Electrochemistry produces polymers

Abstract

To provide a reactor for electrochemical reactions.SOLUTION: The invention consists of device, addition polymerization, condensation polymerization, process with piping, control and procedure. The device is a mechanical design to continuously remove solid deposit, conductive or not, on electrode surface. Besides overcoming the limitation of electrochemical polymer production where the products block the electrode from further operation, the device provides cheaper operation for electrometallurgy to harvest the valuable metals formed on electrode. The novel process allows retrofitting conventional polymer production process by replacing conventional reactor with electrochemical reactor, for low-cost rapid implementation. The novel reactions consist of addition reaction to produce polymers; and intermolecular reaction to produce classes of condensation polymers.SELECTED DRAWING: Figure 7

Description

[Technical Field]

[0001] Its technical field is mainly related to the production methods of polymers and chemical compounds. Specifically, it consists of the design of electrochemical equipment, polymerization, superposition and synergistic chemical processes, specific process implementation, process control methods and operation flow. [Background technology]

[0002] Regular 1-8 polymer production involves mixing reactants 1-6 and sending them to a conventional reactor 1-2. The reaction occurs via the application of high heat energy 1-11 and pressure 1-12, as shown in Figure 1. The 1-8 polymer forms as a solid suspension and is separated from the liquid phase, washed, and further refined 1-4. The remaining reagents are then reduced to valuable by-products. For example, in the continuous production of polypropyl esters (PLEs), lactic acid [1] uses the 1-13 catalyst to polymerize and bond with the carrier, removing water or solvent. Meanwhile, polyethylene production [2] uses the 1-13 catalyst, composed of aluminum and transition metal compounds, to produce 1-8 polymer in a polymerization reactor, followed by the polymer and solvent reduction system.

[0003] Design flaws typically associated with polymer production (1-8), however, include the need for high thermal energy (1-11) and pressure (1-12), often associated with the use of hazardous reagents such as 6-3 photocatalysts and expensive catalysts (1-13). For example, the 1-8 polymer production process [3] uses heat to drive the polymerization of aromatic dicarboxylic acids, such as diethyl ether (2,2-di(4-hydroxyphenyl)propane) (also known as 6-2 bisphenol A) and acetate esters (hydroxybenzoates). This is remedied because the aggregated reaction is not fundamentally energy-intensive. Regarding typical polymerization reaction kinetics, as shown in Figure 2, the reaction rate is primarily limited by the kinetic bottleneck (2-1). Due to the high thermal energy (1-11) and pressure (1-12), the remaining reaction steps involve the propagation step (2-2) and the completion step (2-3), all of which occur rapidly, resulting in significantly lower energy demands.

[0004] Additionally, the polymerization reaction is driven by electricity (3-1) rather than thermal energy (1-11). This alternative electrochemical reaction involves connecting a power source to the electrodes (1-7) in the electrolyte (Figure 3). This 1-7 electrolyte is typically a conductive liquid mixture containing 1-6 reactants, which may be ionic (6-6) or conductive (30-6) membranes immersed in the liquid mixture containing 1-6 reactants. These electrodes act as conductive materials, providing electrical current for the chemical reaction to occur at their surfaces. The electrode connected to the positive end of the power source, called 3-2, is the anode where the oxidation reaction occurs, while the electrode connected to the negative end of the power source, called 3-1, is the cathode where the reduction reaction occurs. Although not required for the reaction, a third electrode, called 3-4, is always included to provide voltage measurement at the 3-4 electrode.

[0005] During electrochemical reactions, solid products tend to adhere to the electrode surface, forming solid deposits (3-5). Solid removal is typically required to maintain the performance of electrochemical devices. Solid removal is of interest in electrochemical metallurgy and battery applications, where the metal formation is related to the electrode. Solid deposits on the electrode require further recovery and separation (1-4 processing). For metal products, solid deposits can typically be removed manually. Some machine-arm systems [4] have also been designed to remove metal deposits (3-5) from the cathode (3-3), mimicking the movements of a human arm, particularly in the mining industry and electrical plants. Solid removal can also be mechanically stripped into large sheets of deposits, which can be used on production lines to recover zinc [5] during metal recovery.

[0006] However, electrochemical polymerization is limited to a few ionic conductive polymers, such as polypyrrole and polythiophene. For example, polypyrrole or its derivatives can be produced electrochemically [6] by depositing the self-monomer 6-6 in the presence of conductive ions, such as 68-3 salt, and connecting it to a power source. A similar analogue, electrochemically producing polythiophene or its derivatives [7], is particularly cost-effective and energy-saving. Fundamentally, 1-8 polymers produced electrochemically are limited to a few types. 1-8 polymers must have unsaturated bonds to provide conductivity, such as aromatic rings and double or triple bonds, as shown in Table 1:

[0007] [Table 1]

[0008] This is because a similar intermittent electrode stripping method is used for conductive metal deposition. If it doesn't work, a 3-5 solid deposit forms (either the 3-2 anode or 3-3 cathode, depending on the reverse response). This solid deposit blocks the electrode surface, and the electrochemical reaction stops due to the lack of conductivity. As a result, other electrochemical methods that produce non-conductive 1-8 polymers have not received much attention, and most current 1-8 polymers, such as polyethylene, are not conductive. Fortunately, this fundamental limitation has been overcome with a new, simple, and elegant design: the 7-1 device, which removes the 1-8 polymer from the electrode, eliminating the continuity, as shown in Figure 4. This new 7-1 device opens the door to producing non-conductive 1-8 polymers through electrochemical methods, and a potential commercial model has emerged for 1-8 polymer production and the value-added 5-2 chemical waste, as shown in Figure 5. This is because electrochemical polymerization is permitted for the use of 5-3 commodity chemicals, which can react with some types of 5-2 waste chemicals to produce valuable 1-8 polymers and secondary 5-5 raw material chemicals, such as fuels, rather than costly disposal. A more complete, yet unlisted list of 5-3 commodity chemicals will be covered in the next chapter. Some examples include, but are not limited to, possible 5-2 waste chemicals and 5-3 commodity chemicals.

[0009] 1. Waste sludge / solvent (toxic) Ethylene glycol Propyl glycol

[0010] 2. Petrochemical waste (toxic) Halogen and alcohol

[0011] 3. Common waste / raw materials ·6-1 urea

[0012] 4.Biomass ·ethanol Electrochemical methods also offer many advantages over conventional methods, which are limited to polymer production, including 1-8, as shown in the example in Figure 6. More gentle 1-11 heat energy and 1-12 pressure reduce costs (capital costs are used for these equipment and operating costs are used for energy input) · Lower dependency on 1-13 catalysts is generally expensive and has an environmental impact. Integrate existing renewable energy sources to drive the reaction rather than fossil fuels. 1-4 processing compatible with downstream polymers. This allows for quick and easy implementation since the product is the same. A normal factory can be acquired and only one 1-2 normal reactors can be converted to 35-1 electrochemical reactors, rather than a redesigned / rebuilt system. Hobby 1-8 Solid removal can earn income through opportunities provided by the metallurgical industry 1-4 Permit

[0013] More importantly, using electrochemical methods to reduce reactive and dangerous / toxic 5-3 commodity chemicals also has negative environmental impacts. For example, expensive and toxic 6-3 gas is commonly used in 6-7 polycarbonate production, and the corrosive 6-8 hydrogen chloride and 6-9 ammonia are relatively harmless and can fetch high selling prices. [Prior art documents] [Patent documents]

[0014] [Patent Document 1] U.S. Patent No. 5,357,035 [Patent Document 2] U.S. Patent No. 3,300,458 [Patent Document 3] U.S. Patent No. 4,075,173 [Patent Document 4] US Patent No. 2007 / 0144894 [Patent Document 5] U.S. Patent No. 3,501,385 [Patent Document 6] U.S. Patent No. 4,547,270 [Patent Document 7] U.S. Patent No. 4,986,886 Summary of the Invention [Means for solving the problem]

[0015] As shown in Figure 7, this invention relates to the electrochemical production of polymers 1-8, which are related to the main elements: 7-1 equipment, 7-2 chemistry, 7-3 polymer addition, 7-4 condensation polymer, 7-5 process, 7-8 process, 7-6 pipeline and 7-7 control.

[0016] The 7-1 device is a new design, the 9-8 solids removal device, which can continuously remove 3-5 solid deposits formed on electrodes, regardless of conductivity. 3-5 solid deposits are removed on a continuous basis, without the need for electrodes, using a periodic / circular movement to contact the electrode surface. While many other configurations are possible, the four main variations are the 9-1 column electrode, 9-2 belt electrode, 9-3 rotating disk electrode, and 9-4 helical / screw electrode. It also involves the use of the 7-1 device, which includes a top lift function, the 9-7 movement transmission, the 9-13 stay, and the 9-9 solids transport.

[0017] When 7-3 polymers are added, an electrochemical additive reaction occurs without the formation of by-products. For example, in 1-8 polymers containing some 7-3 polymers, the main chain is mostly carbon atoms (typically polyethylene 1-8 polymers include polyethylene, polystyrene, and polyvinyl chloride). In some embodiments, the polymerization reaction forms olefins by intramolecular elimination, which then react in situ (in the reagents) to form the polymerized product. In homogeneous variants, only one type of initial raw material is used, or in copolymers, different initial raw materials may be mixed together to prepare 1-8 polymers with more complex structures.

[0018] 7-4 condensation polymers undergo self-electrochemical condensation reactions. For example, some 7-4 condensation polymers contain 1-8 polymers whose main chains contain oxygen atoms (polyethers and 33-8 polyesters) or nitrogen atoms (polyamides such as 33-9 proteins and nylons). This involves intermolecular elimination, ultimately bonding the ends of the monomer molecules. This primarily involves condensation, although more complex condensation and / or exchange reactions can occur when exchanged with esters. 1-8 polymers can also form long chains by extending open loops to cyclic monomer molecules.

[0019] The process outlines a general-purpose electrochemical production process in an industrial environment (34-1 Concept and 34-5 Block Flowchart). Auxiliary polymer processing equipment may be designed to combine with 35-1 electrochemical reactors; this process can also be extended to 34-3 by modifying existing conventional 1-8 polymer production processes through the design of electrochemical 7-1 equipment, combining with existing auxiliary 1-8 polymer processing equipment, and replacing the existing 1-2 conventional reactor unit. In some cases, the chemical recovery unit 1-5 can be replaced with a simpler version (34-2 Recycling), provided the chemical by-products are not more hazardous.

[0020] 7-6 Pipelines are related to the implementation of specific industrial processes, including 40-1 Process Flow Diagram and Auxiliary Units, 40-2 Pipeline Types, 40-3 Pumps / Compressors, 40-4 Heaters / Coolers, 40-5 Facilities, and 40-6 Valves, which facilitate industrial implementation. The process flow and the connected units are further detailed to establish and implement more than just a part of the process, such as a tank.

[0021] 7-7 control consists of indicators, controllers, and control strategies to maintain continuous operation of the 7-7 process. This includes combining 48-2 feedforward, 48-3 feedback, 48-4 scaling, 48-5 time course, 48-6 override selection, and 48-7 indicator / alarm process control methods to ensure the process is protected from disturbances. In some embodiments, 7-7 control is designed so that any disturbances eventually move to a level, allowing for a high tolerance.

[0022] 7-8 provides operational technology for the planned 59-2 configuration of the 7-1 equipment, which is fast and reliable. This modularization includes stacking 59-1 of the electrochemical reactors and raw material allocation. 59-2 configuration 35-1 excludes the electrochemical reactors, which provides the processes described in 34-3, modification, 59-3 maintenance, and 34-4 scrap management.

[0023] Finally, the industrial production process involves the joint use of the above elements and combinations thereof. [Brief explanation of the drawings]

[0024] [Figure 1] Conventional polymer production processes and conventional reactors are key components. [Figure 2] Conventional chemical processes explain why high temperatures and pressures are required to generate free radicals and initiate reactions. [Figure 3] FIG. 1 illustrates a laboratory scale electrochemical polymerization or any general electrochemical reaction that produces a solid deposit. [Figure 4] Principle of continuous solids removal [Figure 5] About elerGreen Industries, a universal chemical business model [Figure 6] The advantages associated with the new electrochemical process are presented. [Figure 7] A particular feature of the invention is the ElerGreen process. [Figure 8] It shows a diagram of the reading process. [Figure 9] The details are about modifications to the design of new electrochemical devices. [Figure 10] Basic operating principle of solid removal (column electrode) [Figure 11] Unitary element electrochemical reactor (columnar electrode) [Figure 12] Basic operating principles for solid removal (conveyor electrode) [Figure 13] The identity elements in Figure 13 relate to the electrochemical reactor (belt electrode). [Figure 14] Basic Operating Principles for Solid Removal (Rotating Disk Electrode) [Figure 15] Electrochemical reactor (rotating disk electrode) of unitary element [Figure 16] Basic operating principles for solid removal (spiral / screw electrode) [Figure 17] Electrochemical reactor of unitary element (spiral / screw electrode) [Figure 18] About the details device [Figure 19] Movement Generation [Figure 20] exercise denron [Figure 21] Solids Removal and Conveyance [Figure 22] reaction vessel [Figure 23] Stay [Figure 24] Gas removal device [Figure 25] Stack the solid removal device as shown in Figure 25. [Figure 26] Brush [Figure 27] Waxing [Figure 28] Figure 28 Variant Transports Solids About Drain / Channel [Figure 29] Specifics of electrochemical production plus polymers [Figure 30] The variant of Figure 30 is for conductive ions. [Figure 31]Variants for co-solvents [Figure 32] About the additives [Figure 33] The details concern the main possibilities of electrochemical production of condensation polymers. [Figure 34] For details, please refer to the collaboration process. [Figure 35] In the general-purpose variant, for the production process of a new electrochemical polymer, the traditional chemical reactor is replaced by an electrochemical reactor, and the by-products are recovered by a similar recovery unit. [Figure 36] The new electrochemical polymer production process variants are designed for when recovery units are not required and the by-products are easy to handle. [Figure 37] Kaizo features [Figure 38] waste management [Figure 39] General Block Flow Diagram [Figure 40] Regarding the detailed pipeline [Figure 41] Process flow diagram for industrial implementation [Figure 42] Normal reactor route [Figure 43] Electrochemical reactor pathway [Figure 44] Solvent Extraction Route [Figure 45] Absorption pathway [Figure 46] Figure 46 by-product is low key [Figure 47] By-products are high-key [Figure 48] Detailed process control [Figure 49] Detailed Pipeline and Instrumentation Diagram (P&ID) for the electrochemical polymer production process [Figure 50] About P&ID [Figure 51] Serial level control example [Figure 52] Feedforward Example [Figure 53] Feedback example [Figure 54] Proportional control example [Figure 55] Subroutine control example [Figure 56] Figure 56 describes the shunt control interlock [Figure 57] Override selection control example [Figure 58] Indicator and alarm examples [Figure 59] Detailed operation flow [Figure 60] Stack Electrode [Figure 61] Stack element (2x1) [Figure 62] Stack element (2x2) [Figure 63] Stack element (2xn) [Figure 64] Example of stacking layout elements [Figure 65] Stack elements (2xn) stacked and facing outwards [Figure 66] Stack element (nxn), suspension electrode [Figure 67] This is related to the placement flow element in Figure 67. [Figure 68] Experimental setup gas flow rate measurement [Figure 69] Experimental setup for degassing rate measurement [Figure 70] Sample observation [Figure 71] Product Authentication [Figure 72] Conversion rate is for integrated charge [Figure 73] Shows Moore's response to integrated charge [Figure 74] The current is [Figure 75] Gas Flow Rate vs. Current DETAILED DESCRIPTION OF THE INVENTION

[0025] 1.Chemical terms This electrochemical polymerization reaction can be expressed as Equation 1 via the following general equation:

[0026]

number

[0027] Before describing the invention in further detail, some symbols are outlined in Table 2 as terms in later sections.

[0028] [Table 2]

[0029] First, the substituents are represented as wave-like curves of chemical bonds and band numbers, which are simply index numbers of the substituents.

[0030] The carbon backbone, either aliphatic (alkyl) or aromatic (aromatic group), is represented as any applicable adjacent chemical bond, where n is simply the index number of the carbon backbone group.

