation device (100), comprising: The separation device (100) comprises: Length l ｃ a container (1) having a container wall with an inner surface (1a) enclosing a treatment chamber (2) of length 1, height H and width W, said container (1) comprising at least one substance inlet (3) and at least one first outlet (4) and at least one second outlet (5) for the non-evaporable and evaporable portions (12a, 12b), respectively; a heating device (6) arranged outside the treatment chamber (2); The length l of the treatment chamber (2) ｃ a rotatable shaft (7a) arranged within said treatment chamber (2) oriented along a radial direction d ｍｄ and axial length l ｍｄ A rotary mechanism (7) comprising a mixing device (7b-d) of The method comprises: A. Heating the inner surface (1a) by using the heating device (6) and distributing thermal energy to the minimum peripheral volume (V ｐ ) B. By use of a rotary drive (10) operatively fixed to said rotatable shaft (7a), said rotary mechanism (7) is driven to a minimum peripheral rotational speed (v ) of 5 meters per second measured at the radially outer boundary of said mixing device (7b-d). ｐ，ｍｉｎ ) ｐ ) and C. Using a delivery device (20), delivering said substance (12) through said at least one substance inlet (3) into said treatment chamber (2), said substance (12) comprising two or more components, at least one of said components having a vaporization temperature (T ｅ ) in which the mixture is evaporated; D. the input power of the heating device (6); a flow of said material (12) fed into at least one of said at least one material inlet (3); The input power of the rotary drive unit (10); an output flow of a non-vaporized portion (12a) of said substance (12) discharged from said at least one first outlet (4); and At least one of the minimum peripheral volumes (V ｐ ) during operation is at least a portion of the evaporation temperature (T ｅ ) operating temperature (T ｏｐ ) by the heating device (6), ｐ the amount of heat energy transferred into the portion of the heating element comprises more than 60% of the total heat energy transferred; the total transferred heat energy combined with the rotation of said rotary mechanism (7) produces a vapor cloud comprising a mixture of said non-evaporable and vaporizable portions (12a, 12b); the peripheral rotation speed (vp) of said rotary mechanism (7) is adjusted so that part or all of the evaporated portion (12b) of said substance (12) present in said minimum peripheral volume (Vp) in the form of said vapor cloud acquires turbulent characteristics, said turbulent characteristics being detected by measuring a temperature difference ΔT between said container wall and said vapor cloud; A method comprising:

2. The method of claim 1, wherein the outermost radial portion of the mixing device (7b-d) comprises a plurality of radially separated mixing protrusions (7c, 7d).

3. The plurality of radially separated mixing protrusions (7c, 7d) are spaced apart over the axial length (l) of the mixing device (7b-d). ｍｄ ) into one or more sets distributed axially along said rotatable shaft (7a), the number of mixing protrusions (7c, 7d) in each set being defined as the number of said mixing protrusions (7c, 7d) in a perfect circle around said rotatable shaft (7a) as viewed along the direction of said rotatable shaft (7a); The minimum peripheral rotation speed (v ｐ，ｍｉｎ ) is further defined as follows: v ｐ，ｍｉｎ = C (d ｍｄ / # ｍｐ ) / Second During the ceremony, C is a constant greater than or equal to 12π; # ｍｐ is the number of said radially separated mixing lobes (7c, d) in each set, d ｍｄ [m] is the radial diameter of the mixing device (7b-d); The method of claim 2.

4. The plurality of radially separated mixing protrusions (7c, 7d) are spaced apart over the axial length (l) of the mixing device (7b-d). ｍｄ ) into one or more sets distributed axially along said rotatable shaft (7a), the number of mixing protrusions (7c, 7d) in each set being defined as the number of said mixing protrusions (7c, 7d) in a perfect circle around said rotatable shaft (7a) as viewed along the direction of said rotatable shaft (7a); The minimum peripheral rotation speed (v ｐ，ｍｉｎ ) is further defined as follows: v ｐ，ｍｉｎ = C (d ｍｄ / # ｍｐ ) / Second During the ceremony, C is a constant equal to or greater than 45π; # ｍｐ is the number of said radially separated mixing lobes (7c, d) in each set, d ｍｄ [m] is the radial diameter of said mixing device (7b-d) The method of claim 2.

