1. A method for continuously processing polymeric material, comprising:

(a) selecting a solid polymeric material;

(b) heating the solid polymeric material in an extruder to produce a molten polymeric material;

(c) filtering the molten polymeric material;

(d) placing the molten polymeric material in a reactor through a chemical depolymerization process to produce a depolymerized polymeric material;

(e) cooling the depolymerized polymeric material; and is

(f) Decontaminating the depolymerized polymeric material.

2. The method of claim 1, further comprising:

(g) using gas and oil produced during the purification of the depolymerized polymeric material as fuel for at least one step of the process.

3. The method of claim 1, wherein,

the filtration involves a wire mesh changer.

4. The method of claim 1, wherein,

the filtration involves a filter bed.

5. The method of claim 1, wherein,

the solid polymeric material is a recycled plastic.

6. The method of claim 1, wherein,

the depolymerization process uses a catalyst.

7. The method of claim 6, wherein,

the catalyst is [ Fe-Cu-Mo-P ]]/Al₂O₃。

8. The method of claim 1, wherein,

the depolymerization process uses a second reactor.

9. The method of claim 8, wherein,

the reactors are connected in series.

10. The method of claim 9, wherein,

the reactors are stacked vertically.

11. The method of claim 9, wherein,

the reactors are stacked horizontally.

12. The method of claim 1, wherein,

the reactor includes a static mixer.

13. The method of claim 1, wherein,

the purification uses one of flash separation, an absorbent bed, clay polishing, or a thin film evaporator.

14. A system for continuously processing recycled polymeric material, comprising:

(a) a hopper configured to feed the recycled polymeric material into the system;

(b) an extruder configured to convert the recycled polymeric material into a molten material;

(c) a first reactor configured to depolymerize the molten material; and

(d) a heat exchanger configured to cool the depolymerized molten material.

15. The system of claim 14, wherein,

the extruder uses hot fluid.

16. The system of claim 14, wherein,

the extruder employs an electric heater.

17. The system of claim 14, further comprising:

(e) a separate heater configured to assist the extruder.

18. The system of claim 14, further comprising:

(e) a second reactor.

19. The system of claim 18, wherein,

the first reactor and the second reactor are connected in series.

20. The system of claim 14, wherein,

the reactor uses a catalyst material.

21. The system of claim 20, wherein,

the catalyst is [ Fe-Cu-Mo-P ]]/Al₂O₃。

22. The system of claim 21, wherein,

the catalyst is contained in a permeable container.

23. The system of claim 14, wherein,

the reactor includes a spacer tube.

24. The system of claim 14, wherein,

the reactor includes a static mixer.

25. The system of claim 14, wherein,

the reactor includes an annular insert.

26. The system of claim 24, wherein,

the static mixer is removable.

27. The system of claim 25, wherein,

the annular insert is removable.

Background

Wax and grease mixtures are constantly needed by manufacturers of machinery, food packaging machines, and other users of wax and grease for lubrication, sealing. These waxes and greases are expensive to manufacture because of the need for expensive petroleum feeds in the manufacturing process.

It would be advantageous to use readily available polyethylene waste and recycle them for the production of waxes and greases at lower cost.

It would be advantageous to produce wax and grease based feedstocks in a relatively inexpensive process. Such a process desirably employs inexpensive feeds that are readily available and uses an inexpensive process. Waste plastics/polymers have been used in known processes for making such products. Plastic waste is one of the fastest growing solid wastes, and this solid waste is utilized to produce useful waxes and greases to solve the growing plastic disposal problem.

Furthermore, most polymer/plastic wastes can be polyethylene, and due to its non-biodegradability, it accumulates in nature. Generally, polyethylene wastes are landfilled or incinerated, resulting in material loss and land waste, while incineration results in emission of greenhouse gases; at present, only a small part of plastic waste is recycled into secondary polymer, and the secondary polymer has poor quality and low return rate.

Recently, considerable efforts have been made to convert these polymeric solid wastes into useful products, such as fuels, lubricants, waxes and grease-based raw materials. Existing conversion processes may be inefficient and may release greenhouse gases into the environment. Furthermore, current techniques may be sensitive to the quality and quantity of waste plastic feed, and they may have an impact on the final product quality. This may be particularly important because the consistency of plastic waste may vary from grade to grade.

It would be desirable to provide a reactor system that is versatile enough to produce different grades of product without requiring substantial changes to operating conditions or throughput.

Disclosure of Invention

In one particular aspect, a method of producing a reaction product from a polymeric material comprises:

(a) assembling a first reactor having a first reaction zone and comprising a total number "P" of reactor modules from "N" reactor modules, wherein "N" is an integer greater than or equal to 1, wherein each of the "N" reactor modules defines a respective module reaction zone, the respective module reaction zone includes a catalyst material disposed therein, and each of the "N" reactor modules is configured to direct a flow of a molten polymer material of the reactor arrangement through the respective module reaction zone such that a flow of the molten polymer material of the reactor arrangement through the respective module reaction zone effects contact of the molten polymer material of the flowing reactor arrangement with the catalyst material, thereby effecting depolymerization of the molten polymer material of the flowing reactor arrangement, and wherein, when "N" is an integer greater than or equal to 2, each of the "N" reactor modules is configured to be connected in series to one or more of the other of the "N" reactor modules such that the plurality of reactor modules are connected in series to one another and include a plurality of module reaction zones disposed in series fluid communication with one another such that a total number of module reaction zones corresponds to a total number of connected reactor modules, and wherein the plurality of connected reactor modules are configured to direct the molten polymeric material of the reactor arrangement to flow through the plurality of module reaction zones such that the flow of the molten polymeric material of the reactor arrangement through the plurality of module reaction zones effects contact of the molten polymeric material of the flowing reactor arrangement with the catalyst material, thereby effecting depolymerization of the molten polymeric material of the flowing reactor arrangement, such that the first reaction zone comprises "P" number of module reaction zones, wherein, when "P" is an integer greater than or equal to 2, assembling the first reactor comprises connecting "P" number of reactor modules to each other in series such that "P" number of reaction zones are disposed in series fluid communication with each other;

(b) heating a polymeric material to produce a molten polymeric material;

(c) flowing molten polymeric material through a first reaction zone to effect production of a first depolymerized product material;

(d) collecting the first depolymerization product material;

(e) suspending the flow of molten polymeric material through the first reaction zone; and

(f) the first reactor was changed to a different reactor,

such that, when "P" equals 1, the modifying comprises connecting a total of "R" reactor modules of "N-1" reactor modules not used to assemble the first reactor to the first reactor, wherein "R" is an integer from 1 to "N-1", thereby producing another reactor, and the other reactor comprises a total of "R + 1" reactor modules connected in series with each other, and such that the other reactor comprises a second reaction zone comprising "R + 1" module reaction zones, wherein the other reactor is configured to direct a flow of molten polymeric material, such that the flow of molten polymeric material disposed by the reactor through the second reaction zone effects the generation of another depolymerized product material and its discharge from the other reactor; and when "P" is an integer greater than or equal to 2 but less than or equal to "N-1", the change comprises one of: (a) removing a total of "Q" reactor modules of the "P" reactor modules from the first reactor, wherein "Q" is an integer from 1 to "P-1", thereby producing another reactor and the other reactor comprises a total of "P-Q" reactor modules connected in series with each other, and such that the other reactor comprises a second reaction zone having "P-Q" module reaction zones, wherein the other reactor is configured to direct a flow of molten polymeric material such that the flow of molten polymeric material disposed by the reactor through the second reaction zone effects the production of another depolymerized product material and its discharge from the other reactor, or (b) connecting a total of "R" reactor modules of the "N-P" reactor modules that have not been used to assemble the first reactor to the first reactor, wherein "R" is an integer from 1 to "N-P" such that another reactor is produced and comprises a total of "P + R" reactor modules connected in series with one another, and further comprises a second reaction zone having "P + R" module reaction zones, wherein the other reactor is configured to direct a flow of molten polymeric material such that flow of molten polymeric material disposed by the reactor through the second reaction zone effects production of another depolymerized product material and discharge thereof from the other reactor; and when "P" is equal to "N", the altering comprises removing a total of "Q" reactor modules of the "P" reactor modules from the first reactor, wherein "Q" is an integer from 1 to "P-1", such that another reactor is produced and comprises a total of "P-Q" reactor modules connected in series with each other, and such that the other reactor comprises a second reaction zone having "P-Q" module reaction zones, wherein the other reactor is configured to direct a flow of molten polymer material, such that the flow of molten polymer material disposed by the reactor through the second reaction zone effects the production of another depolymerized product material and its discharge from the other reactor.