[0031] The backbone outside of the substituent removal carbon is usually the active site for the reaction and will be represented as any applicable adjacent chemical bond.

[0032] For simplicity's sake, ion conduction refers to any substance that provides mobile ions for electrical conduction, including salts (sodium chloride / table salt), organic salts (sodium palmitate / common soap), ionizable molecules (hydrochloric acid), or ion exchange membranes. They are used in electrochemical systems to provide conductivity to facilitate electrochemical reactions. The commonly used 68-3 soluble salt for industrial ion conduction can be a 30-5 inorganic salt, such as sodium chloride (table salt), or a 30-4 organic salt (sodium palmitate), depending on the polarity of the system.

[0033] Finally, the number 1-8 is used in parenthetical subscripts in many chemical equations to simply represent the number of repeating units in a polymer. This can range from 1 (simple molecule) to large numbers, ranging from 1 to tens of thousands or more.

[0034] 2. Diagram Labels Labels are set in the drawing based on their order to appear first in the drawing.

[0035] 1. Figure 1. Conventional polymer production process and conventional reactor are key components. 1-1 Preparation 1-2 Conventional reactor 1-3 Solid separation 1-4 Finishing 1-5 Recovery 1-6 Reactants 1-7 Electrolytes 1-8 Polymers 1-9 Clean Polymer 1-10 Polymer products 1-11 Thermal energy 1-12 Pressure 1-13 Catalyst 1-14 Waste electrolyte 1-15 By-products

[0036] 2. Figure 2 Explains why conventional chemical processes require high temperatures and pressures to generate free radicals and initiate reactions. 2-1 Start 2-2 Propagation procedure 2-3 Steps completed

[0037] 3. Figure 3. Diagram of laboratory-scale electrochemical polymerization, or any general-purpose electrochemical reaction, producing a solid deposit. 3-1 Electricity 3-2 Positive pole 3-3 Cathode 3-4 Reference electrode 3-5 Solid deposits

[0038] 4. Figure 4 Principle of continuous solid removal 4-1 Dynamic electrodes 4-2 Removal device

[0039] 5. Figure 5 Universal Chemical Business Model for ElerGreen Industries 5-1 ElerGreen Process 5-2 Chemical waste 5-3 Commodity chemicals 5-4 Renewable Energy 5-5 Raw material chemicals

[0040] 6. Figure 6 illustrates the advantages associated with the new electrochemical process. 6-1 Urea 6-2 Phenol A 6-3 Energy of Light 6-4 Permit 6-5 Applied voltage 6-6 Conduction Ions 6-7 Polycarbonate 6-8 Hydrogen Chloride 6-9 Ammonia

[0041] 7. Figure 7. Specific features of the invention are the ElerGreen process 7-1 Equipment 7-2 Chemistry 7-3 Adding polymer 7-4 Condensation polymers 7-5 Process 7-6 Pipeline 7-7 Control 7-8 Process

[0042] 8. Figure 8 shows a diagram of the reading process. 8-1 Can supply A 8-2 Stream 1 A 8-3 Control valve V-01 A 8-4 Rate Indicator 01 A 8-5 Rate Indicator Controller 01 A

[0043] 9. Figure 9 Details of the transformation into new electrochemical device designs 9-1 Column electrode 9-2 Belt electrode 9-3 Rotating disk electrode 9-4 Spiral / Screw Electrode 9-5 Machinery 9-6 Motion generation 9-7 Motion Transmission 9-8 Solid removal 9-9 Solid transportation 9-10 sheets 9-11 Conveyor Channels 9-12 9-13 Stay 9-14 Movable 9-15 Built-in 9-16 Parts 9-17 Gas Removal 9-18 Brush 9-19 Waxing 9-20 Container

[0044] 10. Figure 10 Basic operating principle for solid removal (column electrode) 10-1 Counter electrode

[0045] 11. Regarding the identity element in Figure 11, electrochemical reactor (columnar electrode)

[0046] 12.Basic Operating Principles for Solid Removal (Conveyor Electrode) 12-1 Slide

[0047] 13. The identity elements in Figure 13 are for the electrochemical reactor (belt electrode)

[0048] 14. Basic operating principle of Figure 14 Solid removal (rotating disk electrode)

[0049] 15. The identity elements in Figure 15 are for an electrochemical reactor (rotating disk electrode)

[0050] 16. Figure 16 Basic operating principle for solid removal (spiral / screw electrode)

[0051] 17. Electrochemical reactor (spiral / screw electrodes) for the identity element in Figure 17

[0052] 18. Figure 18 Details device

[0053] 19. Figure 19. Motion generation 19-1 Motor / Engine 19-2 Gears 19-3 Axis

[0054] 20. Figure 20 Motion transmission 20-1 Chain drive

[0055] 21. Figure 21 Solid removal and solid transport 21-1 Baffle 21-2 Detergent 21-3 Blade adjustment 21-4 Detergent inlet 21-5 Detergent outlet

[0056] 22. Figure 22 Reaction vessel 22-1 Electrolyte inlet 22-2 Electrolyte outlet 22-3 Side window

[0057] 23. Figure 23 Stay 23-1 Hydraulic Top 23-2 Arms 23-3 wheel 23-4 Housing

[0058] 24. Figure 24 Gas removal device 24-1 Ventilation hole 24-2 Hat 24-3 Cover 24-4 Heavy objects 24-5 Sleeve (Washing Tube) 24-6 Sleeve (Tank Tube) 24-7 Sleeve (electrode frame)

[0059] 25. Stacking solids removal equipment in Figure 25

[0060] 26. Figure 26 Brush 26-1 Accessory Stay

[0061] 27. Figure 27 Waxing 27-1 Wax layer

[0062] 28. The variant in Figure 28 transports solids about a draw / channel 28-1 radians (standard) 28-2 Rectangular 9-12 Channel 28-3 Triangle 9-12 Channel 28-4 Right-angle baffle (default) 28-5 Acute angle baffle 28-6 Obtuse angle baffle

[0063] 29. Figure 29 Details of electrochemical production plus polymers. 29-1 Homogeneous material 29-2 Copolymer 29-3 Alcohol group 29-4 Variant

[0064] 30. The variant of Figure 30 is about conductive ions. 30-1 Dissolved ions 30-2 Metal 30-3 Non-metals 30-4 organic 30-5 Inorganic 30-6 Membrane

[0065] 31. Figure 31 Variants for cosolvents 31-1 Co-solvent 31-2 Design molecules 31-3 Crowned Ether 31-4 Solvents

[0066] 32. Figure 32. About the variable additives 32-1 Additives 32-2 Oxidation-reduction 32-3 Other

[0067] 33. Figure 33 Details of the main possibilities for electrochemical production of condensation polymers 33-1 Indentation 33-2 Polyether 33-3 Simple alcohols: furans and phenolic resins 33-4 Cellulose 33-5 Polysulfides 33-6 Polyamines 33-7 Transesterification 33-8 Polyester 33-9 Polyamide 33-10 Creatinine 33-11 Polyimide 33-12 Urethane 33-13 Ring opening 33-14 Miscellaneous atoms: polysilicon, polysulfone, polyphosphinate, polynitrate 33-15 Polysilicone 33-16 Polysulfone

[0068] 34. The details in Figure 34 are related to the collaboration process. 34-1 Concept 34-2 Recycling 34-3 Kaizo 34-4 Scrap Management 34-5 Block Flowchart

[0069] 35. Figure 35. A general variant of the new electrochemical polymer production process in which the conventional chemical reactor is replaced by an electrochemical reactor, and the by-products will be recovered by a similar recovery unit. 35-1 Electrochemical reactor

[0070] 36. Figure 36 shows a variant of the production process of a new electrochemical polymer, where the recovery unit is not required and by-products are more easily processed. 36-1 Emissions

[0071] 37.Figure 37 Renovation features 37-1 Akiji 34-4 Waste management

[0072] 38. Figure 38 Waste Management 38-1 Scrap Extraction

[0073] 39. Generalized block flow diagram in Figure 39

[0074] 40. Figure 40: Detailed Pipeline 40-1 Process flow diagram and auxiliary units 40-2 Pipeline type 40-3 Pump / Compressor 40-4 Heating machine / cooling machine 40-5 Facilities 40-6 Valve

[0075] 41. The generic process flow chart in Figure 41 is for industrial implementation.

[0076] 42. Figure 42 Typical reactor path 42-1 Conventional reacting flow 42-2 Conventional solid flow 42-3 Normal Mixture Flow

[0077] 43. Figure 43 Electrochemical reactor pathway 43-1 Electrochemical reaction flow 43-2 Electrochemical Solid Flow 43-3 Electrochemical Hybrid Logistics

[0078] 44. Figure 44 Solvent extraction pathway 44-1 Solvent extraction

[0079] 45. Figure 45 Absorption pathway 45-1 Suction current

[0080] 46. ​​The by-product of Figure 46 is low key 46-1 Top-Tank Flow 46-2 Bottom - Solvent Stream

[0081] 47. Figure 47 By-products are high key 47-1 Top-solvent flow 47-2 Bottom-tank flow

[0082] 48. Figure 48 Detailed process control 48-1 in series 48-2 Feedforward 48-3 Feedback 48-4 scale 48-5 minutes distance 48-6 Override Selection 48-7 Indicators / Alarms 48-8 Quick Response 48-9 Accuracy 48-10 Reliability 48-11 times 48-12 Different responses required 48-13 Flexibility and Safety 48-14 Stem Storage

[0083] 49. Figure 49 Detailed Pipeline and Instrument Diagram (P&ID) for the Electrochemical Polymer Production Process

[0084] 50. Figure 50 Figure Notes P&ID

[0085] 51. Figure 51 Serial level control example

[0086] 52. Figure 52 Example of feedforward

[0087] 53. Feedback Examples

[0088] 54. Example of proportional control in Fig. 54

[0089] 55. Figure 55 Example of shunt control

[0090] 56. Figure 56 illustrates the shunt control interlock.

[0091] 57. Figure 57 Example of override selection control

[0092] 58. Figure 58 Example of indicators and alarms

[0093] 59. Figure 59 Operation flow of details 59-1 stack 59-2 Department 59-3 Maintenance

[0094] 60. Figure 60 Stack electrode 60-1 substitution 60-2 sets 60-3 Insulator 60-4 Circuit / Electricity Connection

[0095] 61. Figure 61 Stack element (2x1) 61-1 Personnel 61-2 Monitor side 61-3 Maintenance side 61-4 Stack side

[0096] 62. Figure 62 Stack element (2x2)

[0097] 63. Figure 63 Stack element (2xn)

[0098] 64. Figure 64 shows an example of stacking layout elements.

[0099] 65. Figure 65 shows how elements (2xn) are stacked and oriented outwards.

[0100] 66. Figure 66 Stack element (nxn), suspension electrode 66-1 Surrounded Units

[0101] 67. The placement flow in Figure 67 is for elements. 67-1 Configuration reactor vessel 67-2 Electrode placement stay 67-3 Adjusting the electrode position 67-4 Arrangement solid transportation 67-5 Installation gas removal

[0102] 68. Figure 68 Experimental setup Gas flow rate measurement 68-1 Material A 68-2 Material B 68-3 Dissolved Salts 68-4 with heating plate mixer 68-5 Magnetic Mixer 68-6 Tapered Bin 68-7 Bubble Flow Meter 68-8 stopper 68-9 Pipe 68-10 Initial Flag 68-11 Subsequent Marker

[0103] 69. Figure 69 Experimental setup for degassing rate measurement 69-1 Beaker

[0104] 70. Figure 70 Sample observation 70-1 Work electrode 70-2 Liquid Polymer 70-3 Bubbles

[0105] 71. Figure 71 Product Authentication

[0106] 72. The conversion rate in Figure 72 is

[0107] 73. Figure 73 shows Moore's response to an integrated charge.

[0108] 74. The current in Figure 74 is

[0109] 75. Figure 75 Gas flow rate vs. current

[0110] 3. Project drawing symbols Symbols are also used in process diagrams, especially process flow diagrams (PFDs) and piping and instrumentation diagrams (P&IDs). First, we will show multiple devices as codes in Table 3.

[0111] [Table 3]

[0112] The 7-5 process is also identified in Table 4 as a code.

[0113] [Table 4]

[0114] Because the type is different, the 40-6 valve is used in the 7-5 process, so the 40-6 valve is divided into different codes.

[0115] [Table 5]

[0116] In order to provide a better understanding of the 7-5 process, the focused streams are identified as their respective orders and components, as shown in Table 6 below:

[0117] [Table 6]

[0118] There are different types of lines, and the 40-2 pipeline type is shown in Table 7 below.

[0119] [Table 7]

[0120] For the P&ID, the Process 7-7 control elements are represented as Table 8 below.

[0121] [Table 8]

[0122] Meanwhile, the specific parameters and parameter processing in question are specified as codes in Table 9.

[0123] [Table 9]

[0124] Parameter processing includes control, indication, forwarding, and relaying. Control means assigning a parameter to a setpoint value of interest, and the controller ensures that the actual measurement is close to the setpoint value and controls devices that may affect the measurement. Indication means displaying the parameter value of a process (7-5) via a field meter or control panel in the operator's room. Change means sending the parameter value to a subsequent process control element, as indicated by the arrow. Finally, relaying means sending the process parameter of interest (7-5) to a subsequent process control element, in a manner that allows it to change. The only difference is that relaying is a variable used in a calculation, such as the ratio between two flow rates, rather than an actual flow rate measurement representing a physical quantity.

[0125] An example is shown in Figure 8. 8-1 Can A is filled with 68-1 Material A, designated T-01A. 8-2 Stream 1A is primarily composed of 68-1 Material A and T-01A. 8-2 Stream 1A is also equipped with 8-3 Control Valve V-01A, designated as a wired control valve. 8-4 Rate Indicator 01A (FIT 01A) measures the flow rate locally and sends the measurement signal to the control system. 8-4 Rate Indicator 01A (FIT 01A) sends a signal in the direction indicated by the arrow. 8-5 Rate Indicator Controller 01A (FIC 01A) displays the control setpoint and rate. The 8-5 Rate Indicator Controller 01A, FIC 01A then controls the 8-3 Control Valve V-01A to set the setpoint value (as indicated by the arrow) to achieve the desired flow rate. That is, the 8-4 Rate Indicator Converter 01A, FIT 01A ensures that the 8-5 Rate Indicator Controller 01A, FIC 01A is close to the setpoint value within a certain tolerance range, which depends on the controller software settings and hardware, particularly the measurement accuracy and sensitivity of the control valve. From the meter recognition perspective, both the 8-4 Rate Indicator 01A, FIT 01A and the 8-5 Rate Indicator Controller 01A, FIC 01A have a shared display / control, meaning that the measurements are displayed on the field meter and the control panel in the operator's control room, respectively.

[0126] Attach continuous 9-8 solid removal 7-1 to the electrode There are several variations of the 7-1 device, namely, 9-1 column electrode, 9-2 belt electrode, 9-3 rotating disk electrode, and 9-4 helical / screw electrode, as shown in Figure 9. These share several common features, including 9-5 machine, 9-6 motion generator, 9-7 motion relay, 9-8 solids removal, 9-9 solids transport, 9-13 stay, 9-20 vessel, and 9-16 components, especially 9-17 gas removal. These similar general-purpose components and principles will be further detailed in the variations.

[0127] An electrochemical reaction element consists of a 3-1 power supply connected to an immersion electrode in an electrolyte. The 1-7 electrolyte is typically a conductive liquid mixture containing 6-6 conductive ions, but can also be a conductive 3-6 membrane immersed in a liquid. This electrode forms a self-conducting material on which the electrochemical reaction occurs. The electrode connected to the 3-1 power supply (positive end) is called the 3-2 anode, where the oxidation reaction occurs, and the electrode connected to the 3-1 power supply (negative end) is called the 3-3 cathode, where the reduction reaction occurs. A third electrode, called a 3-4 reference electrode, is typically included to provide voltage measurement, although it is not required for the reaction to occur.