5. The radial diameter (d ｍｄ ) and the radial diameter (d ｃ 5. The method according to claim 1, wherein the ratio between

6. The rotatable shaft (7a) is aligned with the central axis (C) of the treatment chamber (2). ＴＣ 6. The method of claim 1, wherein the sequence is aligned in accordance with the sequence of the first sequence.

7. The heating device (6) is arranged to extend over the length l of the treatment chamber (2). ｃ The method according to any one of claims 1 to 6, wherein the first and second electrodes are oriented in the direction of

8. The heating device (6) further comprises: An enclosure (13), arranged around the vessel (1) such that a gap (14) is created between an outer surface (1b) of the vessel wall and an inner surface of the enclosure (13), the enclosure (13) comprising an enclosure inlet (13a) allowing the feeding of a heating means (6') into the gap (14). The method according to any one of claims 1 to 7, comprising:

9. The method according to any one of the preceding claims, wherein at least a portion of the outer surface (1b) of the vessel wall is provided with a plurality of outer fins (16).

10. The method according to any one of the preceding claims, wherein the heating device (6) is arranged at least partially within the vessel wall.

11. Flow rate (S ｉ ) is set at a constant rate, the input power to the heating device (6) and the input power to the rotary drive (10) are ｐ ) in at least a portion of the operating temperature (T ｏｐ The method according to any one of claims 1 to 10, wherein the above-mentioned formula (1) and (2) are mutually adjusted so as to achieve the above-mentioned formula (1).

12. When the input power to the rotary drive (10) and the input power to the heating device (6) are set at a certain level, the flow rate (S ｉ ) is the minimum peripheral volume (V ｐ The operating temperature (T ｏｐ The method according to any one of claims 1 to 11, wherein the above-mentioned formula (1) is adjusted so as to achieve the above-mentioned formula (1).

13. The separation device (100) further comprises: a temperature sensor (19) arranged such that the temperature in or at the treatment chamber (2) can be monitored; A control system in signal communication with the temperature sensor (19), the feeding device (20), the rotary drive (10), and the heating device (6), the control system controlling a flow rate (S ｉ a control system configured to automatically adjust at least one of the input power of the rotary drive (10) and the input power of the heating device (6); The method according to any one of claims 1 to 12, comprising:

14. The separation device (100) further comprises: A temperature sensor (19) arranged such that the temperature in or at the treatment chamber (2) can be monitored. Equipped with The separation device further comprises: A control system in signal communication with the temperature sensor (19) and the delivery device (20), the control system controlling a flow rate (S) from the delivery device (20) based on the temperature measured by the temperature sensor (19). ｉ a control system configured to automatically adjust Equipped with Step D is Measuring the temperature in or at the treatment chamber (2); The new flow rate (S ｎ transmitting said temperature to said control system which calculates The new flow rate (S ｎ ) to the flow rate (S ｉ ) adjusting the The method according to any one of claims 1 to 12, comprising:

15. The mixing device (7b-c) a plurality of rotary discs (7b) fixed with an axial offset to the rotatable shaft (7a); a plurality of axially oriented elongate bodies (7c) interconnecting said plurality of rotary discs (7b); The method according to any one of claims 1 to 14, comprising:

16. 16. The method according to claim 15, wherein each of said plurality of rotary discs (7b) presents at least one through opening (7b1) for allowing said evaporation portion (12b) to flow therethrough during operation.

17. The method according to any one of the preceding claims, wherein the mixing device (7b-c) comprises a plurality of radially projecting elements (7d) distributed with an offset along the length of the rotatable shaft (7a).

18. 18. The method according to claim 17, wherein the mixing device (7b-c) comprises a plurality of rotary discs (7b) fixed with an axial offset relative to the rotatable shaft (7a) and a plurality of axially oriented elongated bodies (7c) interconnecting the plurality of rotary discs (7b), and the plurality of radially protruding elements (7d) are displaceably connected to the plurality of axially oriented elongated bodies (7c).

19. The container (1) has an inner axial length l ｃ and the inner radial diameter d ｃ and a cylinder having an inner axial length l ｃ and the inner radial diameter d ｃ The method according to any one of claims 1 to 18, wherein the ratio between is less than or equal to 4.0.

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