A method for continuously processing polymeric materials can include selecting a solid polymeric material; heating a solid polymeric material in an extruder to produce a molten polymeric material; filtering the molten polymeric material; placing the molten polymeric material in a reactor through a chemical depolymerization process to produce a depolymerized polymeric material; cooling the depolymerized polymeric material; and decontaminating the depolymerized polymeric material. In some embodiments, the method may further comprise operating a portion of the method using gas and oil produced during the purification of the depolymerized polymeric material.

In some embodiments, the filtration involves a wire mesh loader or filter bed. In certain embodiments, the solid polymeric material is a recycled plastic.

In some embodiments, the depolymerization process uses a catalyst, e.g., [ Fe-Cu-Mo-P ]]/Al₂O₃. In other or the same embodiments, the depolymerization process uses a second reactor. In certain embodiments, the reactors are connected in series, stacked vertically, and/or stacked horizontally.

In some embodiments, the one or more reactors comprise one or more static mixers.

In some embodiments, the purification utilizes one of flash separation, an absorbent bed, clay polishing, or a thin film evaporator.

A system for continuously processing recycled polymeric material may include a hopper configured to feed recycled polymeric material into the system; an extruder configured to convert the recycled polymeric material into a molten material; a first reactor configured to depolymerize a molten material; a heat exchanger configured to cool the depolymerized molten material; a second reactor; and/or a separate heater configured to assist the extruder.

In certain embodiments, the extruder uses one or more hot fluids and/or one or more electric heaters. In some embodiments, the reactors are connected in series and/or use a catalyst, e.g., [ Fe-Cu-Mo-P ]]/Al₂O₃. In some embodiments, the catalyst may compriseContained in a permeable container.

In certain embodiments, the one or more reactors comprise one or more spacer tubes, one or more static mixers, and/or one or more annular inserts. In certain embodiments, one or more static mixers and/or one or more annular inserts are removable.

Drawings

Fig. 1 is a flow chart illustrating a process for treating a polymeric material.

Fig. 2 is a schematic diagram of a system including a reactor having a total of five reactor modules.

Fig. 3 is a schematic view of the reactor shown in fig. 2, wherein the reactor is modified by removing one reactor module such that the reactor has a total of four reactor modules.

FIG. 4 is a schematic of the reactor shown in FIG. 2, wherein the reactor is modified by adding one reactor module such that the reactor has a total of six reactor modules.

FIG. 5 is a schematic diagram of a system including a reactor having two reactor modules, an inlet reactor module and an outlet reactor module.

FIG. 6 is a cross-sectional side view of the reactor module with some catalyst material removed for clarity.

FIG. 7 is a cross-sectional elevation view of one end of the reactor module of FIG. 6 with the flow guides and some catalyst material removed for clarity.

Fig. 8 is a cross-sectional side view of a connected reactor module with flow guides and catalyst material removed for clarity.

FIG. 9 is an elevation view of one end of an end cap assembly of the reactor module.

FIG. 10 is a cross-sectional side view of the end cap assembly shown in FIG. 9.

FIG. 11 is a cross-sectional elevation view of an end of the end cap assembly of FIG. 9 installed within a conduit barrel shaft of a reactor module.

FIG. 12 is a front view of an end cap assembly of the reactor module opposite the end shown in FIG. 9.

FIG. 13 is a cross-sectional elevation view of the end cap assembly shown in FIG. 12 installed within a conduit barrel shaft of a reactor module;

FIG. 14 is a partial cross-sectional perspective view of the tube spool, flow guides, wire mesh and spacer tubes of the reactor module.

FIG. 15 is a schematic view of an upstream portion of an inlet reactor module, shown connected to a heater of the system.

FIG. 16 is a schematic view of a downstream portion of the inlet reactor module shown in FIG. 15 connected to an upstream portion of an outlet reactor module of a reactor.

FIG. 17 is a schematic view of a downstream portion of the outlet reactor module shown in FIG. 16 connected to a heat exchanger of the system (for cooling the molten product material).

FIG. 18 is a schematic view of an intermediate reaction module that may be integrated within the reactor of the system shown in FIG. 16.

FIG. 19 is a cross-sectional side view of a catalytic reactor with a removable static mixer configured to be heated by a hot fluid/molten salt.

FIG. 20 is a cross-sectional side view of a catalytic reactor with a removable static mixer configured to be heated using electricity.

FIG. 21 is a cross-sectional side view of a catalytic reactor with a removable ring insert configured to be heated by a hot fluid/molten salt.

FIG. 22 is a cross-sectional side view of a catalytic reactor having a removable ring insert configured to be heated using electricity.

FIG. 23 is a cross-sectional side view of a catalytic reactor having a hollow inner member configured to be heated by a hot fluid/molten salt.

FIG. 24 is a cross-sectional side view of a catalytic reactor having hollow internals configured to be heated using electricity.

Fig. 25 is a cross-sectional elevation view of a group of catalytic reactors arranged in parallel as shown in fig. 19-24.

FIG. 26 is a cross-sectional side view of the parallel catalytic reactor device of FIG. 25 shown in a horizontal configuration.

FIG. 27 is a cross-sectional side view of the parallel catalytic reactor device of FIG. 25 shown in a vertical configuration.

FIG. 28 is a cross-sectional side view of a vertical spiral internal catalytic reactor device having two reactors connected in series.

FIG. 29 is a cross-sectional side view of a vertical annular catalytic reactor device having two reactors connected in series.

FIG. 30 is a cross-sectional side view of a vertical catalytic reactor device having two hollow reactors connected in series.

FIG. 31 is a perspective view of a horizontal reactor with an internal removable helical mixer.

Detailed Description

The process of treating polymeric material (e.g., waste polymeric material) within the reactor of the system is described below. Suitable waste polymeric materials include waste plastic materials. Virgin plastic may also be used.

Fig. 1 illustrates a process 10 for treating a polymeric material. The process 10 may be carried out batchwise, but more preferably is a continuous process. Parameters of the process 10, including but not limited to temperature, flow rate of the plastic, and total number of preheating, reacting, or cooling sections, can be varied to produce end products of different molecular weights. For example, increasing the temperature and/or decreasing the flow rate through the reaction zone or changing the number of reaction zones will result in a product having a lower molecular weight.

In material selection stage 1, a polymer feed is selected and/or prepared for processing. In some embodiments, the polymer feed is sorted/selected to include polyethylene material. In other embodiments, the polymer feed is sorted/selected to include a polypropylene material. In other embodiments, the polymer feed is sorted/selected to include polyethylene and polypropylene materials. In some embodiments, the feed may contain up to 5% polypropylene, small amounts of polystyrene and trace amounts of undesirable additives such as PVC, ash, grit or other unknown particles.

In some embodiments, the material selected in material selection stage 1 comprises recycled plastic. In other or the same embodiments, the material selected in the material selection stage 1 comprises recycled plastic and/or virgin plastic.

In some embodiments, the material selected in material selection stage 1 is heated in an extruder and subjected to a pre-filtration process 3. In some embodiments, an extruder is used to increase the temperature and/or pressure of the incoming plastic and to control the flow rate of the plastic. In some embodiments, the extruder is supplemented or completely replaced by a combination pump/heat exchanger.

The pre-filtration process 3 may employ a wire mesh changer and filter bed and other filtration techniques/devices to remove contaminants from and purify the heated material. The resulting filter material is then moved to an optional pre-heat stage 4, which pre-heat stage 4 brings the filter material to a higher temperature before it enters the reaction stage 5. The preheating stage 4 may employ static and/or dynamic mixers and heat exchangers, such as internal fins and heat pipes, among other devices and techniques.

The material in reaction stage 5 undergoes depolymerization. The depolymerization may be a purely thermal reaction and/or it may use a catalyst. Depending on the starting materials and the desired end product, depolymerization may be used for a slight or extreme reduction in the molecular weight of the starting materials. In some embodiments, the catalyst used is a zeolite support system or an alumina support system or a combination of both. In some embodiments, the catalyst is [ Fe-Cu-Mi-P ]]/Al₂O₃Prepared by combining a ferrous-copper complex with an alumina or zeolite support and reacting it with an acid comprising a metal and a non-metal [ Fe-Cu-Mo-P]/Al₂O₃。

The reaction stage 5 can employ various techniques/devices including fixed beds, horizontal reactors and/or vertical reactors and/or static mixers, among others. In some embodiments, reaction stage 5 employs multiple reactors and/or reactors divided into multiple sections.

After the reaction stage 5, the depolymerized material enters an optional cooling stage 6. The cooling stage 6 may use heat exchangers and other techniques/devices to reduce the depolymerized material to a usable temperature before entering the purification stage 7.

In some embodiments, cleaning/purging of the material is performed by such methods as nitrogen stripping prior to the cooling stage 6.