[0128] During electrochemical reactions, solid products tend to adhere to the electrode surface, forming solid deposits. 3-5 Solid removal is usually required to maintain the performance of electrochemical devices. 9-8 Solid removal is becoming increasingly popular in electrochemical metallurgy and battery applications, and one of the key metal formation areas of interest is the metal deposits on the electrode. 3-5 Solid deposits can form on the electrode, requiring further recovery / separation. 1-4 Processing is also required.

[0129] On the other hand, if a -5 solid deposit (located at the 3-2 anode or 3-3 cathode depending on the reaction) is formed, it is non-conductive, blocking the electrode and the electrochemical reaction will stop due to the lack of conductivity. This means that the non-conductive 3-5 solid deposit needs to be removed quickly, preferably continuously.

[0130] To meet this challenge, the new 7-1 equipment configuration is designed to continuously remove 3-5 solid deposits by relative movement with the electrode, 4-2 removal equipment, for example, by razor blades, 3-5 solid deposits occur above the electrode, and 9-8 solid removal can occur at the top (gas / air).

[0131] The gas phase has low friction and does not require filtering. The liquid / electrolyte is separated from the surface by the relative movement of the electrode. The liquid / electrolyte phase is also stirred by the relative movement of the electrode. The electrolyte is mixed and removed by the removal device. The electrolyte / liquid phase does not require a mixer. It should be noted that the electrolyte tank may be cylindrical, rather than rectangular. This can reduce the volume (and therefore cost) of the electrochemical reactor / reagents, especially when the electrode is cylindrical.

[0132] The 7-1 device can be made into multiple overlapping units in a 3, 3-2 anode-3-2 anode-3-3 cathode-3-3 cathode (cluster stack), or 3-2 anode-3-3 cathode-3-2 anode-3-3 cathode (alternately stacked) sequence to increase the production output scale.

[0133] The arrangement may take many forms, but the main arrangements of interest are 9-1 column electrodes, 9-2 belt electrodes, and 9-3 rotating disk electrodes.

[0134] The present invention provides the following advantages: Shallower 9-20 vessels are no longer needed, allowing 3-5 solids deposits to settle, resulting in smaller 35-1 electrochemical reactor sizes and reagent volumes at lower cost 1-3 is faster and cheaper, with less friction for solid separation. 3-5 The solid deposits in the air / gas phase are thicker than those in the electrolyte phase. 1-7 The solid deposits in the electrolyte phase are thicker than those in the air / gas phase. 3-5 The solid deposits are filtered out of the liquid phase. 1-7 The electrolyte phase and the mixer are not needed to facilitate mixing. Continuous process removal should be turned off for 3-5 electrochemical reactors and 3-5 solid sediment separation Simple design, no complicated 19-2 gearing and 9-5 mechanical devices would be expensive / difficult

[0135] 9-1 Pillar electrode The 9-1 columnar electrode is the simplest variation, involving a conductive columnar material as the electrode. The 9-1 columnar electrode is placed level and partially immersed in the 1-7 electrolyte.

[0136] Electrochemical reactions occur in the liquid / electrolyte phase 1-7. 3-1 When electricity is applied, the cylindrical electrode 9-1 rotates and moves 3-5. The solid deposits elevate to the gas / air phase 4-2. The removal device is used to remove 3-5. The solid deposits consist of a surface, and relative movement, for example, friction, removes between the cylindrical electrode surface 9-1 and the device 4-2.

[0137] In some embodiments, the 7-1 device includes a rigid material, e.g., the substrate is made of a rigid material that can be tilted downward outside the electrochemical device. This allows the solid deposits to gradually slide down the plate toward the outside of the device, allowing downstream processing to occur. Alternatively, the 4-2 removal device can be a single unit. The 9-9 solid transport conveyor 9-11 has a rigid, sharp edge or abrasive surface that contacts the electrode surface, allowing the removed solid deposits to be removed from the electrochemical device in a continuous, automated manner. For example, the rigid edge can be perpendicular to the flat surface of the electrode.

[0138] Another advantage is that the removed 3-5 solid deposit is mostly dry, but there is no significant amount of liquid, which accelerates the 1-3 solid separation time and requires filtration to remove the 3-5 solid deposit itself in the liquid phase.

[0139] The remaining 3-5 solids deposit may or may not be dropped into a tank and filtered as needed. However, 9-8 solids were removed from the air / gas phase, significantly reducing the need for pre-filtration of production. Alternatively, the filter may not be needed all the time, and the 3-5 solids deposit may be collected only during the 59-3 maintenance period.

[0140] 9-2 Belt electrode The 9-2 belt electrode is another variant shown in Figure 12, and is well suited to industrial-scale applications. The working principle is very similar to the 9-1 column electrode, but the application is a 9-11 conveyor setup, and the 12-1 pulley offers more functionality. 1) A larger area is in the liquid phase, allowing for deeper penetration of the 1-7 electrolyte for electrochemical reaction output and a more compact reagent tank. For example, the lower 12-1 pulley and a larger portion of the 9-2 belt electrode can be immersed in the liquid / 1-7 electrolyte phase. 2) Select a larger gas / air phase. 7-1 The device is more reliable and uses 1-7 The device is more reliable and there is less concern about liquid / electrolyte leaking. 19-2 The gears and shafts are for 9-2 The conveyor electrode moves and the wire is attached to the electrode. 3) Larger height allows more space for gas / liquid phase for more reliable design. 7-1 device eliminates 3-5 solid deposits, e.g. 9-11 conveyor conveys eliminated 3-5 solid deposits. 4) It may also be driven through a 12-1 pulley, which is a very narrow version of a 9-11 conveyor belt.

[0141] 9-3 Rotating disc electrode Another variation of the 9-3 rotating disk electrode is the 7-1 device shown in Figure 14, in which a conductive rigid disk is used as an electrode partially immersed in the electrolyte / liquid phase. The 9-3 rotating disk electrode rotates by an axial motion, while the 4-2 removal device is placed against the surface and contacts and removes the solid deposits on the electrode surface.

[0142] It provides the following features: 1) Large surface area 2) It is easy to build and manufacture. 3) Compact design

[0143] Again, please note that the 9-20 vessel can be cylindrical to reduce the space required for the 35-1 electrochemical reactor. The 9-3 rotating disk electrode can also be spiral rather than parallel, allowing the product to be continuously twisted. It's important to note that in any situation, it's a good idea to have the same shape for the 10-1 pair of electrodes, as the electrodes are easy to manufacture and install. For the 7-1 device, the conductivity only needs to be established for operation, and the 10-1 pair of electrodes does not need to have the same shape.

[0144] 9-4 Spiral / Screw Electrode 9-4 The spiral / screw electrode is modified into another one. 7-1 The device shown in Figure 16 uses a conductive screw as an electrode in a partially immersed electrolyte / liquid phase. 1-7 The screw rotates by axial action. 4-2 The removal device is placed against the surface and contacts and removes the solid deposits. 3-5 The solid deposits are on the electrode surface.

[0145] It provides the following features: 1) Large surface area 2) Compact design 3) Efficient 1-7 electrolyte movement and 9-8 solid removal

[0146] It should be noted again that the 9-20 vessel can be cylindrical to reduce the space required for the 35-1 electrochemical reactor. The 4-2 removal device can be screw or helical, and the 9-4 helical / screw electrode can be fitted to maximize the contact surface and more effectively remove solids.

[0147] Note that in any situation, it is a good idea to have the same shaped electrodes in a 10-1 pair, as they are easily manufactured and installed. For a 7-1 device, conductivity only needs to be established for the 10-1 pair to work, and the electrodes do not need to have the same shape.

[0148] Common Mechanisms

[0149] General-purpose and 9-2 belt electrodes The general mechanism will be explained first using the 9-2 belt electrode shown in FIGS.

[0150] 9-5 Machinery includes 9-6 Motion Generation and 9-7 Motion Transmission. 9-6 Motion Generation involves converting energy sources, typically but not limited to 19-1 Motor / Engine, from chemical energy to engines or electrical energy, to create motion in a machine. In some embodiments, 9-6 Motion Generation also leads to 9-7 Motion Transmission, which is accomplished by connecting 19-2 Gears and 19-3 Shafts to 19-1 Motor / Engine.

[0151] The 9-7 motion transmission is a distribution that induces the 9-5 machine to move to a specified position, in this case, generating electrode motion. This distribution can be separated into two or more stages: primary and secondary. As shown in Figure 19, the primary 9-7 motion transmission action transmits the 9-5 machine motion from the 9-6 motion source, typically the 19-1 motor / engine, to intermediate 9-5 machine components, including, but not limited to, the 19-3 shaft, 19-2 gear, 12-1 pulley, or 20-1 chain. In some embodiments, the 20-1 chain drive is used for system reliability, minimizing self-slippage and maximizing cancellation force.

[0152] As shown in Figure 20, the 9-7 level motor transmits the motion to the 9-5 mechanical motor, which then passes through the 9-5 mechanical part and electrode. Commonly used passing methods include, but are not limited to, the 19-3 shaft, 19-2 gear, 12-1 pulley, or 20-1 chain.

[0153] For homogeneous mechanical energy distribution, the 9-5 can use multiple primary and secondary distributions in parallel. For example, the 9-2 belt electrode has a double primary distribution, with top and bottom. On the other hand, the 9-2 belt electrode can have a double to quadruple secondary distribution (9-2 conveyor electrode), and for situations with double 20-1 chain drive, quadruple: top and bottom (9-2 conveyor electrode), left and right (20-1 chain drive).

[0154] As shown in Figure 21, the 9-8 solids removal system includes the 3-5 solids removal electrode, and the 9-9 solids conveyor, which removes the 3-5 solids from the 35-1 electrochemical reactor. Electrode removal can be accomplished by a variety of methods, including, but not limited to, 9-5 mechanical abrasion (4-2 removal device), ultrasound, or fluid injection. The 21-3 blade adjustment device adjusts the blade angle, but is generally not limited to spring systems. In some embodiments, particularly with the 9-2 conveyor electrode and the 9-1 columnar electrode, an additional 4-2 removal device can be placed inside the electrode to increase surface area and increase product output. This comes at the expense of greater complexity and lower operational reliability. Therefore, each case should be evaluated on a case-by-case basis. In some embodiments, using 9-10 or more blades increases removal strength and solids removal efficiency, as shown in Figure 25.

[0155] Solids transport (9-9) can be accomplished in several ways, including but not limited to conveyor 9-11 or fluid movement within channel 9-12. For conveyor 9-11, solids deposits (3-5) are continuously removed from the electrode via electrochemical reactor 35-1, which then transports them through conveyor 9-11. For fluid movement within channel 9-12, solids deposits (3-5) are continuously removed from the electrode via fluid flow within open channel 9-12. The fluid is typically not limited to liquids; water is typically chosen for its low cost. The fluid itself, particularly liquid detergent (21-2), can also be used for the subsequent washing step. As shown in Figure 28, open channel 9-12 can also have a prominent baffle (21-1) to prevent solids deposits (3-5) from overflowing into channel 9-12.

[0156] There are several variations in the default design of the 9-12 channel. An open 9-12 channel is typically made from a 7-6 pipeline cut into a longitudinal section to form a 28-1 radian (standard), a 28-2 rectangular 9-12 channel, a 28-3 triangular 9-12 channel, or any other shape for fluid flow. The default is a 21-1 baffle. The 28-4 right-angle baffle (default) is convenient for manufacturing. However, a 28-5 acute-angle baffle or a 28-6 obtuse-angle baffle can be used to align the overflow path.

[0157] The basic 9-20 vessel is located at the bottom, as shown in Figure 22. There is a pair of electrodes 10-1 on top of the 9-20 vessel. In some embodiments, the 10-1 pair of electrodes is attached to the 9-20 vessel for ease of manufacturing. The 9-20 vessel is loaded with electrolyte liquid 1-7, which has an electrolyte inlet 22-1 and an electrolyte outlet 22-2. In some embodiments, to reduce energy costs, the electrolyte is pumped from the top to the bottom, and the electrolyte inlet 22-1 and the electrolyte outlet 22-2 are arranged by gravity, allowing the electrolyte to enter 1-7 from the top and leave the bottom.

[0158] Figure 23 shows the 9-13 stay, which is a 9-2 conveyor electrode and a 9-14 movable, deformable body. The 9-13 stay is comprised of a 23-4 housing that secures and positions the electrode system. The bottom section of the 23-4 housing is typically equipped with 23-3 wheels or tracks for easy removal from the container and 59-3 maintenance. The 23-2 arm of the 23-4 housing features an adjustable height, but is typically not limited to a 23-1 hydraulic top. The adjustable height feed system shuttles the electrode system from the 9-20 container, eliminating the need for time-consuming 1-7 electrolyte transfer from the 9-20 container. This provides a convenient and fast 59-3 maintenance process, and the electrode requires maintenance. 59-3 maintenance requires cleaning the 9-20 container, which is slow and cumbersome, potentially affecting other operating units.

[0159] The motor / engine attached to the arm 23-2 provides the mechanical drive 9-5. The motion is generated by the motor 9-6. In addition to the electric motor, the mechanical motion can also be generated by an engine (combustion) or any other method.

[0160] The 7-1 device further includes the 9-16 component, specifically the 9-17 gas filter, as shown in Figure 24. The 9-17 gas filter is implemented when unwanted gases, usually flammable or toxic, are released in sufficient quantities. One example is the water splitting reaction, which generates flammable hydrogen. In some cases, the toxic 6-9 ammonia gas is a by-product of the 1-15 process, which is in liquid form and may evaporate into smoke. The 9-17 gas filter can be either closed or open. A closed 9-17 gas filter only directs gases into a designated flow path, such as a condenser or burner, within the 7-1 device's airtight space. An open 9-17 gas filter is an installation similar to a ventilation cabinet, using the chimney effect to draw in gases. The open 9-17 gas filter is used when gas separation is not required, while the closed 9-17 gas filter is used when gas separation is required. In some embodiments, the 9-17 gas filter can be omitted if gas escape is minimal.

[0161] Other components of 9-16 include brush 9-18 and wax 9-19. Maintaining electrical contact can be challenging when the electrode is constantly moving. However, electrical contact is established through conductive solids. In some embodiments, this is through the 4-2 removal device 9-8 solid removal. In some embodiments, additional electrical contact is provided outside the 4-2 removal device, such as the external supply 9-18, which is conductive, as shown in Figure 26, via support 26-1, typically made from carbon, but not necessarily graphite. In some embodiments, the electrode is continuously thinly coated, such as through accessory stay 26-1, similar to wax 9-19, or wax layer 27-1, as shown in Figure 27, to facilitate electrode removal. In some embodiments, wax 9-19 is completed by applying solid friction with wax to the electrode surface. In some other embodiments, wax 9-19 is more complex, using a wax splitter 9-19.

[0162] 9-1 Pillar Electrode: For the 9-1 columnar electrode variant, the recommended 7-1 device configuration is shown in Figure 11. The columnar electrode has a 20-well, of which 1-7 is loaded with electrolyte. 1-7 enters the electrolyte inlet through 22-1, which then leaves through 22-2. To reduce resistance, a pair of conductive electrodes, 10-1, are attached to the inner wall of the 9-20 vessel. For ease of operation, the 9-20 vessel has a side wall, while the 9-15 variant incorporates a 9-13 stay and frame. Two transparent side windows, 22-3, allow for monitoring of changes in the 9-20 vessel.

[0163] The 9-5 machine includes a 9-6 motion generator and a 9-7 motion transmission. The 9-6 motion generator is driven by a 19-1 motor / engine, which in this case drives two 19-2 gears and two 19-3 shaft systems that drive the 9-1 column electrodes.

[0164] 9-8 solid removal includes 3-5 solid deposit removal, 9-1 column electrode, 4-2 removal device, and 21-3 blade adjustment, which adjusts the blade angle to control the wiping action.

[0165] The 9-9 solid transport channel is open. The 9-12 channel contains one flow channel, the 21-2 detergent flow channel, and the 9-1-2 detergent inlet and outlet terminals, respectively. The 21-1 baffle prevents overflow when the 3-5 solid deposits are removed from the self-electrode.

[0166] The 24-2 cap is connected to the 24-1 ventilation port of the ventilation cabinet, and the 24-5 sleeve (washing tube) and 24-7 sleeve (electrode frame) are used to draw in ambient air.

[0167] 9-3 Rotating disc electrode For the 9-3 rotating disk electrode variant, the recommended 7-1 device configuration is shown in Figure 15. The columnar vessel is similar to the 9-20, with the 9-1 columnar electrode variant, containing the electrolyte 1-7. The electrolyte 1-7 enters through the electrolyte inlet 22-1, which then leaves the electrolyte outlet 22-2. To reduce resistance, the 10-1 pair of electrodes sandwiches conductive disks on opposite sides of the 9-3 rotating disk electrode, separated by an insulator 60-3. In some embodiments, the 10-1 pair of electrodes can be attached to the inner wall of the 9-20 vessel as an insulator, providing ease of manufacture while providing some electrical resistance and therefore lowering energy efficiency. For ease of operation, the 9-20 vessel has side panels. The 9-15 variant also incorporates the 9-13 stay and frame, and two transparent side windows 22-3 allow for monitoring changes in the 9-20 vessel.

[0168] The 9-5 machine includes the 9-6 motion generator and the 9-7 motion transmission. The 9-6 motion generator is driven by the 19-1 motor / engine, which drives two 19-2 gears and two 19-3 shafts. The 9-3 rotating electrode is driven by the 9-8 solids removal system. The 9-3 rotating electrode is driven by the 3-5 solids removal system. The 21-3 blade adjustment adjusts the blade angle to control the wiping action.

[0169] 9-9 is the solid transport channel, 9-12 is the open channel containing one flow, 21-2 is the detergent flow channel between two terminals, 21-4 is the detergent inlet and 21-5 is the detergent outlet. 21-1 is a baffle to prevent overflow when solids are removed from the self-electrode.

[0170] The 24-2 cap is connected to the 24-1 ventilation port of the ventilation cabinet, and the 24-5 sleeve (washing tube) and 24-7 sleeve (electrode frame) are used to draw in ambient air.

[0171] 9-4 Spiral / Screw Electrode For the spiral / screw electrode variant, the recommended 7-1 device configuration is shown in Figure 17. The 9-20 vessel has a columnar section, into which the 1-7 electrolyte is loaded. The 1-7 electrolyte enters through the electrolyte inlet 22-1, then leaves through the electrolyte outlet 22-2. To reduce resistance, the 10-1 pair of electrodes sandwich the conductive disk surfaces of the 9-4 spiral / screw electrode, separated by a single 60-3 insulator. In some embodiments, the 10-1 pair of electrodes can be attached to the inner wall as an insulator. The 9-20 vessel is easy to manufacture and has some electrical resistance, but is therefore less energy efficient. For ease of operation, the 9-20 vessel has side windows, while the 9-15 variant incorporates a stay and frame 9-13. Two side windows 22-3 can be transparent to allow monitoring of changes in the 9-20 vessel.

[0172] The 9-5 machine includes the 9-6 motion generator and the 9-7 motion transmission. The 9-6 motion generator, in this case, is driven by a 19-1 motor / engine, two 19-2 gears, and two 19-3 shafts, driving the 9-4 helical / screw electrode. The 9-8 solids removal system includes the 9-4 helical / screw electrode, which removes the 3-5 solid deposits by itself, using the 4-2 removal device. In the diagram, the screws rotate together, but not in the same direction, in opposite directions, and contact the 9-4 helical / screw electrode, which removes the 3-5 solid deposits by friction. In some embodiments, the still blade is fixed to the 9-20 container, or the 9-13 stay.

[0173] 21-3 Blade adjustment adjusts the blade angle to control the wiping action.

[0174] Channel 9-9 is the solid transport channel, and Channel 9-12 contains two open channels. Channel 9-12 contains two detergent channels, 21-2 detergent inlet and 21-5 detergent outlet. There is a baffle 21-1 to prevent overflow when solids deposit on the 3-5 electrode are removed.

[0175] 9-17 Gas removal is provided on the 24-2 cap, which connects the 24-1 ventilation outlet to the ventilation cabinet.

[0176] Electrochemical production 7-3 polymer addition

[0177] The 7-3 polymers are a class of 1-8 polymers formed in additive reactions, producing the 1-15 by-product. Some exemplary 7-3 polymers contain carbon backbones with no hybrid atoms, e.g., Polyethylene base: polyethylene (PE), polypropylene (PP), polystyrene (PS), polyvinyl chloride (PVC), etc. Common polyalkyls, such as polybutadiene (rubber)

[0178] As shown in Figure 29, electrochemically produced 7-3 polymers can be classified into 29-1 homopolymers and 29-2 copolymers. In some embodiments, 29-1 homopolymers are first removed from 29-3 by removing the alcohol group shown in Equation 2, or other 29-4 variants, such as sulfides or amines.

[0179]

number

[0180] The aggregation may start from the second step if the unsaturated compounds contain unsaturated hydrocarbons such as olefins or acetylene as the initial raw materials.

[0181] 29-2 copolymers, on the other hand, can be produced when different initiator groups are mixed. 29-3 alcohol groups, or functional groups such as alcohols and sulfides, can also be produced when these different species are present in the same system. 1-7 electrolytes are present during electrochemical reactions.

[0182] As shown in Figure 30, the 6-6 conductive ions can come from either 30-6 membranes or 30-1 dissolved ions. 30-6 membranes include, but are not limited to, 1-7 electrolysis membranes used in electrolyzers and fuel cells, such as proton exchange 30-6 membranes (commonly used in acidic and neutral aqueous systems) or polymer ion exchange 30-6 membranes (typically used in alkaline aqueous systems). One example is the nanofiber membrane, a type of proton exchange 30-6 membrane typically used in hydrogen fuel cells. 30-1 dissolved ions come from 30-2 metal ions, such as lithium ions (lithium chloride), or 30-3 nonmetallic ions. 30-3 nonmetallic ions are typically classified into 30-4 organic and 30-5 inorganic variants. 30-4 organic variants include surfactants such as palmitate ions, sodium palmitate (commonly used in soaps), or deep-dissolved salts or ionic liquids. For example, choline chloride is a common component of the eutectic 31-4 solvent, while 1-butyl-3-methylimidazole hexafluorophosphate ([BMIM]PF6) acts as a common ionic liquid. In some situations, a 31-1 cosolvent may be necessary, as shown in Figure 31. 31-1 cosolvents can include 30-4 organic and 30-5 inorganic variants. 30-4 organic variants can include 31-2 engineered molecules, particularly 31-3 crown ethers, used to dissolve metal ions in the organic phase, or common 31-4 solvents, such as acetone, which are miscible or soluble in both the organic and polar phases. 30-5 inorganic variants include 6-9, where ammonia and water are commonly used solvents, and 1-15 by-products are generated during the reaction.

[0183] The 32-1 additive composition, consisting of 1-13 catalysts, is outlined in Figure 32 and is classified as 32-2 redox and 32-3 other. This can include 32-2 redox catalysts, particularly electron shuttles, which function by facilitating electron transfer in either the oxidation or reduction step, such as triaromatic amines and pyridines. 32-3 other catalysts include catalysts that function in non-redox steps by stem interference. 1-13 catalysts, including coordination catalysts, are incorporated into monomer molecules, such as titanium tetrachloride (TCl) and triethylaluminum (TTA), to facilitate the transfer of transition metals. While 32-1 additives are generally homogeneous catalysts in fluid form, they can also constitute self-solid catalyst suspensions in some embodiments.

[0184] 29-3 alcohol group The main transformation product is alcohol as the initial material, which causes dehydration-polymerization of water to form 1-15 by-product, as shown in Equation 3.

[0185]

number

[0186] Examples of this include the following generic polymers 1-8 shown in Table 10:

[0187] [Table 10]

[0188] 29-4 Plasmodium: Sulfide Similar to the reaction of 29-3 with alcohol groups, sulfide is also formed in the electrochemical reaction of 7-3 with polymer, which is charged with hydrogen sulfide to form 1-15 as a by-product, as shown in Equations 4 and 5.

[0189]

number

[0190]

number

[0191] 29-4 Variant: Amine Similar to the reaction of alcohols and sulfides, amines can also undergo electrochemical reactions to form polymers 7-3 and 1-15, as shown in Equations 6 and 7:

[0192]

number

[0193] If the above substituent 3 is a hydrogen atom, 6-9 ammonia is formed instead of an amine.

[0194]

number

[0195]

number

[0196] 29-2 copolymer

[0197] As mentioned previously, 29-2 copolymers can be formed when different types of initial alcohols are present in the 1-7 electrolyte system, as shown in Equation 8. Different types of initial groups, including alcohols, sulfides, or amines, can also result in similar 29-2 copolymer final products.

[0198] Some examples of 29-2 copolymers are included in Table 11.

[0199] [Table 11]

[0200] Note that 29-2 copolymers have three or more types of initial chemicals, such as the common acrylonitrile butadiene styrene (ABS) resin. Valuable and widely used engineering plastics are shown in Table 12.

[0201] [Table 12]

[0202] Note: The order of each unit in the 29-2 copolymer may be arbitrary.

[0203] List 13 below is a more specific response.

[0204] [Table 13] JPEG2025134691000023.jpg255168JPEG2025134691000024.jpg251170JPEG202 5134691000025.jpg137170JPEG2025134691000026.jpg245170JPEG20251346910 00027.jpg160170JPEG2025134691000028.jpg255168JPEG2025134691000029.j pg106170JPEG2025134691000030.jpg197170JPEG2025134691000031.jpg233170

[0205] Electrochemical Production of 7-4 Condensation Polymers As shown in Figure 33, 7-4 condensation polymers are the second class of 1-8 polymers formed via condensation polymerization in the 7-2 chemistry. This includes, but is not limited to: 33-2 Polyesters (including cellulose, furan, phenolic and related resins) 33-5 Polysulfide 33-6 Polyamines 33-8 Polyester 33-9 Polyamide 6-7 Polycarbonate 33-10 Creatinine 33-11 Polyimide 33-12 Urethane 33-13 Ring opening 33-14 Miscellaneous atoms: polysilicon, polysulfone, polyphosphinate, polynitrate Electrochemical production of 7-4 condensation polymers involves 33-1 condensation with ester exchange. 33-1 condensation removes an active group between molecules to form bonds, while ester exchange often involves more complex removal of a carbonyl group.

[0206] 33-1 indent, 33-2 polyester The simplest reaction is electrochemical: 33-1 indents glycol to form 33-2 polyester, which is then reacted with water to form 1-15 byproduct, as shown in Equation 9.

[0207]

number

[0208] Similar to the 7-3 polymer addition, copolymerization can occur between different types of glycols, but in the same system, as shown in Equation 10,

[0209]

number

[0210] The copolymerization order of each unit may be arbitrary. Specific reactions of interest are detailed in Table 14.

[0211] [Table 14] JPEG2025134691000035.jpg71170

[0212] 33-1 Indentation, 33-3 Monoalcohol, Furan and Phenolic Resins In the case of aromatic compounds with a carbon backbone, such as furans and phenols, 33-1 indentation can occur through a single alcohol group, as shown in Equations 11 and 12. The final product is a 33-2 polyether or polyalkyl group.

[0213]

number

[0214]

number

[0215] Note: For the above situation, adjacent hydrogen atoms are not available for intramolecular dehydration / elimination, and therefore intermolecular reactions are the only available reactions. Table 15 illustrates the commercial interest in the reaction of furan with phenolic resins.

[0216] [Table 15]

[0217] 33-1 Indent, 33-4 Cellulose It should be noted that the carbon backbone can contain sugars or their derivatives; in this case, the final product formed from the 33-2 ether is actually a 33-4 cellulose resin, a 1-8 polymer typically used in biodegradable applications. For example, the starting material can be glucose, as shown in Scheme 13.

[0218]

number

[0219] A similar reaction applies to sugar derivatives, where some of the -OH groups of glucose are esterified to acetate groups, as shown in Equation 14.

[0220]

number

[0221] 33-4 Cellulose copolymers may also react when different sugars are mixed in the same system.

[0222] 33-1 Indent, 33-5 Polysulfide Similar to 33-2 polyester, 33-5 polysulfide can electrochemically self-produce disulfide as shown in Equation 15.

[0223]

number

[0224] A similar reaction applies to sugar derivatives, where some of the -OH groups of glucose are esterified to acetate groups, as shown in Equation 14.

[0225]

number

[0226] Notable polysulfide reactions are listed in Table 16.

[0227] [Table 16]

[0228] 33-1 Indent, 33-6 Polyamine Similar to 33-2 polyester and 33-5 polysulfide, 33-6 polyamine can be generated electrochemically as shown in Equation 17.

[0229]

number

[0230] Copolymers are also possible when different dimines are mixed in the same system, as shown in Equation 18.

[0231]

number

[0232] 33-7 ester exchange, 33-8 polyester The 33-8 polyester can be produced by transesterification of 33-7, which is similar in some respects to the 33-1 indentation. The simplest variant is the reaction of an alcohol with a carboxylic acid group in the same hydroxy acid molecule, as shown in Equation 19.

[0233]

number

[0234] It should be noted that hydroxy acids react to form 3-8 polyesters, which are very useful in the production of many biodegradable 1-8 polymers, such as polylactic acid, which is made from lactic acid, polyacrylate, and acrylic acid.

[0235] The next transformation is the reaction between an alcohol and a carboxylic acid group in a different molecule, for example, between a glycol and a diacid, as shown in Equation 20.

[0236]

number

[0237] Specific reactions under polyesters are detailed in Table 17.

[0238] [Table 17] JPEG2025134691000049.jpg252170JPEG2025134691000050.jpg251170JPEG2025134691000051.jpg70170

[0239] 33-7 Transesterification: 33-9 Polyamide 33-9 polyamide is a useful 1-8 polymeric material, including biopolymers and materials such as nylon and kettle. Very similar to 33-8 polyester, it involves the reaction between amine and carboxylic acid groups to produce the product. The simplest variation is amino acid polymerization, where the amine and carboxylic acid groups are combined in the same molecule, as shown in Formula 21.

[0240]

number

[0241] Another variant is a molecule with different ester amine and carboxylic acid groups, between a diamine and a diacid, as shown in formula 22.

[0242]

number

[0243] Polyamide reactions of interest are described in Table 18.

[0244] [Table 18]

[0245] 33-7 Transesterification: 6-7 Polycarbonate 6-7 Polycarbonate can also be produced electrochemically by the reaction between glycol and a carbonyl compound, as shown in Equation 23. This is a very useful reaction because the carbonyl compound may be present in 6-1 urea, which is abundant, inexpensive, and not extremely toxic. Carbonic acid is produced from carbon dioxide, and dimethyl carbonate is an industrially available 5-3 commodity chemical. 1-15 The by-product is usually recovered as a useful fuel or valuable 5-5 raw material chemical.

[0246]

number

[0247] When different glycols are present, copolymeric carbonates can be produced as shown in Equation 24.

[0248]

number

[0249] Polycarbonate reactions of interest are described in Table 19.

[0250] [Table 19]

[0251] 33-7 Transesterification: 33-10 Creatinine 33-10 polyanhydrides can electrochemically generate their own diacids and anhydrides as shown in Equation 25. The by-products are carboxylic acids or their derivatives.

[0252]

number

[0253] 33-7 Transesterification: 33-12 Urethane 33-12 Polyurethane can be electrochemically generated by the reaction of glycol with isocyanate ester, as shown in Equation 26.

[0254]

number

[0255] Specific polyurethane reactions of interest are listed in Table 20.

[0256] [Table 20]

[0257] 33-7 Transesterification: 33-11 Polyimide 33-11 Polyimides can undergo self-reaction between dianhydrides and diamines, and between anhydrides and diisocyanates. The reaction of dianhydrides with diamines is more efficient because of the abundance of diamines, as shown in Equation 27.

[0258]

number

[0259] On the other hand, the reaction of diisocyanic anhydride generates carbon dioxide, which can be easily separated into gases 1-5, as shown in Equation 28.

[0260]

number

[0261] Polyimide reactions of interest are further detailed in Table 21.

[0262] [Table 21]

[0263] 33-7 Transesterification: 33-13 Ring Opening Ring-opening reactions are a useful method for producing 1-8 polymeric self-cyclized compounds, shown in Formula 29. The cyclized compounds are typically spurious loops containing groups such as carbonyl (C=O) groups, carbonates, ethers, esters, amides, sulfides, or other groups with atoms other than carbon atoms.