The clarification stage 7 involves the refining and/or clarification of the depolymerised material. Techniques/devices that can be used for the purification stage 7 include, but are not limited to, flash separation, adsorbent beds, clay polishing, distillation, vacuum distillation, and filtration to remove solvents, oils, color bodies, ash, inorganics, and coke. In some embodiments, a membrane or wiped film evaporator is used to remove gas, oil and/or grease from the depolymerized material. In some embodiments, the oil, gas, and grease may in turn be combusted to help operate various stages of the process 10.

The process 10 ends in the finished wax stage 8, where the initial starting material selected in the material selection stage 1 has been converted into wax. In at least some embodiments, the finished wax stage 8 wax is commercially viable and does not require additional processing and/or refinement.

As shown in fig. 2, the system 1000 includes a reactor 100 having five reactor modules 102(a) through 102 (e). The size of the reactor modules 102 may vary and/or the reactor modules 102 may be connected in parallel and/or in series. In other embodiments, various numbers of reactor modules 102 may be used. For example, fig. 3 shows a system 1000 having four reactor modules 102(a) through 102 (d). Similarly, fig. 4 shows a system 1000 having six reactor modules 102(a) through 102 (f). The ability to customize the number of reactor modules 102 allows for greater control over the amount of depolymerization.

The system 1000 may include a hopper 111 for receiving the polymeric material and/or directing a supply of the polymeric material to the optional extruder 106. In some embodiments, extruder 106 processes the polymeric material received from hopper 111 by producing molten polymeric material. The temperature of the polymeric material processed by the extruder 106 is controlled by adjusting the level of shear stress and/or heat applied to the polymeric material by the one or more extruder heaters 105. The extruder heater may use a variety of heat sources including, but not limited to, electricity, hot fluids, and/or combustion gases. The heat is regulated by the controller in response to the temperature sensed by one or more temperature sensors 107.

In some embodiments, the pressure sensor 109 measures the pressure of the molten polymeric material discharged from the extruder 106 to prevent or at least reduce the risk of pressure spikes. The discharged molten polymeric material is pressurized by pump 110 to effect its flow through heating zone 108 and reactor 100. While flowing through the reactor 100, the molten polymer material disposed in the reactor comes into contact with the catalyst material, which causes depolymerization.

One or more pressure sensors 109 and/or one or more temperature sensors 107 may also be used to measure the temperature and/or pressure, respectively, of the molten polymeric material of the reactor arrangement as it flows through the reactor 100. One or more pressure sensors 109 may monitor the plugs before and/or after each reaction zone. The one or more pressure sensors 109 may also maintain the system pressure below a maximum pressure, such as the maximum pressure for which the reactor 100 is designed. The overpressure can be controlled by feedback from the pressure transducer 109 to a controller that sends command signals to shut down the extruder 106 and pump 110, preventing further pressure increases.

In the event that the shut-off of the extruder 106 fails to release the overpressure, the discharge valve 117 can be opened to access the container to remove material from the system 1000 and avoid the overpressure condition. During shutdown, the vent valve 117 may be opened to purge the system 1000 with nitrogen to remove residual material to avoid plugging and degrading the material during the next start-up.

The system 1000 may also include a pressure relief device, such as a pressure relief valve or a burst disk, disposed at the outlet of the extruder 106 to relieve pressure from the system 1000 in the event of an overpressure.

The temperature sensor 107 may help control the temperature of the molten polymeric material flowing through the reactor arrangement of the reactor 100. This allows more precise control of the chemical reaction and the resulting polymerization. The one or more temperature sensors 107 also help maintain the temperature below a predetermined maximum temperature, such as the maximum design temperature of the reactor 100.

The temperature is controlled by a controller (not shown) that is responsive to the temperature sensed by one or more temperature sensors 119 to regulate the heat applied by the heater 118, the heater 118 being disposed in heat transfer communication with the reaction zones 102(a) through 102(e) of the reactor 100.

Flow control may also be provided within the system 1000. In some embodiments, the system 1000 includes a valve 115 disposed at the discharge of the extruder 106 for controlling flow from the extruder 106 to other unit operations within the system 1000. Valve 116 facilitates recirculation. Valve 117 enables collection of the product.

During operation, the valve 115 may be closed to recirculate and raise the temperature of the molten polymeric material to a desired temperature. In this case, valve 116 will be open, valve 117 will be closed, extruder 106 will be "shut down," and pump 110 will be recirculated.

The resulting molten product material 112 is cooled in a heat exchanger 114. among other methods, the heat exchanger 114 may be jacketed with water, air cooled, and/or cooled by a refrigerant. A portion of the cooled resulting molten product material may be recycled (in which case valve 116 would be opened) for reprocessing and/or for energy savings.

In some embodiments, the system 1000 is configured to be purged with nitrogen to mitigate oxidation of the molten product material and the creation of explosive conditions.

In another embodiment, shown in fig. 5, the system 2000 includes a reactor 600. The reactor 600 has two reactor modules, an inlet reactor module 300 and an outlet reactor module 400. The system 2000 also includes an extruder 606 for receiving the polymeric material. The extruder 606 processes the polymeric material by producing molten polymeric material. The temperature of the polymeric material processed through reactor 600 is controlled by adjusting the heat applied to the polymeric material by process heaters HE01, HE02, HE04, HE06, HE 08. Temperature sensors TC01, TC04, TC06, TC07 TC09, TC10, TC12 are provided to measure the temperature of the molten material within the reactor 600. Temperature controllers TC03, TC05, TC08, TC11 are provided to monitor and control the temperature of process heaters HE01, HE02, HE04, HE06, and HE 08. Flange heaters HE03, HE05, HE07, and HE09 are also provided to mitigate heat loss through the flange connection.

The discharged molten polymer feed material is directed through a heater 608 and reactor 600 in series. While flowing through the reactor 600, the molten polymer material disposed in the reactor is contacted with a catalyst material to effect depolymerization. The resulting molten product material is cooled in heat exchanger 614, and further, heat exchanger 614 may be jacketed with water, air cooled, or cooled with a refrigerant. In some embodiments, waste heat from cooling the molten product may be used to perform other processes. A cooling section heater HE10 is provided to melt the wax that solidifies in the cooling section.

In both system 1000 and system 2000, the reactors 100 and 600 include one or more reactor modules. Each reactor module includes a respective module reaction zone in which molten polymer material of the reactor arrangement contacts catalyst material for a residence time defined by the module, thereby causing depolymerization of the flowing molten polymer material of the reactor arrangement. In some of these embodiments, the module-defined residence times of the at least two reactor modules are the same or substantially the same. In some of these embodiments, the residence time defined by at least some of the plurality of modules differs between the residence times defined by the plurality of modules. In some of these embodiments, the catalyst material of at least two reactor modules is the same or substantially the same. In some of these embodiments, the catalyst material of at least two reactor modules is different.

In some embodiments, each reactor module comprises a reactor-disposed molten polymeric material permeable vessel containing a catalyst material. The vessel is configured to receive molten polymeric material such that at least partial depolymerization of at least a portion of the received molten polymeric material is effected by the catalyst material and to discharge molten product material comprising depolymerization reaction products (and may also include unreacted molten polymeric material and intermediate reaction products, or both). The flow of the reactor disposed molten polymeric material through the reactor disposed molten polymeric material permeable container effects contact between the catalyst material and the reactor disposed molten polymeric material to effect at least partial depolymerization of at least a portion of the reactor disposed molten polymeric material. In this regard, the flowing reactor arrangement molten polymeric material permeates through the catalyst material within the vessel and contacts the catalyst material contained within the vessel while permeating the catalyst material to effect at least partial depolymerization of at least a portion of the reactor arrangement molten polymeric material.

In system 1000 and system 2000, the first reactor is assembled from reactor modules. The first reactor has a first reaction zone and includes a total number of "P" reactor modules from "N" reactor modules, where "N" is an integer greater than or equal to 1.

Each of the "N" reactor modules defines a respective module reaction zone, the respective module reaction zone including a catalyst material disposed therein, and each of the "N" reactor modules is configured to direct a flow of a reactor-disposed molten polymer material through the respective module reaction zone such that the flow of the reactor-disposed molten polymer material through the respective module reaction zone contacts the catalyst material, thereby causing at least partial depolymerization of at least a portion of the flowing reactor-disposed molten polymer material. In this regard, the first reaction zone includes "P" modular reaction zones.