[0264]

number

[0265] It should be noted that although the scheme begins with the shortest possible ring, i.e., a triangular ring, this ring can be made larger by using larger rings. In some embodiments, the resulting 1-8 polymer contains a carbon backbone. Some notable examples include 3-13 rings that open into the cyclic carbonate, i.e., the main ring, to produce 6-7 polycarbonates, as shown in Scheme 30 and Scheme 31:

[0266]

number

[0267]

number

[0268] The loop opening polymerization reactions noted are detailed in Table 22.

[0269] [Table 22]

[0270] 33-7 Transesterification: 33-14 Miscellaneous atoms: Polysilicon, Polysulfone, Polyphosphinic acid ester, Polynitrate ester 33-1 indentation and / or 33-7 transesterification also work when the adjacent atoms are not carbon atoms. 33-14 miscellaneous atoms, polysilicones, polysulfones, polyphosphinates, and polynitrates. For example, silicon oxytane can undergo 33-1 indentation (similar to 33-2 polyesters) to form 33-15 polysilicones, as shown in formula 32.

[0271]

number

[0272] Oxytane, another example, glycols can undergo transesterification 33-7 by exchanging with sulfonyl compounds (similar to carbonyl compounds) to form 33-16 polysulfones, as shown in Equation 33.

[0273]

number

[0274] Polyphosphinates are also possible if the miscellaneous atom is phosphorus, as shown in Equation 34.

[0275]

number

[0276] Other possibilities include polynitrates, etc. Miscellaneous atom variants of interest are listed in Table 23.

[0277] [Table 23]

[0278] Chemistry 7-5 Process As shown in Figure 34, the 7-5 process generally involves 34-1 Concept, 34-2 Recovery and Removal, 34-3 Reform, 34-4 Waste Management and finally 34-5 Block Flowchart.

[0279] 34-1 concept The first variant, the electrochemical 5-1ElerGreen process for polymer production (Figure 35), is very similar to the common 7-5 process, except that the conventional reactor 1-2 requires significant heat energy (1-11), pressure (1-12), and catalyst (1-13), while the 35-1 electrochemical reactor uses electricity (3-1) and ions (6-6). While heat energy (1-11) and pressure (1-12) are usually not required, they can still be added to the 35-1 electrochemical reactor if necessary, depending on the type of reaction. In such cases, the temperature and pressure (1-12) are often lower than the conventional 7-5 process.

[0280] Generic variables, variables 1, can be used when 1-15 by-products are valuable but harmful 36-1 when emissions are environmentally hazardous, such as amines or alcohols. In these situations, 1-5 recovery units are used to recover the valuable (albeit environmentally harmful) 5-5 raw chemicals for sale rather than being discharged / disposed of, resulting in a more complex 7-5 process.

[0281] 34-2 Recycling Another morph, morph 2, is simpler than morph 1, as shown in Figure 36. Its by-products are not recovered, but are simply discharged to the atmosphere. The by-products are neither harmful nor valuable. For example, water is the source of many reactions. This further reduces capital and operating costs due to recovery.

[0282] 34-3 Kaizo While many other green technologies involve rebuilding the entire 7-5 process, this new electrochemical 1-8 polymer production 5-1 electroGreen process involves replacing the core of the 1-2 conventional reactor with a 35-1 electrochemical reactor, while retaining the existing industrial standard (if not with minimal adjustments) and adding additional operating units, as shown in Figure 37.

[0283] This compatibility allows a conventional system to purchase a conventional factory consisting of 1-2 conventional reactors and 35-1 electrochemical reactors, rather than having to build a completely different chemical factory from the start. As a result, many green technologies that exceed budgets can be avoided. The acquisition of a conventional factory itself also serves to shorten the project's implementation time. In addition to providing a revenue stream, it can also be used to repay bonds / loans. After the product is renewed, the cost remains essentially the same, except for the market share utilized, at a substantially lower cost.

[0284] The method of accessing 34-3 is to access the 35-1 reactor from the 37-1 path to the 1-2 normal reactor system. This is achieved by constructing the 35-1 chemical reactor on-site, connecting the column pipeline to the 37-1 path system as an alternative, debugging this alternative system, and ultimately shutting down the normal system.

[0285] The purpose of the 34-3 modification is to install a new type in the distillation tower, which is placed between the top and bottom of the distillation tower and the solvent to exchange the solvent, and is easily connected with the 7-6 pipeline and switching valve.

[0286] 34-4 Scrap Management Another variant, an additional 34-4 waste management unit, is shown in Figure 38. For 34-4 scrap management, a 38-1 waste extraction facility is required. A simple variant is the installation of a 38-1 waste extraction facility to extract active ingredients (usually toxic substances in 5-2 chemical waste) from the 5-2 chemical waste. Alternatively, the 38-1 waste is separated into a 7-5 chemical process, or in a separate facility, where the separated active ingredients are transported to a 1-8 polymer production facility and stored in conventional material storage tanks. The 38-1 waste extraction facility typically consists of separation from 7-5 process equipment, including, but not limited to, solvent extractors and distillation columns. The exact type and specifications used depend on the chemical process in which the 5-2 chemical waste and active ingredients of interest are processed, depending on the individual plan.

[0287] One embodiment of the 34-1 concept is the self-extraction of ethylene glycol from paint sludge and waste disposal prevention material 38-1, which is then used for scrap management. Ethylene glycol can cause neurological damage, vomiting, and death after ingestion, and is also harmful to the environment. When excreted, it is absorbed into paint sludge and waste refrigerants. However, when condensed to industrial levels, ethylene glycol can be produced as a raw material for 5-5, which is of interest to the chemical industry and can be easily sold for profit. Ethylene glycol can be separated from paint sludge using a distillation column or other separation process, such as membrane filtration. For this purpose, 34-4 scrap can be integrated into the 1-8 polymer production 7-5 process. A 5-2 chemical waste tank with a separation device can be installed upstream, with the ethylene glycol continuously separated and stored in a material storage tank before the storage tank. Alternatively, 34-4 Scrap Management can be conducted on a separate plant site (which may be owned by the same entity or by other entities, including but not limited to suppliers and 34-4 Scrap Management customers) designated for 34-4 Scrap Management plant and transport the separated ethylene glycol via chemical trucks to polymerize 7-5 course.

[0288] 34-5 Block Flowchart As detailed in Figure 39, the general 7-5 process consists of multiple modules: materials, 1-1 preparation, synthesis, 1-3 solids separation, 1-4 processing, and 1-5 recovery.

[0289] material: The material module consists of 1-6 reactant tanks, supply tank A, and other 1-6 reactants, such as supply tank B or supply tank C, D, E, F, and possibly others. 68-1 Material A is supplied from a chemical tank truck through an inlet, usually but not necessarily at the top, of supply tank A. Supply tank A has an outlet, usually at the bottom, for various purposes, such as 59-3 maintenance, sorting, and shutdown, to discharge empty cans. 68-1 Material A leaves supply tank A through an outlet, usually but not necessarily at the bottom, and enters a mixing tank.

[0290] In some embodiments, if the polymerization reaction involves more than one monomer, other materials are required, and additional feed tanks are required, connected in parallel to Feed Tank A. Material B, on the other hand, is typically fed from another chemical tank via an inlet, usually not necessarily at the top of Feed Tank B. Feed Tank B, similar to Feed Tank A, has a drain, usually at the bottom, for purposes such as draining empty containers for maintenance, cleanup, and shutdown. Material B leaves Feed Tank B via an outlet, usually at the bottom, but not necessarily at the bottom, and enters a mixing tank. Other materials, such as Materials C, are required, such as Materials D, E, and F, especially for coagulation. Feed Tank C is connected in parallel to Feed Tank B, with D, E, and F added in parallel.

[0291] 1-1 Preparation: The automatic mixing tank 1-1 is intended to consist of a heater and pump. Mixing tank 1-6 contains reactants (materials A and B, and C, D, E, F, etc., if applicable), and 1-7 contains electrolytes (unreacted materials 68-1, A and B, and C, D, E, F, etc., if applicable). 6-6 contains conductive ions (e.g., 68-3 dissolved salts), if applicable. 32-1 contains additives and 31-1 contains cosolvents. The mixer includes a mixer, typically driven by a motor or engine, but not necessarily mechanically, using fan blades to stir the mixer. In some embodiments, the motor or engine does not need to be physically connected to the blades via a shaft. The movement of the fan blades can be indirectly influenced, for example, by a magnetic field similar to that of 68-5 magnetic mixer. In some cases, the change in the magnetic field can be induced by an inductor system, eliminating the need for a motor / engine. In some embodiments, agitation is achieved in the absence of mechanical means under a motor or engine, for example by using ultrasound to vibrate molecules, or by creating turbulence in a static mixer to mix and homogenize materials through multiple corners and barriers, or by bubbling gas into the liquid phase in a drum to induce mixing.

[0292] The mixed 1-7 electrolyte, consisting of 68-1 Material A and 68-2 Materials B, C, D, E, and F (if applicable), 68-3 Salt Dissolver, and 32-1 Additive and 31-1 Co-solvent (if applicable), leaves the mixer through an outlet, usually but not necessarily at the bottom of the mixing tank. It is then heated and pumped into 40-3 Pump / Compressor using a heater. In some embodiments, the heater may be replaced with other heating methods, such as a heat exchanger, to achieve a higher temperature relative to other fluids through conduction and convection. This is typically not limited to hot steam, but is typically used for hot water or oil. In some embodiments, the heater can be replaced with a cooling unit if cooling is required. In some embodiments, if heating or cooling the 1-7 electrolyte is not required, the heating and / or cooling units may be eliminated.

[0293] The 1-7 electrolyte then enters the 40-3 pump / compressor, which increases the pressure of the 1-12 to the level required for the subsequent chemical reaction. While a compressor is typically used, it can be replaced with a pump, such as a centrifugal pump, if the 1-12 pressure is not required to achieve cost reduction goals. In some embodiments, the 40-3 pump / compressor can be swapped upstream from the heating / cooling unit. That is, the 40-3 pump / compressor can be placed before the heater, rather than the standard configuration, where the heater is placed before the 40-3 pump / compressor. In some embodiments, the 1-12 pressure is not required, and the 40-3 pump / compressor unit can be eliminated. The mixture, at the appropriate temperature and pressure, then enters the synthesis module.

[0294] Synthesis: The synthesis module starts with a switching valve that guides 1-7 electrolytes through two possible paths.

[0295] a. General Selection The electrolyte then enters the reactor. Conventional reactors (1-2) have adjustable temperature and pressure. The reactants (1-6) react with the mixture to form polymers (1-8), suspended solids (1-15), and by-product chemicals (1-15). Depending on the specific process requirements (7-5), conventional reactors (1-2) may have heating / cooling systems or insulators for temperature control and safety. Reinforced / reinforced conventional reactor walls and / or pressure vent valves or bursting pieces (1-12) are used for pressure safety. Conventional reactors (1-2) may also be coupled to agitators driven by a motor / engine. In some embodiments, mechanical transmission can be achieved without direct shaft contact, while non-contact influences, such as magnetic fields, may be used for magnetic mixers (68-5). In some embodiments, the motion can be coupled to the motor / engine by altering the magnetic field of a self-inductor system rather than magnetically. In some embodiments, mixing can be non-mechanically induced, such as by ultrasound to vibrate molecules or multiple bends / obstacles to create turbulence in the flow. In some embodiments, the lack of mixing may be beneficial to reaction efficiency by reducing dilution of reactants 1-6; for such purposes, reactors 1-2 are used rather than the usual reactors.

[0296] The resulting mixture of 1-14 waste electrolyte, 1-8 polymer, and 1-15 by-product is separated by a filter. In some embodiments, the filter can replace other methods of solid-liquid separation, such as a cyclone separator. The solid 1-8 polymer leaves the filter or a solid-liquid separation unit and enters the electrochemical pathway via a switch valve. The liquid 1-14 waste electrolyte and 1-15 by-product chemicals leave the filter or a solid-liquid separation unit, exit through another outlet, and enter the electrochemical pathway via another switch valve.

[0297] b. Electrochemical selection The electrochemical route consists of a new electrochemical reactor (35-1), in which reactants (1-6) react with the mixture to form polymers (1-8) and by-products (1-15). The electrochemical reactor (35-1) has an adjustable operating current. The applied voltage (6-5), wiper position, electrode speed, and temperature (1-12) are controlled by the pressure. Depending on the specific process requirements (7-5), the electrochemical reactor (35-1) may have a heating / cooling system or an insulator (7-7) for temperature control and safety. Strengthening / reinforcing the vessel wall (9-20) and / or a pressure release valve or bursting piece (1-12) are used for pressure safety (1-12). While agitation is provided by default in the electrochemical reactor (35-1), the relative movement of the electrode pair (1-7) can be used to drive the electrolyte, while the electrochemical reactor (35-1) can involve a stirring blade to drive a motor / engine. In some embodiments, mechanical transmission can be achieved without direct shaft contact, while non-contact influences, such as magnetic fields, can be used for the magnetic mixer (68-5). In some embodiments, motion can be controlled by a motor / engine, rather than magnetically, by alternating magnetic fields with a self-inductor system. In some embodiments, mixing can be achieved non-mechanically, such as by using ultrasound to vibrate molecules or by using multiple bends / obstacles to create turbulence in the flow. For example, in a solid-liquid separation unit, the lack of mixing can be beneficial to reaction efficiency by reducing dilution of the reactants. For this purpose, a plug flow 35-1 electrochemical reactor can be used instead. Depending on the specific process requirements, a gas scrubber (9-17) can be installed in the 35-1 electrochemical reactor. As previously mentioned, a specially designed gas scrubber (9-17) can be used to remove gas escaping from the electrochemical reaction. Furthermore, hydrogen and oxygen can be split from water to form by-products in the electrochemical reaction. When large amounts of water are present in the 1-7 electrolyte, the 1-7 electrolyte can contain large amounts of water.

[0298] The solids deposited in 3-5 and 1-8 are continuously removed from the electrode and passed through 9-8, where the solids are removed and sent to 35-1, then discharged to 35-1. Although 9-9 is a single-flow solids transport system, 21-2 detergent is in an open-flow channel 9-12. 1-8 polymer solids are collected in 1-8, and then sent to 1-3, where they are separated. In some embodiments, 9-9 solids transport is mechanically controlled by 9-11 conveyors. 1-8 polymer is wetted with some remaining waste electrolyte 1-14, with or without detergent 21-2, and then combined with 1-2, a conventional reactor, via a switching valve. The combined stream is then sent to 1-3, where it is washed and converted into water or the associated detergent 21-2, and further processed into 1-10 polymer products.

[0299] 1-3 Solid separation The 1-3 solids separation module constitutes a self-cleaning device, typically driven by a mixer or mixing vessel. In some embodiments, the motor and engine do not need to be physically connected to the fan through a shaft; rather, the movement of the fan blades can be indirectly affected. For example, a magnetic field similar to that of a 68-5 magnetic mixer can be generated. In some cases, magnetic field changes can be induced by an inductor system, eliminating the need for a motor or engine. In some embodiments, mixing is achieved without a mechanical motor or engine, for example, by using ultrasound to vibrate molecules, or by generating turbulence in a static mixer to mix and homogenize materials through multiple angles and barriers, or by bubbling gas into the liquid phase to induce mixing. The 21-2 detergent contains the 1-8 polymer suspension and traces of 1-14 waste electrolyte. The 1-14 waste electrolyte that is delivered to the scrubber is dissolved in 21-2 detergent, which then reconstitutes the 1-8 polymer solids. The suspension is then diluted with 21-2 detergent, which is then sent to a downstream settler.

[0300] The settler is a large container that mixes 21-2 detergent with trace amounts of dissolved 1-14 waste electrolyte and 1-9 clean polymer, maintaining the suspension. The 1-9 clean polymer and 1-8 polymer suspension are separated by gravity. In some embodiments, this polymer separation may be accomplished by other means, such as centrifugation, a filter, or a cyclone separator. The discarded 21-2 detergent leaves the settler through an outlet (although not always at the top), and the 1-9 clean polymer sediment leaves the settler through another outlet (although usually not at the bottom). However, under normal circumstances, the 1-9 clean polymer is heavier than the 21-2 detergent, causing it to settle to the bottom. In some embodiments, the 1-9 clean polymer is lighter than the liquid. The 1-9 clean polymer solid is removed from the outlet at the top, but remains at the bottom, rather than the 21-2 detergent. The discarded 21-2 detergent is recycled to the detergent tank, and at the same time, the 1-9 clean polymer deposit is sent to the dryer to dry the remaining 21-2 detergent self-cleaning 1-9 clean polymer.

[0301] The dryer is typically a spray dryer, which sprays the precipitate to increase surface area and residence time, allowing evaporation in a heated chamber (21-2 detergent). In some embodiments, it may be another type of dryer, such as a centrifugal dryer or rotary dryer. Both operate by providing a high surface area and elevated temperature, allowing the remaining fluid to evaporate and form 1-9 clean polymer solids. 21-2 detergent is collected as vapor and flows to the outlet, although not always at the top, and 1-9 clean polymer solids fall to the end of the drying chamber, where they are expected to be further processed into 1-10 polymer products by the next unit, i.e., the molding machine. The gas outlet is then condensed and recycled back to the detergent tank. Note: 1-3 solids separation module has an auxiliary detergent tank, allowing recirculation of 21-2 detergent, saving costs and reducing the environmental footprint. 35-1 electrochemical reactor and scrubber are intended for 21-2 detergent, which is used as a reservoir to supply the double-use detergent.

[0302] 1-4 processing: The 1-4 processing module starts the process of molding the clean polymer powder, which is then shaped into the required polymer product. Different molding techniques are used depending on the type of polymer product. For long, cylindrical objects like plastic straws and wire, extrusion molding is typically used. For closed, hollow objects like bottles, blow molding is used. For some complex shapes, like statues and toys, injection molding is used. The clean polymer powder moves through the machine via a spiral transport or conveyor, but is not limited to this.

[0303] The finished 1-10 polymer products are then sent to a polymer packaging machine unit to be packed into sets. For example, plastic straws are counted and assembled into sets by the machine, for example, 100 sets. These combinations are then packed into bags, before being sealed by the machine. The sets are then sorted in bulk, either manually by workers or automatically by the machine, and trucks arrive to transport the goods for sale.

[0304] 1-5 Recovery 1-5 Recovery module, start switch valve guide 1-14 Waste electrolyte into two possible paths, according to -15 by-product type

[0305] a. Absorption unit If the 1-15 by-product is low-value and benign, such as water, the absorption unit can be used to separate the 1-15 by-product from the 1-14 waste electrolyte and simultaneously recycle the 1-7 electrolyte. The absorption unit typically consists of a self-absorber that separates the 1-15 by-product from the 1-14 waste electrolyte by absorption or chemical absorption. Typically, the 1-15 by-product is water, which is low-value and benign, and the absorption unit can be a dehumidifier, where the water is absorbed through some type of desiccant, such as calcium sulfate or magnesium sulfate. The desiccant is then recovered, usually without heating, to release the absorbed water as steam and minimize environmental impact.

[0306] In some embodiments, the absorption unit may be replaced by other conventional equipment, including a blow / spray dryer where the by-product is separated from the waste electrolyte and the stream is sprayed against hot air to evaporate the by-product.

[0307] b. Recovery of by-products 1-5 If some by-products 1-15 are 5-5 raw chemicals waiting to be recovered, such as 6-9 ammonia or some alcohols, which have double resale value and adverse environmental impacts, then recovery of the by-products 1-5 is usually more expensive, but absorption units are used to recover the 1-15 by-products instead of discharging them for resale.

[0308] The by-product 1-5 recovery pathway begins with the solvent extractor, where the by-product 1-15 is loaded with the waste electrolyte 1-14, awaiting separation. The solvent has selective solubility, and the by-product 1-15 flows into a separate inlet. In many cases, the incoming solvent and the incoming waste electrolyte 1-14 are typically arranged countercurrently for better separation efficiency; however, in some other embodiments, cross-current or parallel flow is used to accommodate specific situations.

[0309] Solvent extractors also typically involve mixing between the waste electrolyte and solvent phases. This is typically driven by a motor / engine via a mixer. In some embodiments, the motor and engine do not need to be physically connected to the fan via a shaft; rather, the movement of the fan blades can be indirectly affected. For example, the magnetic field is similar to that of a magnetic mixer. In some embodiments, changes in the magnetic field can trigger a self-inductor system, so a motor / engine is not even required. In some embodiments, hybrid systems can be completed without mechanical means, such as using ultrasound to vibrate molecules, or by generating turbulence in a static mixer using multiple rotation angles and barriers to mix and homogenize the materials, or by adding bubbling gas into the liquid phase to induce mixing. In some embodiments, turbulence is generated between the waste electrolyte and solvent phases by placing barriers or impingement through pipeline installation. The waste electrolyte and solvent streams are directed toward each other, enhancing mixing.

[0310] The resulting solvent, 1-15, then leaves the solvent extractor and enters a distillation column to separate the by-product 1-15, which is the self-solvent. The distillation column is typically a column, or may be fitted with a distillation column, distillation packing, or distillation tray / plate. A reboiler is located at the bottom, providing the necessary heat energy for distillation 1-11, and a condenser is located at the top. The reboiler is typically a heater, but in some embodiments, the reboiler can be other heating methods, such as a thermal switch carrying hot steam, hot water, or hot oil. The condenser is typically a heat exchanger with a coolant such as water, but in some embodiments, it can be a chiller.

[0311] However, the locations where the solvent and by-product 1-15 leave the distillation column are quite unique compared to each other in the boiling points of the 5-1 ElerGreen process, which allows for flexibility. The 7-6 pipelines are located at the top and bottom. The top outlet of the column contains concentrated low-bound components, i.e., substances with lower boiling points, while the bottom outlet contains concentrated high-bound components, i.e., substances with higher boiling points. In many cases, the solvent, despite being a low-bound component, leaves the top, while the by-product 1-15, a high-bound component, leaves the bottom. In other cases, the opposite occurs, with the solvent leaving the bottom and the by-product 1-15 leaving the top.

[0312] At the top outlet, there is a switching valve that guides the top into these two paths. a. If the top is 1-15 by-product, the top is directed to the switching valve 1-15 by-product tank b. If the top is solvent, it is directed to another selector valve and leads to the solvent pickup.

[0313] There is also another switching valve at the bottom outlet, which guides one of two paths from bottom to bottom. a. If the top is 1-15 by-product, the bottom is directed to the switching valve 1-15 by-product tank b. If the bottom is solvent, this is directed to another selector valve and leads to the solvent pickup.

[0314] The 1-15 by-product is then stored in containers, usually cans, for convenient sale. The 1-15 by-product tanks are then transported to chemical tank trucks for sale. The solvent is then circulated back to the solvent extractor, completing the 1-5 recovery process.

[0315] The remaining separation is due to the effect of the 1-15 by-product. The 1-15 by-product 1-5 recovery can be performed in other separation units, such as dialysis, filtration, and precipitation, based on the properties and interactions of the 1-15 by-product and the 1-7 electrolyte. The 1-7 electrolyte is removed from the 1-15 by-product, except for the 1-15 by-product unit or the 1-5 recovery by-product, which then passes through another selector valve before being recycled to the mixing tank.

[0316] Implementation and the 7-6 Pipeline As shown in Figure 40, the 7-6 pipeline consists of 40-1 process flow diagram and auxiliary units, 40-2 pipeline type, 40-3 pump / compressor, 40-4 heater / cooler, 40-5 facility, and finally 40-6 valve.

[0317] 40-1 Process flow diagram and auxiliary units The process flow diagram and auxiliary units for carrying out the 7-5 process are detailed in Figure 41. The following are the equipment required to carry out the 7-5 process:

[0318] The 7-5 process begins with Supply Tank A, T-01A. Supply Tank A has a feed port, usually not necessarily at the top of the tank, through which supplier trucks can transport Material A via the 7-6 pipeline. This tank also has a drain port, usually not necessarily at the bottom. Material A is drained via Stream 59-3 for occasional use, such as maintenance and debugging. Stream 1A, primarily containing Group A, leaves T-01A and enters Mixing Tank M-02, whose flow rate is controlled by an in-line valve, V-01A.

[0319] In some embodiments, another raw material, e.g., Material B 68-2, is required. In this case, another receiving tank B, T-01B, is connected in parallel to Supply Tank A, T-01A. Similar to Supply Tank A, Supply Tank B has a feed port, usually not necessarily at the top of the tank. Supplier trucks can transport Material B 68-2 through the 7-6 pipeline. This tank also has a drain port, usually not necessarily at the bottom of the tank. Emptying Material B 68-2 is used for emergency purposes, e.g., maintenance and debugging 59-3. Stream 1B, primarily containing Group B, leaves T-01B and enters the mixing tank M-02, whose flow rate is controlled by an in-line valve, V-01B.

[0320] In some embodiments, particularly complex conjugation reactions require more raw materials, such as materials C, D, E, and F. For these situations, process 7-5 simply adds these feed tanks, connected in parallel to feed tank A, labeled T-01A. 7-6 uses pipeline and connection structures similar to those for feed tank A and feed tank B, but uses substitute materials labeled C, D, E, E, etc.

[0321] The first support unit is the flux tank, D-00A. Unlike raw materials, 31-1 cosolvent is consumed more slowly, so a small and convenient storage tank is used. Although an inlet is installed, 31-1 cosolvent is transported through the supply tank, which may not be necessary for small storage volumes. The tank resembles a can, with a vent hole. The vent hole also has a vent hole. The space 31-1 cosolvent is used for emergencies, such as maintenance and debugging. Stream 0A, which mainly contains the group 31-1 cosolvent, leaves D-00A and enters the mixing tank, M-02. Its flow rate is controlled by an in-line valve, V-00A.

[0322] Another support unit is the additive tank, D-00B. Similar to the 32-1 additive, 31-1 cosolvent differs from the raw material in that consumption is slower. Therefore, a small and convenient storage tank is used. Although an inlet is provided, 32-1 additive is transported through the supply tank; for small storage volumes, this may not be necessary. Similar to a can, the groove also has an exhaust port, though it is usually not necessarily at the bottom. Emptying 32-1 additive is used for occasional purposes, such as maintenance and debugging. Stream 0B, primarily containing Group Z, is 32-1 additive, leaving D-00B and entering the mixing tank, M-02. Its flow rate is controlled by an in-line valve, V-00B.

[0323] The mixing tank, M-02, has inlets 1A, 1B, 0A, and 0B, as previously mentioned. It also has another inlet. Stream 2R acts as a recirculation for the electrolyte stream 1-7, recovering 1-5, as detailed in the electrolyte section. The principle of mixing the streams, 1B, 0A, 0B, and 2R, is typically not necessarily mechanical, e.g., a motor or engine-driven mixer. In some embodiments, mixing can be non-mechanical and / or non-agitating, e.g., using air through a styrofoam container, or using ultrasound to induce liquid mixing through molecular vibrations.

[0324] The mixed electrolytes 1-7 leave the mixing tank and are sent as Stream 2 (M-02), containing Groups A, B, S, Y, and Z. The intermediate component S is the 68-3 salt / solute. The temperature of Stream 2 is controlled by an in-line heater (H-02). In some embodiments, the heater may be replaced by other methods to control the temperature of the stream, such as a heat exchanger or refrigeration unit. Meanwhile, the pressure of Stream 1-12 and Stream 2 are controlled via an in-line compressor (Q-02), and its flow rate is controlled by an in-line valve (V-02). In some embodiments, the compressor can be replaced by a pump to reduce costs. The flow direction of Stream 2 can be either 1-2, a conventional reactor (CR-03A), or 35-1, an electrochemical reactor (ER-04), and is controlled by an in-line valve. S-03A, which is typically, but not necessarily, designed to repel each other, means that stream 2 can only flow to one of two conventional reactors, CR-03A, or 35-1 electrochemical reactors, ER-04, one at a time but not two simultaneously. In some embodiments, a diverter valve can replace a three-way valve to allow use with a conventional electrochemical unit, particularly when a 34-3 retrofit is involved, which can result in revenue interruption, as is the case when retrofitting a 34-3 conventional polymer plant.

[0325] The conventional reaction stream (42-1) exits the reactor (42) and passes through the selector valve (S-03A). After passing through the selector valve (S-03A), flow 2 enters the conventional reactor (CR-03A) (1-2), where the polymerization reaction occurs using heat energy (1-11) and pressure (1-12) to form polymer (P) (1-8) and by-product (H) (1-15). According to process conditions (7-5), process safety measures (7-5) can be applied to the conventional reactor (1-2), such as pressure-resistant reactor walls and a coolant (usually, but not necessarily, water) to prevent overheating. The pressure relief valve (1-12) is also opened to release pressure to prevent explosions if the pressure becomes too high for some reason. Although the conventional reactor (1-2) is a stirred tank, mixing in the conventional reactor (1-2) can be achieved mechanically by a motor / engine-driven mixer, or by other methods, such as ultrasonic waves, which induce molecular vibrations and drum-gas bubbles in the liquid mixture.

[0326] The reactive mixture, stream 3A, containing the remainder of materials A and B (68-1), dissolved salts / solutes S (31-1), cosolvent Y (32-1), additive Z (32-1), and the resulting polymer P and by-product H (1-15), leaves reactor 1-2 (CR-03A). If pressure in reactor 1-12 drops significantly, it is re-elevated. Stream 3A is then pumped through pump P-03A and then passes into the filter. Stream 42-2, the conventional solids stream, passes through CF-03B, of which the solid polymer P is the self-filtered reaction mixture. Stream 3B then passes through selector valve S-03B, leaving filter CF-03B. Stream 42-3 is the conventional mixture stream.

[0327] The electrochemical reaction stream (43-1) is shown in Figure 43. After passing through selector valve S-03A, it enters electrochemical reactor ER-04 (35-1) instead of stream 2. When voltage (6-5) is applied (using heat energy (1-11) and pressure (1-12), if necessary, but not usually necessary), it forms polymer P (1-8) and by-product H (1-15). Depending on process conditions (7-5), process safety measures (7-5) may be applied to electrochemical reactor 35-1, such as the use of a coolant (usually, but not necessarily, water) to prevent overheating. Gas removal and collection of escape gases (9-17) are also required. For example, hydrogen and oxygen are decomposed from water, and typically form a mixture when water is the primary component. While mixing can occur by moving the electrolyte fluid relative to the electrode surface (1-7), additional mixing can be achieved by a mechanical mixer driven by a motor / engine, ultrasonic waves, or non-mechanical means such as passing a foaming gas through the mixer.

[0328] For the 35-1 electrochemical reactor, the 9-17 gas removal setup begins with the intake of 4 L of ambient air. The main component is air U entering the 35-1 electrochemical reactor volume. The gas outlet of the 35-1 electrochemical reactor is stream 4 H, which is mainly composed of air U and some deviated gas G. Blower B-04 is used to drive air blowing 4 H, and at the same time, it drives a 4 L flow to act on the ambient air by intake.

[0329] The formed 1-8 polymer P is recovered in the vapor phase from 35-1 electrochemical reactor and then transported to the washing stage, passing through 43-2 electrochemical solids stream. The detergent inlet 21-4 flows from detergent tank T-05B to 35-1 electrochemical reactor ER-04, where the removed solids are developed through controlled valve V-04. 1-8 polymer P remains in suspension in 21-2 detergent, which leaves 35-1 electrochemical reactor ER-04 and passes through 21-5 detergent outlet and selector valve S-04 to become Stream 4. Stream 4, consisting mostly of 21-2 detergent (usually but not exclusively water) and the solid 1-8 polymer P suspension, then enters WP-05A scrubber. While this is a common route, it also merges with the washing stage via switch valve S-04, which is the same as the electrochemical route.