When "N" is an integer greater than or equal to 2, each of the "N" reactor modules is configured to be connected in series to one or more of the other "N" reactor modules such that the plurality of reactor modules are connected in series with each other, and the plurality of reactor modules comprises a plurality of module reaction zones disposed in series fluid communication with each other such that a total number of the module reaction zones corresponds to a total number of the connected reactor modules. The plurality of connected reactor modules are configured to direct a flow of molten polymeric material of the reactor arrangement through the plurality of module reaction zones such that it contacts the catalyst material, thereby effecting at least partial depolymerization of at least a portion of the molten polymeric material of the flowing reactor arrangement.

When "P" is an integer greater than or equal to 2, the assembling of the first reactor comprises connecting "P" reactor modules to each other in series such that "P" reaction zones are arranged in series fluid communication with each other.

In the embodiment shown in fig. 2, "P" is equal to 5, such that the reactor 100 comprises five reactor modules 102(a) to 102(e), the reaction zone being composed of five modular reaction zones 104(a) to 104(e), each reaction zone corresponding to one of the five reactor modules. It is understood that "P" may be more or less than five.

In another embodiment shown in fig. 5, "P" equals 2, such that the reactor 600 comprises two reactor modules: an inlet reactor module 300 and an outlet reactor module 400.

The molten polymeric material is produced by heating the polymeric material for supply to the constructed reactor. In some embodiments, the heating is caused by a heater. In fig. 2, the heating is caused by a combination of an extruder 106 and a separate heater 108. In fig. 5, heating is caused by a combination of an extruder 606 and a separate heater 608. In such embodiments, the resulting molten polymeric material is forced out of the extruder, flows through a separate heater, and then is fed to the module reaction zone. In some embodiments, the extruder is configured to provide sufficient heat to the polymeric material such that the resulting molten polymeric material is at a sufficiently high temperature to be supplied to the reactor, and a separate heater is not required.

As shown in fig. 2, a pump 110 receives molten polymeric material from the extruder 106 and effects delivery (or "flow") of the molten polymeric material through a heater 108 and then through the first reaction zone. In some embodiments, the extruder 106 is configured to impart sufficient force to achieve a desired flow of the molten polymeric material produced, such that the pump 110 is optional. Figure 5 shows an example without a pump.

In some embodiments, the molten polymeric material is obtained from a polymeric material feed that is heated to effect production of the molten polymeric material. In some embodiments, the polymeric material feed comprises primary particles of polyethylene. The virgin particles may comprise Low Density Polyethylene (LDPE), Linear Low Density Polyethylene (LLDPE), High Density Polyethylene (HDPE), polypropylene (PP), or a mixture comprising a combination of LDPE, LLDPE, HDPE, and PP.

In some embodiments, the polymeric material feed comprises a waste polymeric material feed. Suitable waste polymeric material feeds include mixed polyethylene waste, mixed polypropylene waste and mixtures including mixed polyethylene waste and mixed polypropylene waste. The mixed polyethylene waste may comprise Low Density Polyethylene (LDPE), Linear Low Density Polyethylene (LLDPE), High Density Polyethylene (HDPE), polypropylene (PP), or a mixture comprising a combination of LDPE, LLDPE, HDPE, and PP. In some embodiments, the mixed polyethylene waste comprises food bags, milk bags, stationery documents. In some embodiments, the waste polymeric material feed includes up to 10% by weight of a material other than polymeric material based on the total weight of the waste polymeric material feed.

Molten polymer material is supplied to the reactor and flowed through a first reaction zone (i.e., a first reaction zone comprising "P" reaction zones) as molten polymer material for the reactor setup. The flow of molten polymeric material through the first reaction zone of the reactor arrangement contacts it with the catalyst material to produce molten product material, including depolymerized product material (and, in some embodiments, unreacted molten polymeric material and/or intermediate reaction products). The molten product material was collected.

In some embodiments, the catalyst material comprises [ Fe-Cu-Mo-P ]]/Al₂O₃. By combining a ferrous-copper complex with an alumina support and combining it with a binder comprisingThe acid of the metal and the nonmetal reacts to prepare the catalyst to obtain the catalyst material. Other suitable catalyst materials include zeolites, mesoporous silica, H-mordenite, and alumina. The system can also be operated without a catalyst and produce wax by thermal degradation.

The resulting molten product material is discharged from the reactor and collected/recycled from the reactor. In some embodiments, collection of the molten product material is achieved by discharging a stream of molten product material from the reactor. In those embodiments having multiple reactor modules, the molten product material is discharged from the first reactor module and supplied to the next reactor module in the series for further depolymerization within the next reactor module in the series, and this continues in between each pair of adjacent reactor modules in the series.

In some embodiments, the depolymerized product materials produced include waxes, greases, and grease-based raw materials. Commercial fats and oils are generally prepared by mixing fat and oil based raw materials with small amounts of specific additives to give them desired physical properties. Generally, greases include four types: (a) a mixture of mineral oil and a solid lubricant; (b) a blend of residuum (residue remaining after distillation of petroleum hydrocarbons), unbound fats, rosin oils, and asphalts; (c) soap thickened mineral oil; and (d) synthetic fats and oils such as polyalphaolefins and silicones.

In some embodiments, the polymer feed material is a combination of one or more of: virgin polyethylene (any one or combination of HDPE, LDPE, LLDPE, and MDPE), virgin polypropylene, or wasted, used-in-the-industry polyethylene or polypropylene (exemplary sources include bags, kettles, bottles, drums, etc.), and it is desirable to convert such polymeric feed materials into higher melting waxes (having a melting point of from 106 ℃ to 135 ℃), medium melting waxes (having a melting point of from 86 ℃ to 105 ℃), lower melting waxes (having a melting point of from 65 ℃ to 85 ℃), lower melting waxes (having a melting point of 40 ℃ to 65 ℃) using embodiments of the systems disclosed herein. In each case, the conversion is achieved by heating the polymer feed to produce a molten polymer material, and then contacting the molten polymer material with the catalyst material in a reaction zone disposed at a temperature between 325 ℃ and 450 ℃. The quality of the wax produced (high, medium or low melting point wax) depends on the residence time of the molten polymeric material within the reaction zone. In the case where 1 to 12 reactor modules are connected in series, the residence time is 1 to 120 minutes, preferably 5 to 60 minutes, when operating in a continuous system according to the flow rate of an extruder or a gear pump. In some of these embodiments, the supplying and heating of the polymer feed material is accomplished by a combination of an extruder and a pump, wherein the material discharged from the extruder is supplied to the pump. In some of these embodiments, the Extruder 106 is a 10HP, 1.5 inch (3.81em) model Apex 1.5 Xincinnati Milacron base Extruder (Cincinnati Milacron pendant Extruder) and the pump 110 is sized 1.5HP for a 1.5 inch (3.81cm) line.

The pressure sensor PT01 monitored the plug within the extruder (and prior to PT02, see below) to maintain the system pressure below a maximum pressure (e.g., the maximum design pressure of the reactor 100). Likewise, the pressure sensor PT02 monitors the stopper elsewhere in the system. The overpressure is controlled by feedback of the pressure transmitted by PT01 and PT02 to a controller that sends command signals to shut down the extruder 106 and pump 110, preventing further pressure increases.

In some embodiments, the reactor 100 is a first reactor 100, and the reaction zone of the first reactor is a first reaction zone, and the flow of molten polymeric material through the first reaction zone is halted (e.g., such as interrupted). After the pause, the first reactor was changed.

When "P" is equal to 1, the modifying comprises connecting a total of "R" reactor modules of "N-1" reactor modules not used to assemble the first reactor to the first reactor, wherein "R" is an integer from 1 to "N-1", thereby creating another reactor, and the other reactor comprises a total of "R + 1" reactor modules connected in series with each other, and such that the other reactor comprises a second reaction zone having "R + 1" module reaction zones. The other reactor is configured to direct a flow of molten polymeric material such that the flow of molten polymeric material disposed by the reactor through the second reaction zone effects the production of another depolymerized product material and its discharge from the other reactor;

when "P" is an integer greater than or equal to 2 but less than or equal to "N-1", the change includes one of:

(a) removing a total of "Q" reactor modules of the "P" reactor modules from the first reactor, wherein "Q" is an integer from 1 to "P-1", such that another reactor is produced and comprises a total of "P-Q" reactor modules connected in series with each other, and such that the other reactor comprises a second reaction zone having "P-Q" module reaction zones, wherein the other reactor is configured to direct a flow of molten polymeric material such that the flow of molten polymeric material disposed by the reactor through the second reaction zone effects the production of another depolymerized product material and its discharge from the other reactor, or

(b) Connecting a total number "R" of reactor modules of the "N-P" reactor modules not used to assemble the first reactor to the first reactor, wherein "R" is an integer from 1 to "N-P", thereby producing another reactor, and the other reactor comprises a total number "P + R" of reactor modules connected in series with each other, and such that the other reactor also comprises a second reaction zone comprising "P + R" module reaction zones, wherein the other reactor is configured to direct a flow of molten polymeric material such that the flow of molten polymeric material disposed by the reactor through the second reaction zone effects the production of another depolymerized product material and its discharge from the other reactor; and is

When "P" is equal to "N", the changing comprises removing a total number of "Q" reactor modules of the "P" reactor modules from the first reactor, wherein "Q" is an integer from 1 to "P-1", such that another reactor is produced and the another reactor comprises a total number of "P-Q" reactor modules connected in series with each other, and such that the another reactor comprises a second reaction zone comprising "P-Q" module reaction zones. The other reactor is configured to direct a flow of molten polymeric material such that the flow of molten polymeric material disposed by the reactor through the second reaction zone effects the production of another depolymerized product material and its discharge from the other reactor.