[0330] In the WP-05A scrubber, except for inlet stream 4, the inlet is 21-2 detergent (5B), which is mostly composed of 21-2 detergent (W), and its flow rate is controlled via in-line valve V-05B. The scrubber is typically equipped with a mixer, but is not limited to motor / engine-driven mixing. Mixing can also be achieved by other methods, such as ultrasonic waves, which induce molecular vibrations and the introduction of drum-shaped bubbles. The washing action is caused by the solid suspension mixing between 1-8 polymer P and 21-2 detergent W, and the adsorption or absorption of 1-14 waste electrolyte dissolves from 1-8 polymer P particles in 21-2 detergent W. The outlet is 5A, and the self-floating 1-8 polymer P has a small (acceptable) amount of adsorption / absorption of 1-14 waste electrolyte, and 21-2 detergent has a small amount of dissolved 1-14 waste electrolyte. The flow rate is controlled via in-line valve V-05A.

[0331] Flow 5A then enters precipitator SP-06 to further separate the solids (1-9 clean polymer P and 21-2 detergent W). Precipitators typically do not have a large holdup capacity; the 1-9 clean polymer P suspension settles to the bottom of the tank and separates out, allowing gravity to pass through. In a typical unspecified configuration, the 21-2 detergent W outlet is located at the top of the tank and the 1-9 clean polymer P outlet is located at the bottom, allowing gravity to pass through the correspondingly concentrated solution. In some embodiments, some 32-1 additive is used as a coagulant. 21-2 detergent W flows through 6B, which is then recycled to detergent tank T-05B. For stream 6B, the flow rate is controlled by in-line valve V-06B, and pump P-06B is typically required due to the low pressure of 21-2 detergent 1-12 at the top of the tank. 1-9 Clean Polymer P, thickened by precipitation, then enters dryer DP-07 via stream 6 A, the flow rate of which is controlled via in-line valve V-06 A.

[0332] In dryer DP-07, stream 6A, primarily consisting of 1-9 clean polymer P suspension and a portion of 21-2 detergent, is heated and sprayed into the drying chamber. Heating can be performed before spraying, or hot air can be blown into the drying chamber, or both. The term "drying chamber" refers only to the volume of the dryer's container; it must be tall enough for 21-2 detergent to evaporate and then drop the mixture into the drying chamber. The drying chamber has an outlet, usually but not necessarily at the top of the chamber, that collects the vapors from 21-2 detergent and passes through stream 7B, the flow rate of which is controlled via in-line valve V-07B. The condensed liquid then passes into condenser X-07B, typically via a heat exchanger (though a chiller is possible in some embodiments). The condensed stream 7B, like stream 6B, is then recycled to the detergent tank T-05B. The dry clean polymer 1-9 is collected at the bottom and mechanically conveyed to the molding machine via stream 7A. In stream 7A of the molding machine, the mostly dry clean polymer powder 1-9 is mechanically conveyed to the mold via stream 7A and enters the molding machine. The mold then enters the molding machine. The molding machine applies thermal energy to melt the clean polymer powder 1-9, producing the desired shape of the polymer product 1-10. Depending on the desired shape, different molding techniques are used. For example, air-blowing molding is used for bottles or seals. Extrusion molding is used for long column shapes like plastic wire or straws, while injection molding is used for solid shapes. These are general guidelines, but are not completely limiting. For example, for short column shapes, both double extrusion and injection molding are applicable. The formed polymer product 1-10, made from stream 1-8, is then mechanically conveyed to stream 8 and enters the polymer packaging machine unit PP-09.

[0333] The formed 1-10 polymer products are sorted and packaged in the polymer packaging machine PP-09, usually not limited to an automatic arm method (a cheaper option is to hire workers to sort and package them manually). The packaged 1-10 polymer products are then stored as bulk inventory and await truck delivery for sale.

[0334] The auxiliary unit recirculates detergent 21-2 from detergent tank T-05B. For detergent 21-2, the facility water 40-5 is selected through 5H, usually located at the top of the tank, but not necessarily at the bottom. The flow rate is controlled through in-line valve V-05H. There is also a 5L outlet, usually located at the bottom of the tank. The flow rate is prevented from passing through stop valve C-05L by in-line valve V-05L and return valve C-05L. Detergent 21-2 is supplied from detergent tank T-05B to washer WP-05A via 5B as previously mentioned. Recirculation is also involved from streams 6B and 7B, affecting the 7-5 process to reduce costs and environmental impacts.

[0335] There is another auxiliary unit, namely, the coolant system, which comes from the central coolant tank D-16. The coolant tank D-16 is supplied with Stream 16C, its flow rate controlled via in-line valve V-16C. Similar to a can, the channel also has a vent, usually not necessarily at the bottom, for discharging the coolant. It is used for emergency maintenance and debugging purposes (see Example 59-3). The first outlet is Stream 7C, its flow rate controlled via in-line valve V-07C to condenser X-07B for cooling. The second outlet is Stream 13D, its flow rate controlled via in-line valve V-13D to condenser X-13C for cooling. The double stream 7C combines with Stream 13D to form Stream 16A, which enters thermal switch X-16A before being recycled to the coolant tank D-16. Heat exchanger X-16 A acts as a cooling fluid, typically cooling the air by refrigeration. Ambient air is blown into stream 16 B, the flow rate of which is controlled via in-line valve V-16 B, and the warmed air discharge is vented to ambient air.

[0336] The waste electrolyte 1-14, 3 B, and the remaining materials 68-1 A and B, 68-3 S, 31-1 Y, 32-1 Z, and 1-15 H, including the dissolved salt / solute, are discharged. The remaining materials are then discharged to the electrochemical reactor ER-04 via the switching valve S-03 B. The remaining materials are then discharged to the electrochemical hybrid reactor 43-3.

[0337] Stream 3B, flowing from either the conventional or electrochemical route, enters Pump P-03B, where the pressure in Stream 1-12 increases (usually after leaving either the conventional reactor 1-2 or the electrochemical reactor 35-1). Its flow rate is controlled via Valve V-03B. Its flow rate is also controlled via Valve V-03B, which then flows to either the SB-10A adsorption unit or the XB-11 solvent extractor. The in-line switching valve, S-10A, is typically, but not necessarily, designed to mutually exclude the streams. This means that Stream 3B can only flow to either the SB-10A adsorption unit or the XB-11 solvent extractor, one at a time, but not both. In some embodiments, the switching valve is replaced with a three-way valve to allow the adsorption unit and the solvent extractor to operate in parallel. This can cause revenue interruptions, especially when retrofitting Stream 34-3, which is necessary when retrofitting a conventional polymer plant.

[0338] The absorbent stream 45-1 is shown in Figure 45. After passing through the switching valve S-10A, Stream 3B enters the absorbent unit SB-10A, where by-product H is separated from the waste electrolyte 1-14 and then transferred to the absorbent, usually via absorption or sorption. The absorbent can be any suitable solid material, including but not limited to silicon dioxide or alumina, for absorbing / adsorbing water. The absorbent can be replaced between maintenance periods 59-3 or switched to continuous operation. The recovered electrolyte 1-7 leaves the absorbent unit SB-10A and flows through the switching valve S-10B to Stream 11B.

[0339] For continuous operation, the absorbent is attached to the conveyor unit 9-11 between the suction unit SB-10A and the absorbent regenerator SR-10B. Flow 10A, consisting primarily of absorbent V and absorbent / absorbent byproduct H, is fed to the absorbent regenerator SR-10B. The absorbent regenerator SR-10B typically releases absorbent by intensely heating the absorbent, which may or may not be absorbed byproduct H. The released byproduct H is then discharged to the ambient air if it is benign, e.g., water vapor. In some embodiments, the released byproduct H is first wiped, e.g., when it contains ammonia 6-9, before being released to the ambient air. Flow 10B, consisting mostly of recovered absorbent V, is then recycled to the absorbent unit SB-10A.

[0340] The solvent extraction flow for 44-1 is shown in Figure 44. After passing through selector valve S-10A, flow 3B enters solvent extractor XB-11, where byproduct 1-15, H, is separated from the waste electrolyte 1-14 and the solvent phase. The solvent phase enters as stream 13B, primarily consisting of autosolvent X. The pressure is increased by a wire pump P-13B before entering solvent extractor XB-11, and its flow rate is controlled via valve V-13B. The solvent phase leaves as stream 11A, primarily consisting of autosolvent X and byproduct 1-15, H, whose flow rate is controlled via valve V-11A. The recovered electrolyte 1-7 leaves solvent extractor XB-11 and then passes through selector valve S-10B to stream 11B.

[0341] The solvent extractor has a support unit, solvent tank D-12, which regulates the solvent retention level. Unlike raw materials, solvent consumption is more gradual, so a small and relatively convenient storage tank is used. Although an inlet is installed, the solvent is transported through a supply tank; for small retention volumes, this may not be necessary. Similar to a can, the groove also has an exhaust port, although it is usually not necessarily at the bottom. It can be used for emergency purposes, such as draining solvent (59-3 maintenance and debugging). Stream 12A flows from solvent tank D-12, mainly comprising solvent X. Its flow rate is controlled by valve V-12A, and reflux is prevented from passing through stop valve C-12A. Excess solvent flows through 12B, mainly comprising solvent X. Its flow rate is controlled by valve V-12B and reflux is prevented from passing through stop valve C-12B, leaving the solvent extractor XB-11 and entering solvent tank D-12.

[0342] In the solvent extraction process, downstream of distillation column DB-13, 1-15 by-product H is purified in solvent extractor XB-11, and solvent X is simultaneously recycled. Stream 11A, consisting mainly of 1-15 by-product H and solvent X, enters distillation column DB-13 and solvent extractor XB-11.

[0343] A distillation column is made up of materials throughout the tower, usually including but not limited to distillation packing and distillation trays.

[0344] At the bottom of the column is distillation column DB-13, which is connected to reboiler H-13L, a device typically used for heating (but not necessarily a heat exchanger). The bottoms stream is split into two streams: one enters reboiler H-13L and the other passes through selector valve S-13L. Stream H-13L is heated by reboiler H-13L, allowing it to heat the remaining streams. The heat is transferred to distillation column DB-13, whose flow rate is controlled via valve V-13L. The other stream passes through selector valve S-13L and is then directed to one of two paths: to selector valve S-13B or selector valve S-13A. When directed through the selector valve S-13B, this is recycled back to the solvent extractor XB-11 as Stream 13B, of which the pressure is increased by 1-12. The flow rate is controlled by the pump P-13B and through the valve V-13B, as demonstrated in Figure 46. When directed through the selector valve S-13A, this enters the sub-product tank TB-14 and is stored as Stream 13A. The flow rate is controlled by the valve V-13A, as demonstrated in Figure 47. Stream 47-2 is the bottoms tank.

[0345] Above the distillation column DB-13 is a condenser X-13C, usually a hot switch (although not necessarily a chiller, which can also be used) that cools the column and the fluids inside. The top stream, Stream 13C, primarily consists of by-product 1-15. After passing through Condenser X-13C, it is split into two streams: one into distillation column DB-13 and the other through Switching Valve S-13H. Flow 13H's flow rate is controlled via Valve V-13H before being recycled to distillation column DB-13. The other stream then passes through Switching Valve S-13H and is directed to either Switching Valve S-13B or Switching Valve S-13A. When directed to selector valve S-13B, it is recycled to solvent extractor XB-11 as stream 13B, of which the pressure is increased by 1-12. The flow rate is controlled by pump P-13B and through valve V-13B, as previously described. The upper solvent stream is shown in Figure 47-1. When directed to selector valve S-13A, it enters sub-product tank TB-14 and is stored as stream 13A. The flow rate is controlled by valve V-13A, as shown in Figure 46-1. The upper tank flow is shown.

[0346] The by-product route ends at the by-product tank, TB-14. By-product tank TB-14 is used for export. By-product 1-15 is loaded onto trucks and sold through pipelines 7-6. This outlet also serves as a drainage outlet. By-product 1-15 is used for incidental purposes, such as maintenance and debugging.

[0347] The recovered 1-7 electrolyte passes through selector valve S-10B, then combines with Stream 15B in storage tank T-15, where it merges with Stream 11B. Storage tank T-15 serves to regulate the level in mixer M-02. This tank also has a drain, usually (but not necessarily) at the bottom of the tank. Material A is drained from 68-1 for contingency purposes, such as maintenance and debugging. Stream 15B leaves tank T-15, usually (but not necessarily) from the bottom of the tank, with its flow rate prevented from passing through stop valve C-15B by in-line valve V-15B and reflux. The tank's inlet is 15A, usually (but not necessarily) from the top of the tank, with its flow rate prevented from passing through stop valve C-15A by V-15A and reflux.

[0348] After Stream 11B is combined and formed, the pressure in 1-12 becomes high (so the pressure in 1-12 may become very low after consecutive operation units) through Pump P-11B, and its flow rate is controlled through Valve V-11B. Stream 11B is then split into Stream 15A for recirculation into Tank T-15, and then recycled to Mixing Tank M-02 along with Stream 2R. Stream 2R's flow rate is controlled through Valve V-02R, and its reflux is prevented from passing through Stop Valve C-02R. This closes the recirculation circuit, ensuring cost-effectiveness and a low environmental footprint for the 1-7 electrolyte 7-5 process.

[0349] 40-2 Pipeline Type Insulation is implemented for hot and cold streams. This is usually a layer of material with low thermal conductivity wrapped around the outer wall. For the process of interest, insulation is used for the 2 streams between H-02 and ER-04 and CR-03 A of the 35-1 electrochemical reactor. Stream 13 C is located between DB-13 and S-13 H. Stream 13 H is located between X-13 C and DB-13. Stream 13 L is located at DB-13 and between H-13 L and S-13 L.

[0350] Alternatively, this equipment may be insulated. CR-03A, DP-07, DB-13, MP-08, SB-10A, and SR-10B may require insulation. In some embodiments, the 35-1 electrochemical reactor ER-04 may be insulated. The above is one embodiment of this process; other equipment may also be insulated, or higher temperature operation may be required.

[0351] Mechanical lines are used to transport solids, such as powders or well-defined shapes. In some embodiments, the mechanical lines are conveyors 9-11, which are installed to continuously transport powders or solids. In some embodiments, the mechanical lines can include worms or robots. The speed of such transport depends primarily on the speed at which the mechanical circuits are driven, e.g., the rotational speed of the wheels of conveyor 9-11. For the process of interest, mechanical lines are used for streams 7A and 8, which consist of 1-9 clean polymer powder and 1-10 polymer product, respectively. Meanwhile, streams 10A and 10B are also constructed from mechanical lines.

[0352] 40-3 Pump / Compressor For electrochemical production in the 5-1ElerGreen process, the 40-3 pump / compressor is typically deployed at high pressures or flow rates when a certain flow is required.

[0353] In contrast to the 7-5 process safety, many 40-3 pump / compressors have two 40-6 valves installed at the pump. One valve is upstream, before the 40-3 pump / compressor, and the other is downstream, after the 40-3 pump / compressor. These valves are usually controlled, and the previous valve is usually fully open. The controlled valve is after the pump, while the control valve before the pump can cause fluid starvation and pump damage due to cavitation. In some embodiments, the upstream valve can be omitted to save process costs without significantly affecting process safety.

[0354] In some embodiments, a compressor is used instead of a pump, especially when high pressure is required. For example, the pressure of Stream 2 is controlled by an in-line compressor, Q-02. In some other embodiments, the compressor is replaced by a pump to reduce costs.

[0355] Pumps P-03A, P-03B, P-06B, P-11B, and P-13B are used. P-03A is used to increase the pressure of Stream 3A, which may be significantly reduced when leaving either a conventional reactor or, in the case of an electrochemical reactor, 35-1. P-03B is used to increase the pressure of Stream 3B. P-06B is used to increase the pressure of Stream 6B because the pressure of Stream 21-2 is lower at the top of the tank. P-06B is used to increase the pressure of Stream 6B because the pressure of Stream 21-2 is lower at the top of the tank. P-11B is used to increase the pressure of Stream 11B because the pressure of Stream 1-12 can be very low after a continuous operation unit. P-13B is used to increase the pressure of Stream 1-12, which would cause a huge pressure drop to provide the pressure required for the solvent extractor, which passes through many stages before entering the solvent extractor.

[0356] In some cases, additional pumps can be added to the flow to increase pressure or flow rate. This is due to process safety considerations. If the pressure of the liquid is lower than its boiling point, depending on which part of the flow is in the flow, this part will cavitate and the liquid will evaporate. Cavitation is a problem. Evaporation and condensation of the liquid will cause pressure fluctuations in the flow, damaging the system and, for example, deforming or bursting pipes and 40-6 valves after their useful life has expired.