In some embodiments, after the first reactor is modified (by any of connecting/adding or removing reactor modules) to effect production of another reactor, another reactor is used to produce a second depolymerization product material. In this regard, the polymeric material is heated to produce a molten polymeric material, and the molten polymeric material is flowed through the second reaction zone to effect production of a second depolymerization product material. The second depolymerization product material is then collected from the reactor.

In some embodiments, the same catalyst material is disposed within each of the "N" reactor modules.

In some embodiments, the reaction zone of each of the "N" reactor modules is the same or substantially the same.

Referring to fig. 6-14, in at least some embodiments, each reactor module 200 includes a spool shaft 201. In some embodiments, the reactor module 200 includes a spool shaft 201 (only one end shown in the illustrated embodiment) having opposite first and second ends, with a flange 230 at each end for facilitating connection with other reactor modules 200.

The reactor module 200 includes an inlet 202A at a first end of the spool, an outlet 202B at an opposite second end of the spool, and a fluid passageway 206 extending between the inlet 202A and the outlet 202B. Fluid channel 206 includes a catalyst material containment space disposed within a molten polymer material permeable container of a reactor arrangement, and catalyst material 204 is disposed within catalyst material containment space 216. The catalyst material receiving space 216 defines the module reaction zone 205 of the reactor module 200.

The reactor module 200 is configured to receive molten polymer material disposed by the reactor through the inlet 202A and direct the received molten polymer material through the fluid channel 206 such that it contacts the catalyst material 204. This results in at least partial depolymerization of at least a portion of the molten polymeric material, such that a molten product material is produced that includes depolymerization reaction products (and, in some embodiments, unreacted molten polymeric material and/or intermediate reaction products (e.g., partially depolymerized material)). The reactor module 200 then discharges the molten product material from the outlet 202B.

A relatively unobstructed fluid passage portion 218 of the fluid passage 206 extends between the inlet 202A and the outlet 202B and is disposed in fluid communication with the catalyst material receiving space 216 via the wire mesh. Wire mesh 208 is disposed within the conduit sleeve shaft 201 to divide the fluid passageway 206 into a relatively unobstructed fluid passageway portion 218 and a space 204 containing catalyst material. The wire mesh 208 contains the catalyst material 204 within the catalyst material containment space 216, thereby defining a molten polymer material permeable container 203.

The wire mesh 208 is disposed in spaced relation to the inner wall 210 of the conduit cylinder shaft 201 defining the fluid passageway and extends longitudinally through the length of the conduit cylinder shaft 201. The space between the wire mesh 208 and the inner wall 210 defines a relatively unobstructed fluid passage portion 218 of the fluid passage 206. Fluid communication between the fluid passage portion 218 and the catalyst material accommodating space 216 is made possible through the space within the wire net 208. Thus, the wire mesh 208 allows molten polymeric material to permeate from the relatively unobstructed fluid passage portion 218 to the catalyst material containment space 216 (thereby facilitating contact of the molten polymeric material with the catalyst material 204 within the reaction zone), and also to permeate from the catalyst material containment space 216 to the relatively unobstructed fluid passage portion 218 (for discharge of molten product material including depolymerized reaction products and unreacted molten polymeric material and/or intermediate reaction products), while preventing or substantially preventing catalyst material 204 from flowing out of the catalyst material containment space 216 to the relatively unobstructed fluid passage portion 218.

In some embodiments, the conduit sleeve shaft 201 is cylindrical and the wire mesh 208 is also cylindrical and nested within the conduit sleeve shaft 201 such that a relatively unobstructed fluid passage portion 218 is defined within an annular space between the inner wall 210 of the conduit sleeve shaft 201 and the wire mesh 208, and a catalyst material receiving space 216 is provided in the wire mesh 208. In these embodiments, the catalyst material containing fluid passage portion 216 is spaced radially outward from the axis of the conduit barrel shaft 201 relative to the relatively unobstructed fluid passage portion 218.

In some embodiments, spacer tubes 214 extend through the space defined by wire mesh 208 and facilitate the flow of the molten polymeric material of the reactor arrangement to the portion of tube shaft 201 that is closely configured to the heat transfer elements (see below). This embodiment helps to maintain the molten polymeric material of the reactor set at the desired temperature. Moreover, by taking up space, the spacer tubes 214 effectively reduce the volume of the module reaction zone 205, thereby increasing the velocity of the molten polymeric material of the flowing reactor arrangement.

In some embodiments, the spacer tube 214 extends longitudinally through the length of the conduit spool 201. In some embodiments, a catalyst material containment space 216 is defined within the annular space between the spacer tube 214 and the wire mesh 208.

The molten polymeric material of the reactor arrangement is received by the inlet 202A at the first end of the conduit spool 201 and is directed through the wire mesh 208 between the relatively unobstructed fluid passage portion 218 and the catalyst material receiving space 216 as it passes through the conduit spool 201 via the fluid passage 206 to the opposite end. This produces a molten product material comprising depolymerized reaction products (and, in some embodiments, unreacted molten polymer material and/or intermediate reaction products) that are discharged via an outlet 202B at the opposite second end of conduit spool 201. While being directed through catalyst material receiving space 216, the molten polymer material of the reactor arrangement is brought into contact with catalyst material 204, causing at least partial depolymerization of at least part of the molten polymer material of the reactor arrangement.

As shown in fig. 6 and 14, in some embodiments, the flow guides 222, 223 are disposed within the relatively unobstructed fluid passage portion 218. In some embodiments, the baffle 222 is welded to the end cap 212(a) and is in the form of a resilient wire that is wrapped around the wire mesh 208. In some embodiments, deflector 223 is in the form of a resilient wire that is pressed through the space between conduit spool 201 and wire mesh 208, welded to end cap 212(a), and biased against inner wall 210 of spool 201.

The flow guides 222, 223 promote mixing of the flowing reactor arrangement molten polymeric material and promote uniform distribution of heat and mitigate charring of the reactor arrangement molten polymeric material, which can lead to deposition of solid organic material on the structure defining the flow channel 206 and to fouling. The flow guides 222, 223 also promote flow of the reactor disposed molten polymeric material from the relatively unobstructed fluid passage portion 218 to the catalyst material containment space 216 and increase contact between the reactor disposed molten polymeric material and the catalyst material 204.

As shown in fig. 9-13, an end cap assembly 211 is provided and installed within the interior space of the conduit spool 201. The end cap assembly 211 includes rigid end caps 212(a) and 212(b), wire mesh 208, and spacer tubes 214. Cover 212(a) is disposed near one end of conduit spool 201, and end cover 212(b) is disposed near the opposite end of conduit spool 201. In some embodiments, end caps 212(a) and 212(b) are also permeable to the flow of molten polymeric material of the reactor arrangement.

Wire mesh 208 is disposed between end caps 212(a) and 212(b), and its axial positioning within conduit cartridge shaft 201 relative to conduit cartridge shaft 201 is determined by end caps 212(a) and 212 (b). One end of the wire mesh 208 is welded to the end cap 212(a), while the opposite end of the wire mesh 208 is disposed within a recess formed in the end cap 212(b), such that a catalyst material accommodating space 216 containing the catalyst material 204 is defined within the space bounded by the wire mesh 208 and the end caps 212(a) and 212 (b).

The spacer tube 214 is disposed between the end caps 212(a) and 212 (b). One end of the spacer tube 214 is welded to the end cap 212(a), while the opposite end of the spacer tube 214 is disposed within a recess formed in the end cap 212 (b).

As shown in fig. 11 and 12, end cap 212(a) is welded to conduit cartridge shaft 201 for connection of end cap assembly 211 to conduit cartridge shaft 201. In this regard, the end cap 212(a) includes a plurality of rigid end cap spacers 2120(a) to (c) that protrude radially outward from the end cap hub 2122 (the wire mesh 208 and spacer tube 214 are welded to the end cap hub 2122). The end cap spacers 2120(a) to (c) are received in corresponding recesses provided in the end cap hub 2122. The end cap spacers 2120(a) to (c) are spaced apart from each other such that fluid communication between reactor modules 200 connected to each other is allowed, and in particular between reaction zones of connected reactor modules 200. End cap spacers 2120(a) to (c) may be welded to the interior of conduit barrel shaft 201, thereby determining the position (a) of end cap 212 relative to conduit barrel shaft 201, and also the axial position of spacer tube 214 relative to conduit barrel shaft 201 (which is welded to end cap 212 (a)).

As shown in fig. 9-11, the positioning of the end cap 212(b) relative to the tube spool 201 is determined by placing the end cap 212(b) in contacting engagement with the tube spool 201, spacer tube 214, and through an adjacent tube structure, such as a welded end cap 212(a) or conduit of another reactor module 200. Each of the spacer tube 214 and the adjacent conduit structure is a relatively rigid structure such that the substantially fixed axial positioning of each of the spacer tube 214 and the adjacent conduit structure relative to the conduit barrel shaft 201 determines the axial positioning of the end cap 212(b) relative to the conduit barrel shaft 201. When the reactor module 200 is assembled, the end cap 212(b) is compressed between the spacer tube 214 and the adjacent tube structure (in the embodiment shown in fig. 8, the adjacent tube structure is the end cap 212(b) of another reactor module 200) such that the axial positioning of the end cap 212(b) relative to the tube spool shaft 201 (and thus the end cap 212(a)) is determined by the spacer tube 214 and the adjacent tube structure.

The end cap 212(b) also includes rigid end cap isolators 2124(a) through (c) that are disposed within corresponding recesses within the end cap hub 2126. The end cap hub includes a recess that receives the spacer tube 214 and the wire mesh 208. The end cap spacers 2124(a) to (c) are disposed in contacting engagement with the inner wall of the conduit barrel shaft 201. The end cap spacers 2124(a) to (c) protrude radially outward from the end cap hub 2126. The end cap spacers 2124(a) to (c) are spaced apart from each other so that fluid may flow between the reactor modules 200 connected to each other, and in particular between the reaction zones of the connected reactor modules 200. End cap spacers 2124(a) to (c) serve to substantially fix the vertical positioning of end cap 212(b) relative to conduit spool 201 when disposed in contacting engagement with the inner wall of conduit spool 201 and mated with spacer tube 214 and adjacent conduit structure.

By configuring end cap 212(b) such that end cap 212(b) is removable from end cap assembly 211, repair and maintenance within the reaction zone, including replacement of catalyst material 204, is facilitated.

A heater 220 is disposed in heat transfer communication with the fluid channel 206 to effect heating of the molten polymeric material flowing through the reactor arrangement of the fluid channel 206. Maintaining the molten polymeric material in the flowing reactor arrangement at a sufficient temperature results in at least partial depolymerization. In some embodiments, the heater 220 comprises an electrical heating tape mounted to an outer wall of the conduit spool 201 and configured to provide heat to the fluid channel 206 by means of heat transfer through the conduit spool 201.

Referring to fig. 16-18, in some embodiments, the reactor includes an inlet reactor module 300, an outlet reactor module 400, and optionally one or more intermediate reactor modules 500.

In some embodiments, the inlet reactor module 300 includes a duct cartridge shaft 301, the duct cartridge shaft 301 having opposing ends, a respective flange 330A, 330B being provided at each opposing end to facilitate connection with the outlet reactor module 400, and in some embodiments, with the intermediate reactor module 500.

The inlet reactor module 300 includes an inlet 302A at a first end of a conduit spool 301, an outlet 302B at an opposite second end of the spool, and a fluid passageway 306 extending between the inlet 302A and the outlet 302B. The fluid channel 306 comprises a catalyst material containment space 316 disposed within the molten polymer material permeable container 303 of the reactor arrangement, with the catalyst material 304 disposed within the catalyst material containment space 316. The catalyst material containment space 316 defines the module reaction zone 305 of the reactor module 300.

The inlet reactor module 300 is configured to receive molten polymer material of a reactor arrangement through the inlet 302A, direct the received molten polymer material through the fluid channel 306, and, when such directing is performed, contact the molten polymer material with the catalyst material 304 such that at least partial depolymerization of at least a portion of the molten polymer material is achieved, and such that a molten product material is produced that includes depolymerized reaction products (and, in some embodiments, unreacted molten polymer material and intermediate reaction products, or both), and to discharge the molten product material from the outlet 302B.

The fluid channel 306 includes a relatively unobstructed fluid channel portion 318 and a catalyst material containing fluid channel portion 315 containing a catalyst material containing space 316. A relatively unobstructed fluid passage portion 318 extends from the inlet 302A and is disposed in fluid communication with the catalyst material containing fluid passage portion 315 via the wire mesh 308. A fluid passage portion 315 containing catalyst material extends into the outlet 302B.

Wire mesh 308 is disposed within conduit barrel shaft 301 to divide fluid passageway 306 into a relatively unobstructed fluid passageway portion 318 and a fluid passageway portion 316 containing catalyst material. Wire mesh 308 is mounted at one end at and extends from a first end of conduit spool 301, and in some embodiments, wire mesh 308 is mounted at an opposite end to isolation tube 314 (see below). The wire mesh 308 contains the catalyst material 304 within the catalyst material receiving space 316. The wire mesh 308 is disposed in spaced relation to the inner wall 310 of the conduit barrel shaft 301 defining the fluid passageway and extends longitudinally through a portion of the conduit barrel shaft 301. The space between the wire mesh 308 and the inner wall 310 defines a portion of a fluid passage portion 315 containing catalyst material and extends longitudinally through a portion of the conduit shaft 301 to define a portion of a catalyst material containment space 316. In this regard, the relatively unobstructed fluid passage portion 318 extends longitudinally along the axis of conduit spool shaft 301 or near the axis of conduit spool shaft 301.

In some embodiments, wire mesh 308 is cylindrical in shape and is nested within conduit spool shaft 301. In this regard, in some embodiments, the fluid passage portion 315 containing the catalyst material is spaced radially outward from the axis of the conduit barrel shaft 301 relative to the relatively unobstructed fluid passage.

Fluid communication between the relatively unobstructed fluid passage portion 318 and the catalyst material containing fluid passage portion 315 is accomplished through the space within the wire mesh. In this regard, the wire mesh 308 is configured to allow molten polymer material to penetrate from the relatively unobstructed fluid passage portion 318 to the catalyst material-containing fluid passage portion 315 (thereby promoting contact of the molten polymer material with the catalyst material 304 in the reaction zone) while preventing or substantially preventing catalyst material 304 from flowing out of the catalyst material-containing space 316 to the relatively unobstructed fluid passage portion 318.

In some embodiments, at the downstream end of the relatively unobstructed fluid passage portion 318, the end wall is tapered to encourage molten polymer material to flow through the wire mesh 308 to the catalyst material receiving space, thereby reducing pooling of the molten polymer material.

The fluid passage portion 315 containing the catalyst material extends into an annular space defined between the spacer pipe 314 installed in the conduit cylinder shaft 301 and the inner wall 310 of the conduit cylinder shaft 301. By occupying this space, the spacer tubes 314 facilitate the flow of the reactor disposed molten polymeric material in the catalyst material containing fluid channel portion 315 to the portion of the conduit barrel shaft 301 that is closely disposed proximate the heat transfer elements, thereby maintaining the reactor disposed molten polymeric material at a desired temperature. Moreover, by taking up space, the spacer tubes 314 effectively reduce the volume of the modular reaction zone 305, thereby increasing the velocity of the molten polymeric material of the flowing reactor arrangement.

The molten polymer material of the reactor arrangement is received within the relatively unobstructed fluid passage portion 318 via the inlet 302A at the first end of the conduit barrel shaft 301 and is directed through the wire mesh 308 to the catalyst material receiving space 316 of the catalyst material receiving fluid passage portion 315 (see directional arrow 340). While being directed through catalyst material-containing fluid channel portion 315 (see directional arrow 342), the molten polymer material contacts catalyst material 304, producing a depolymerization reaction product, and the molten product material includes the depolymerization reaction product produced within catalyst material-containing fluid channel portion 315 (and, in some embodiments, unreacted molten polymer material and intermediate reaction products, or both), and is then discharged at an opposite second end of conduit barrel shaft 301 via outlet 302B.

In some embodiments, the outlet reactor module 400 includes a duct spool 401, the duct spool 401 having opposing ends, a flange provided at each of the opposing ends to facilitate connection with the inlet reactor module 300, and in some embodiments, one intermediate reactor module disposed between the inlet reactor module 300 and the outlet reactor module 400.

The outlet reactor module 400 includes an inlet 402A at a first end of the conduit spool 401, an outlet 402B at an opposite second end of the spool, and a fluid passage 406 extending between the inlet 402A and the outlet 402B. The fluid channel 406 includes a catalyst material containment space 416 disposed within the molten polymer material permeable container 403 of the reactor arrangement, with the catalyst material 404 disposed within the catalyst material containment space 416. The catalyst material containment space 416 defines a module reaction zone 405 of the reactor module 400.

The outlet reactor module 400 is configured to receive molten polymer material of the reactor arrangement through the inlet 402A, direct the received molten polymer material through the fluid channel 406, and, when such directing is performed, contact the catalyst material with the directed molten polymer material such that at least partial depolymerization of at least a portion of the molten polymer material is achieved and such that a molten product material is produced that includes depolymerized reaction products (and, in some embodiments, unreacted molten polymer material and intermediate reaction products or both), and to discharge the molten product material from the outlet 402B.

The fluid channel 406 includes a catalyst material containing fluid channel portion 415 and a relatively unobstructed fluid channel portion 418, the catalyst material containing fluid channel portion 415 including a catalyst material receiving space 416. A fluid passage portion 415 containing catalyst material extends from the inlet 402A and is disposed in fluid communication with a relatively unobstructed fluid passage portion 418 through the wire mesh 408. A relatively unobstructed fluid passage portion 418 extends into the outlet 402B.

In some embodiments, the spacer tubes 414 are mounted within the conduit barrel shaft 401 at a first end of the conduit barrel shaft 401 such that a space (e.g., an annular space) between the conduit barrel shaft 401 and the spacer tubes 414 defines a portion of the fluid channel portion 415 containing the catalyst material extending from the inlet 402A. By occupying this space, the spacer tubes 414 cause the molten polymer material of the reactor setting to flow within the fluid channel portion 415 containing the catalyst material to the portion of the conduit spool 401 closely positioned adjacent the heat transfer element (see below), thereby maintaining the molten polymer material of the reactor setting at a desired temperature. Moreover, by taking up space, the spacer tubes 414 effectively reduce the volume of the modular reaction zone 405, thereby increasing the velocity of the molten polymeric material of the flowing reactor arrangement.

A fluid passage portion 415 containing catalyst material extends into the annular space defined between the inner wall 410 of the conduit barrel shaft 401 and the wire mesh 408. Wire mesh 408 is disposed within conduit sleeve shaft 401 to divide fluid passageway 406 into a fluid passageway portion 415 containing catalyst material and a relatively unobstructed fluid passageway portion 418. Wire mesh 408 is mounted at one end at and extends from a second end of spool shaft 401, and wire mesh 308 is mounted at the opposite end to spacer tube 414. The wire mesh 408 contains the catalyst material 404 within the catalyst material accommodating space 416. The wire mesh 408 is disposed in spaced relation to an inner wall 410 of the conduit barrel shaft 401 defining a fluid passage and extends longitudinally through a portion of the conduit barrel shaft 401. The space between the wire mesh 408 and the inner wall 410 defines a portion of a fluid passage portion 415 containing the catalyst material and extends longitudinally through a portion of the conduit barrel shaft 401. In this regard, the relatively unobstructed fluid passage portion 418 extends longitudinally along the axis of the conduit spool 401 into the outlet 402B or into the outlet 402B proximate the axis of the conduit spool 401.

In some embodiments, the wire mesh 408 is cylindrical in shape and is nested within the conduit spool 401. In this regard, in some embodiments, the fluid channel portion 415 containing the catalyst material is spaced radially outward from the axis of the conduit barrel shaft 401 relative to the relatively unobstructed fluid channel portion 418.

Fluid communication between the catalyst material containing fluid passage portion 415 and the relatively unobstructed fluid passage portion 418 is achieved through the space within the wire mesh. In this regard, the wire mesh 408 is configured to allow molten polymer material to penetrate from the relatively unobstructed fluid passage portion 418 to the catalyst material containing fluid passage portion 415 (thereby promoting contact of the molten polymer material with the catalyst material 404 in the reaction zone) while preventing or substantially preventing the catalyst material 404 from flowing out of the catalyst material receiving space 416 to the relatively unobstructed fluid passage portion 418.

The molten polymer material of the reactor arrangement is received within the catalyst material containing fluid channel portion 415 via an inlet 402A at a first end of the conduit spool 401 (e.g., from the outlet 302B of the reactor module 300, or such as, for example, from an outlet of the intermediate reactor module 500, see below), is directed through the catalyst material containing fluid channel portion 415 (see directional arrow 440). When directed through the fluid channel portion 415 containing the catalyst material, the molten polymer material contacts the catalyst material 404 such that a molten product material is produced that includes depolymerization reaction products (and, in some embodiments, unreacted molten polymer material and intermediate reaction products, or both). The molten product material, including depolymerization products produced within the fluid passage portion 415 containing catalyst material, is directed through the wire mesh 408 to the relatively unobstructed fluid passage portion 418 (see directional arrow 442) and subsequently discharged at the opposite second end of the conduit spool shaft 401 via outlet 402B.

In some embodiments, the reactor includes one or more intermediate reactor modules 500 disposed between the inlet reactor module 300 and the outlet reactor module 400.

In some embodiments, the intermediate reactor module 500 includes a conduit spool 501 having opposite ends with flanges 530A, 530B provided at each of the opposite ends to facilitate connection with the reactor module. A flange is provided at the first end to facilitate connection with either the inlet reactor module 300 or another intermediate reactor module 500. A flange is provided at the second end to facilitate connection with either the outlet reactor module 400 or another intermediate reactor module 500.

The conduit cartridge shaft 501 includes an inlet 502A at a first end of the conduit cartridge shaft 501, an outlet 502B at an opposite second end of the conduit cartridge shaft 501, and a fluid passageway 506 extending between the inlet 502A and the outlet 502B. The fluid channel 506 includes a catalyst material receiving space 516. A catalyst material-containing space 516 is provided in the molten polymer material-permeable container 503 of the reactor arrangement, and the catalyst material 504 is provided in the catalyst material-containing space 516. The catalyst material receiving space 516 defines the module reaction zone 505 of the reactor module 500.

The intermediate reactor module 500 is configured for receiving molten polymer material of a reactor arrangement through the inlet 502A, directing the received molten polymer material through the fluid channel 506, and, while such directing is performed, contacting the catalyst material 504 with the directed molten polymer material, such that at least partial depolymerization of at least a portion of the molten polymer material is achieved, and such that a molten product material is produced that includes depolymerized reaction products (and, in some embodiments, unreacted molten polymer material and intermediate reaction products, or both), and discharging the molten product material from the outlet 502B.

The fluid channel 506 includes a catalyst material containing fluid channel portion 515 including a catalyst material containing space 516.

In some embodiments, spacer tubes 514 are mounted within conduit barrel shaft 501 at a first end of conduit barrel shaft 501 such that the space between conduit barrel shaft 501 and spacer tubes 514 defines catalyst material containment space 516. By occupying this space, the spacer tube facilitates the flow of the reactor-disposed molten polymer material within the catalyst material-containing fluid channel portion 515 to the portion of the conduit shaft 501 closely disposed proximate the heat transfer element (see below), thereby maintaining the reactor-disposed molten polymer material at a desired temperature. Moreover, by taking up space, the spacer tubes 514 effectively reduce the volume of the modular reaction zone 505, thereby increasing the velocity of the molten polymeric material in the flowing reactor arrangement.

Fig. 19 shows a cross-sectional side view of a catalytic reactor 700a having a removable static mixer 710 configured to be heated by a hot fluid and/or molten salt. Static mixer 710 provides greater mixing in catalytic reactor 700a and may result in the need for lower operating temperatures. In some embodiments, the static mixer 710 is removable, which allows for easier cleaning and maintenance of the reactor 700 a. The removable static mixer 710 also allows for the reuse of the reactor section. For example, a jacketed reactor may be switched to a preheating or cooling section.

The hot fluid and/or molten salt may be heated by natural gas, electricity, waste process heat, and coal, among other means. In some embodiments, the hot fluid and/or molten salt reduces the cost of having to use electricity.

The tubular configuration of catalytic reactor 700a provides several advantages in addition to those already mentioned above. In particular, the use of tubular reactors connected in series allows reliable and consistent parameters, which allows for consistent products. In particular, because the surface area and heat input of the catalyst is maximized, consistent flow through the tubular section produces a more predictable and narrower range of final product than using a continuously stirred reactor. One advantage compared to a continuous stirred reactor is that shortcuts (shortcuts) are eliminated or at least reduced, the flow in the tubular section supposedly moving as a plug. Each hypothetical plug spends the same amount of time in the reactor. The tubular catalytic reactor may be operated vertically, horizontally or at any angle in between. The tubular catalytic reactor (reactor section) and the corresponding preheating and cooling sections (see fig. 28-30) may be of a common size (or one of several standard sizes). This not only allows for a consistent flow of material, but also allows the tubular element to be designed to be interchangeable between sections and to be easily added, removed, cleaned and repaired. In at least some embodiments, the inner surface of the tubular section is made of 304 or 316 steel.

Hot fluid and/or molten salt may enter jacket 720 via inlet/outlet 730. In some embodiments, catalytic reactor 700a is configured to be fitted with a thermocouple/pressure sensor (not shown) and includes an associated notch 735. Notch 735 is used to bring the thermocouple/pressure sensor into physical contact with the fluid. In some embodiments, a thermocouple/pressure sensor will be installed in the well, which reduces the material between the fluid and the sensor.

In some embodiments, catalytic reactor 700a includes a removable wire mesh 760 that can hold catalyst. The removable wire mesh 760 is easily replaceable, overcoming the disadvantages associated with packed bed reactors that make maintenance requirements more complex and result in downtime. In some embodiments, normalization of the removable wire mesh 760 results in consistent product leaving each section and/or allows normalization in multiple reactors.

In other or the same embodiments, the catalytic reactor 700a may include a removable adapter 740, the removable adapter 740 having a cut-out for the static mixer support. The static mixer support reduces the force on the static mixer 710, allowing for more forceful/rapid removal. The cutouts of the adapter 740 improve the seal between the adapter and the wire mesh. Catalytic reactor 700a may include a flange 750 on one or both ends to connect catalytic reactor 700a to other reactors, extruders, and the like.

Fig. 20 is a cross-sectional side view of catalytic reactor 700b with removable static mixer 710 configured to use electrical heating. In some embodiments, electrical heating is preferred over the use of hot oil/molten salt because it can be more convenient, requires fewer ancillary equipment, such as boilers, heating vessels, high temperature pumps, valves and fittings, and is easier to operate. Further, in some embodiments, reducing electrical heating reduces the overall footprint of the system. In some embodiments, catalytic reactor 700b is configured to be fitted with a thermocouple/pressure sensor (not shown) and includes an associated notch 735.

In some embodiments, catalytic reactor 700b includes a removable wire mesh 760 that can hold catalyst. In other or the same embodiments, the catalytic reactor 700b may include a removable adapter 740, the removable adapter 740 having a cut-out for the static mixer support. Catalytic reactor 700b may include a flange 750 on one or both ends to connect catalytic reactor 700b to other reactors, extruders, and the like.

Fig. 21 is a cross-sectional side view showing catalytic reactor 700c having a removable annular insert 712 configured to be heated by a hot fluid and/or molten salt. The annular insert 712 may create an annular flow that may result in improved heat transfer, an increase in superficial velocity, and is easier to maintain than a hollow reactor.

Hot fluid and/or molten salt may enter jacket 720 via inlet/outlet 730. In some embodiments, catalytic reactor 700c is configured to be fitted with a thermocouple/pressure sensor (not shown) and includes an associated notch 735.

In some embodiments, catalytic reactor 700c includes a removable wire mesh 760 that can hold catalyst. In other or the same embodiments, the catalytic reactor 700c may include a removable adapter 740, the removable adapter 740 having cutouts for the removable annular and wire mesh supports. Catalytic reactor 700c may include a flange 750 on one or both ends to connect catalytic reactor 700c to other reactors, extruders, and the like.

Fig. 22 is a cross-sectional side view of catalytic reactor 700d, catalytic reactor 700d having a removable annular insert 712 configured to use electrical heating. In some embodiments, catalytic reactor 700d is configured to be fitted with a thermocouple/pressure sensor (not shown) and includes an associated notch 735.

In some embodiments, catalytic reactor 700d includes a removable wire mesh 760 that can hold catalyst. In other or the same embodiments, the catalytic reactor 700d may include a removable adapter 740, the removable adapter 740 having cutouts for the removable annular and wire mesh supports. Catalytic reactor 700d may include a flange 750 on one or both ends to connect catalytic reactor 700d to other reactors, extruders, and the like.

Fig. 23 is a cross-sectional side view of a catalytic reactor 700e having hollow internals configured to be heated by a hot fluid and/or molten salt. A reactor with hollow internals can increase the residence time a given material spends in reactor 700e, which reduces the number of reactors needed to make a particular product and the volume of catalyst that can be used. Reactors with hollow internals can also be produced more economically than reactors with static mixers. Hot fluid and/or molten salt may enter jacket 720 via inlet/outlet 730. In some embodiments, catalytic reactor 700e is configured to be fitted with a thermocouple/pressure sensor (not shown) and includes an associated notch 735.

In some embodiments, catalytic reactor 700e includes a removable mesh 760 that can hold catalyst. In other or the same embodiments, the catalytic reactor 700e may include a removable adapter 740, the removable adapter 740 having a cutout for the removable wire mesh support. Catalytic reactor 700e may include a flange 750 on one or both ends to connect catalytic reactor 700e to other reactors, extruders, and the like.

Fig. 24 is a cross-sectional side view of a catalytic reactor 700f having hollow internals configured to be heated using electricity. In some embodiments, catalytic reactor 700f is configured to be fitted with a thermocouple/pressure sensor (not shown) and includes an associated notch 735.

In some embodiments, catalytic reactor 700f includes a removable wire mesh 760 that can hold catalyst. In other or the same embodiments, the catalytic reactor 700f may include a removable adapter 740, the removable adapter 740 having a cut-out for the wire mesh support. Catalytic reactor 700f may include a flange 750 on one or both ends to connect catalytic reactor 700f to other reactors, extruders, and the like.

Fig. 25 is a cross-sectional elevation view of a group of catalytic reactors 700, as shown in fig. 19, arranged in parallel. The parallel arrangement shown in fig. 25 allows the overall production rate to be increased/decreased more easily as desired, with minimal changes to the overall plant, and allows multiple different levels of depolymerization to occur at one time.

Housing 800 allows catalytic reactor 700 to be soaked in hot oil/molten salt, which is generally more efficient than electricity. Hot oil/molten salt is held in chamber 780. In some embodiments, the flange 770 allows multiple housings to be connected together.

FIG. 26 is a cross-sectional side view of the parallel catalytic reactor device of FIG. 25 shown in a horizontal configuration. Parallel arrangements allow the construction of higher flow units with smaller pressure drops, which may cause problems, than single tube arrangements. The horizontal configuration is generally more convenient for operation/maintenance.

FIG. 27 is a cross-sectional side view of the parallel catalytic reactor device of FIG. 25 shown in a vertical configuration. The vertical configuration may reduce stratification of the liquid/gas product and may eliminate or at least reduce the need for a static mixer.

FIG. 28 is a cross-sectional side view of a vertical spiral internal catalytic reactor device 900A having two reactors 700A shown in FIG. 19 connected in series. The horizontal helical mixer preheating section 820 is connected to one reactor 700 a. The helical mixer can achieve better mixing by avoiding stagnation and hot spots.

The helical mixer cooling section 830 is shown connected to another reactor 700a at a 45 degree fall. The fall allows the product to flow by gravity, while the 45 degree angle allows for sufficient contact between the cooling medium and the product.

In the illustrated embodiment, the vertical spiral internal catalytic reactor device 900A has several inlets/outlets to allow for the use of a hot fluid/molten salt mixture, although other heating techniques (such as, but not limited to, electrical heating) may also be used.

FIG. 29 is a cross-sectional side view of a vertical loop catalytic reactor device 900B having two reactors 700c as shown in FIG. 21 connected in series.

FIG. 30 is a cross-sectional side view of a vertical catalytic reactor device 900C having two hollow reactors 700f as shown in FIG. 23 connected in series.

Fig. 31 is a perspective view of a horizontal reactor configuration 910 having an internal helical reactor 700b configured to use an electric heater 870 similar to that shown in fig. 20. In fig. 31, the reactor housing has been removed from a portion of the horizontal reactor configuration 910 to aid in viewing the position of the internal screw reactor 700 b.

While particular elements, embodiments and applications of the present invention have been shown and described, it will be understood, of course, that the invention is not limited thereto since changes may be made in the details, particularly in light of the foregoing teachings, without departing from the scope of the disclosure. For example, many of the embodiments show that different combinations of components are possible within the scope of the claimed invention, and the described embodiments are illustrative and other combinations of the same or similar components can be used in substantially the same way to achieve substantially the same results. Furthermore, all claims are hereby incorporated by reference to the description of the preferred embodiments.