[0357] The blower is a type of pump for driving the flow and generates its own gas. The blower is used in B-04 and B-16 B, which respectively sucks in air and removes the escaping gas along with the escaping gas, and blows the air to flow and recover the coolant.

[0358] 40-4 heating machine / cooling machine 1-11 Thermal energy may be in different forms, such as heaters, steam, or heat exchangers. Heaters can take a variety of forms, including but not limited to electric and combustion heaters. In some embodiments, alternatives include solar or geothermal heaters.

[0359] For the process of interest, heaters H-02, H-13L, and H-2 are used to preheat the conventional reactor CR-03A and heat stream 13L to facilitate distillation. H-13L, commonly referred to as a reboiler, is located at the bottom of distillation column DB-13 and heats the mixture for distillation. In some embodiments, either H-02 or H-13L may be used in place of a heating agent in a heat exchanger to perform a similar heating function.

[0360] DP-07 also has an internal heater that heats Flow 6B to accelerate drying, 1-9 clean polymer, and SR-10B to heat the sorbent and remove the by-product, self-sorbing agent. In some embodiments, the heater is used instead of controlling the temperature within the stream by other means, such as a heat exchanger. In some embodiments, either 1-2 conventional reactor CR-03A or 35-1 electrochemical reactor ER-04 may have an internal heating unit.

[0361] Steam is commonly employed as a heating medium, and steam heating is often used for domestic use in some cold climates, particularly in 40-5 installations. While conventional steam-heated 40-5 installations are possible, in some embodiments steam heating is used in specialized heat exchangers depending on the process.

[0362] The hot switch, on the other hand, can be used for heating or cooling, depending on the heat exchanger used, which is hotter or colder than this stream. The coolant is typically but not limited to 40-5 facility water, which has low cost and a low environmental footprint. In some embodiments, the coolant can be other fluids, such as ammonia or heat exchange oil, depending on the process requirements. For the process of interest, heat exchangers X-07 B, X-13 C, and X-16 A are used as coolers to condense Stream 7 B, Stream 13 C, and Stream 16 A, respectively. For X-07 B, the coolant, typically but not limited to 40-5 facility water, is used to cool and condense Stream 7 B of 21-2 detergent vapor into Artificial Dryer DP-07. For X-13 C, the coolant, typically but not limited to 40-5 facility water, is used to cool and condense the distillation vapor from above to Distillation Column DB-13, where Stream 13 C serves as a reflux condenser. For X-16 A, a coolant, typically but not limited to 40-5 facility water, is used to cool coolant stream 16 A before being recycled to coolant reservoir D-16.

[0363] If lower temperatures are required, a chiller can be used instead of a heater. Chillers can take various forms, including but not limited to cooling towers, refrigerants, or heat exchangers. For cost considerations, the process of interest may use a heat exchanger as a means of cooling, resulting in a lower energy cost for the refrigerant. Chillers may also be used for safety purposes to prevent overheating of the equipment. In some embodiments, the 1-2 conventional reactor CR-03 A incorporates a cooling cover to prevent overheating. In some embodiments, the 35-1 electrochemical reactor ER-04 may also have a cooling cover attached to the vessel wall.

[0364] 40-5 facilities The 40-5 facility configuration consists of 40-5 facilities for electricity, 40-5 facilities for water and other 40-5 facilities.

[0365] Electrical power, typically in the form of electricity, is required to power the entire process. This is required to power many devices in the process, including the CR-03A, 35-1 electrochemical reactors ER-04, CF-03B, M-02, WP-05A, DP-07, MP-08, PP-09, SR-10B, XB-11, and DB-13. For example, the 35-1 electrochemical reactor requires electricity to drive the electrochemical polymerization reaction. Mechanical components, such as the 4-1 dynamic electrode, the B-04 ventilation cabinet blower, and the 9-14 retractable bracket, are also required. The 40-5 facility also requires power to power the 40-3 pumps / compressors, the 40-4 heaters / coolers, and the process control system.

[0366] 40-5 facility water has many uses, including as a heat exchanger, containing 21-2 detergent. Depending on the process of interest, 40-5 facility water can be used as a 21-2 detergent to wash 1-8 polymers, 1-9 clean polymers, or as a coolant in heat exchangers, both of which benefit from availability, low cost, and low environmental impact. In some embodiments, the 21-2 detergent and coolant are not necessarily water. For example, organic 21-2 detergents can be used, such as ethanol. Alternative coolants can include 6-9 ammonia, which also has a high specific heat capacity.

[0367] Other facilities include 40-5 facilities that use non-aqueous heat exchangers and non-aqueous 21-2 cleaners, or any other form of heat exchanger. Steam heating, often used for domestic heating in cold climates, is also recognized as a certified facility. Other common types of 40-5 facilities include fuel supply, such as methane gas, used for combustion. In some embodiments, hybrid fluids, such as nitrogen gas or other chemicals, whether liquid or gas, are supplied through 40-5 piping for specific process purposes, such as scrubbing the piping.

[0368] 40-6 valves There are different types of 40-6 valves available for use in the process of interest, including on-off valves, control valves, diverter valves and stop valves.

[0369] On-off valves are used instead of control valves to save costs when flow rate control is not required. For processes of concern, such as bottom cavitation, the valve is used to open and close the bottom outlets of D-00A, D-00B, T-01A, T-01B, T-15, D-12, TB-14, and D-16. This is when the vessel is emptying, so precise flow rate control is generally not required; the goal is to always empty the vessel. Considering relatively large vessels, the operator can continuously discharge the vessel without flow rate control, and turn the valve off to reach the required vessel level. In some cases, an emptying valve may be required. On the other hand, PP-09 does not have an outlet, because it is a solid polymer product (1-10), and is mechanically mounted (manual or robotic) on a vehicle.

[0370] In some embodiments, an on / off valve can replace a control valve when in position, allowing for more precise control of flow. The 40-6 valve is designed to provide more precise control of partial closure, closing this portion to achieve the required flow. The degree to which the portion is closed can be controlled manually by an on-site operator or remotely through a central control system. Control valves are widely used in processes that require precise flow control among many streams, namely, V-00A, V-00B, V-01A, V-01B, V-02R, V-02, V-03A, V-03B, V-05B, V-04, V-05A, V-06A, V-06B, V-05H, V-05L, V-07B, V-07C, V-11A, V-11B, V-13B, V-13H, V-13L, V-13A, V-15A, V-15B, V-13D, V-16B, V-16C, where the number corresponds to the stream number and its flow rate to be controlled.

[0371] Check valves are installed in several streams to prevent backflow, which could cause contamination. Stop valves allow reflux into the streams and have process consequences, particularly C-02R, C-05L, C-12A, C-12B, C-13A, C-13B, C-15A, and C-15B. These stop valves are used to prevent backflow into the corresponding streams, namely Recycle Stream 2R, which drains 5 L from the Detergent Tank, Solvent Tank D-12 Outlet Stream 12A, Solvent Tank D-12 Inlet Stream 12B, By-Product Tank TB-14 Inlet Stream 13A, Solvent Extractor XB-11 Solvent Inlet Stream 13B, Electrolyte Reservoir T-15 Inlet Stream 15A, and Electrolyte Reservoir T-15 Outlet Stream 15B. In some embodiments, additional stop valves may be added to other streams to provide additional process safety; these additional stop valves incur additional costs.

[0372] Switching valves are typically used to control three-way flow in a specific direction. They can be used to direct flow, especially in a mutually exclusive manner, so that only one path can flow at a time, rather than all flowing together. Switching valves are used in a variety of applications, including S-03A, S-03B, S-10A, S-10B, S-13H, S-13L, S-13A, and S-13B. Switching valves are used to diverge between two different options. For the purpose of 34-3 modification, this switching valve usually appears as a pair, one divergence and one convergence, to achieve 34-3 interlock modification, including S-03 A and S-03 B modification for 35-1 electrochemical reactor, S-10 A-10 B pair is modified for 1-5 recovery unit, S-13 H and S-13 L pair are used to reverse the distillation column pipeline and the last S-13 A-13 B to reverse the flow between by-products and solvent.

[0373] In some embodiments, additional switching valves may be added to the streams to switch flow between alternative streams. In some embodiments, switching valves can replace three valves to operate two pathways in parallel. Selecting 34-3 is particularly important when retrofitting a conventional polymer plant, as this would result in revenue interruption.

[0374] Pressure relief valves are used to vent the vessel contents for safety reasons and to prevent the vessel from bursting if the vessel pressure exceeds a certain limit. For the process of interest, pressure relief valves are used in 1-2 conventional reactors, such as CR-03 A. In some embodiments, additional pressure relief valves may be used in other vessels when high pressures are involved.

[0375] Process 7-7 Control Process 7-7 control is outlined in Figure 48. Process 7-7 control is also detailed as a P&ID in Figure 49, with further explanatory diagrams and notes in Figure 50. 48-1 Stage, 48-2 Feedforward, 48-3 Feedback, 48-4 Scale, 48-5 Minute Course, and 48-6 Override Selection are combined to transfer any process to the stem, and 48-7 Indicator / Alarm allows the operator to respond accordingly.

[0376] 48-1 series 48-1 serial control is a 7-7 control method that combines two or more feedback circuits and outputs to a controller (main controller) with a secondary controller adjusting the set point. 48-1 serial level control provides a means of coordinating between different devices. 48-8 quick response during the 7-5 process.

[0377] Figure 51 shows a general overview of the 48-1 series level 7-5 process. The overall goal is to control the process 7-7, which is a new 5-1 Electric Green process, ensuring production at the required speed, especially for 1-8 polymer flow. The embodiment involves transmitting the mains to other parts and connecting them continuously, with the mains to the final point being accepted as a 48-14 mains reservoir. The 48-14 mains reservoir usually represents the tank level and energy consumption, which means the material consumption rate and 40-5 facility (water and 3-1 electricity) costs.

[0378] Set a point on SIC 07 A and then remotely control FIC 02 as the reference (via 48-6 override selection), flow meter controller Flow 2, IIC 04 (electrical) current indicator controller 35-1 electrochemical reactor ER-04, FIC 13A, rate indicator controller Stream 13 A, FIC 01A, rate indicator controller Stream 1 A is upstream and SIC 08 (operating) rate indicator controller downstream of molding machine MP-08.

[0379] SIC 10 B (Operation) Rate Indicator Controller controls Flow 3 B via Rate Indicator Controller in FIC 03 B. FIC 03 B, Rate Indicator Controller Stream 3 B sends a signal to FIC 11 B, whose Rate Indicator Controller is downstream.

[0380] Except for multiple stages, far beyond upstream and downstream, 48-1 serial level control is also used in smaller devices.

[0381] FIC 03A, the rate indicator controller for stream 3A, controls PIC 03B pressure indicator controller stream 3A, which in turn controls PIT 03B pressure indicator controller stream 3A to hold stream 3A at the set point. PIC 03B pressure indicator controller stream 3A also depends on downstream pressure PIT 04 pressure gauge transmitter stream 3B, which is held at the set point by PIT 04 pressure gauge controller stream 3B.

[0382] LIC 05 A level indicator controller cleaning device WP-05 A controls FIC 05 B flowmeter controller flow 5 B.

[0383] LIC 06 level indicator controller precipitator SP-06 controls dual FIC 05 A, flow rate indicator limiter flow 5A sum FIC 06B, flow rate indicator limiter flow 6B.

[0384] FIC 06A, Rate Indicator Controller Stream 5 A and FIC 06 B, Rate Indicator Controller Stream 6 B.

[0385] FIC 06B, rate indicator controller stream 6 B also controls PIC 06 B pressure indicator controller stream 6 B which in turn controls pump P-06 B at set point PIT 06 B pressure indicator stream 6 B.

[0386] FIC 11B, the rate indicator controller flow 11B also controls the pressure indicator controller flow 11B of PIC 11B, which keeps the pressure indicator transmitter stream 11B of PIT 11B at the set point and controls P-11B.

[0387] FIC 13B, rate indicator controller stream 13B also controls pressure indicator controller stream 13B of PIC 13B to maintain pressure indicator stream 13B of PIT 13B at the set point to control P- 13B.

[0388] 48-2 Feedforward 48-2 Feedforward is a method of controlling process parameters by measuring inputs and making corresponding adjustments, which has the advantage of 48-9 accuracy. 48-2 Feedforward is suitable when the parameter is a parameter with a fast response change and its interaction is not affected by complex factors.

[0389] Figure 52 shows a simple example of feedforward control used in a valve. The controller FIC 01 A receives a signal from the upstream FIT 01 A and then sends a signal to control the downstream V-01 A. The characteristic of feedforward control is that a signal is received from the upstream unit and sent to the downstream unit for response.

[0390] For electrochemical production, the 7-5 process, 48-2 feedforward is used for relatively predictable subsystems, such as flow rate, position, speed, current, and 6-5 voltage. Because there are many such subsystems, the 7-5 process, 48-2 feedforward is widely used.

[0391] For 31-1, the cosolvent stream is 0 A, FIC 00 A, the rate indicator controller flow is 0 A, FIT 00 A is held, and the rate indicator stream 0 A is the set point and goes through control valve V-00 A.

[0392] Pair 32-1 additive flow 0 B, FIC 00B, rate indicator controller 0 B, FIT 00 B, rate indicator stream 0 B is the set point and goes through control valve V-00 B.

[0393] For 68-1 Material A Stream 1 A, FIC 01A, Rate Indicator Controller Stream 1 A, FIT 01A is maintained, and Rate Indicator Stream 1 A is the set point, controlled by Control Valve V-01A.

[0394] For 68-2 material B flow 1 B, FIC 01B, flow meter controller flow 1 B, FIT 01 B, hold, rate indicator stream 1 B is at set point, via control valve V-01 B.

[0395] Prepared 1-7 electrolyte stream 2, FIT 02, rate indicator stream 2 set point is maintained via FIC 02, flow meter controller flow 2, its control valve V-02.

[0396] AIC 02 (component) analytical indicator controller is provided 1-7 electrolyte flow 2, used to keep AIT 02 (component) analytical indicator converter is provided 1-7 electrolyte flow 2, at set point.

[0397] Recycle inlet stream 2 R is metered by FIT 02 R and held at set point by rate indicator stream 2 R, selected by FIC 02 R, rate indicator controller stream 2 R, via control valve V-02 R.

[0398] For 1-2, conventional reactor outlet stream 3A is FIT 03A, rate indicator stream 3A is maintained at the set point through FIC 03A, flow meter controller flow 3A, and its control valve V-03A.

[0399] 1-2 normal reactor CR-03 A, SIC 03 A (agitation) speed indicator controller 1-2 normal reactor CR-03 A, control mixer, SIT 03 A, keep the agitation speed at the set point. 1-2 normal reactor CR-03 A, speed meter inverter

[0400] The level 1-2 normal reactor LIT 03 A, the level indicator transmitter 1-2 normal reactor CR-03 A, is maintained at the set point by LIC 03 A, and the level indicator controller 1-2 normal reactor CR-03 A.

[0401] For 1-15 by-product-1-7 electrolyte hybrid stream 3 B, FIC 03 B, flow meter controller flow 3 B, hold FIT 03 B, rate indicator stream 3 B flows through control valve V-03 B at the set point.

[0402] For 21-2 detergent inflow and 35-1 outflow electrochemical reactor stream 4, FIT 04, rate indicator stream 4 measures the inlet flow rate and is held at a set point by FIC 04, rate indicator controller stream 4 controls flow through V-04.

[0403] Meanwhile, the level is controlled by ER-04, LIT 04, level direction indicator transmitter 35-1 electrochemical reactor ER-04, LIC 04, level indicator controller 35-1 electrochemical reactor ER-04.

[0404] The 35-1 electrochemical reactor ER-04, EIC 04, voltmeter controller 35-1 electrochemical reactor ER-04, SIC 04, speedometer controller 35-1 electrochemical reactor ER-04, ZIP 04, and (razor) position indicator controller 35-1 electrochemical reactor ER-04, EIT 04 respectively control the voltmeter inverter 35-1 electrochemical reactor ER-04, SIT 04, speed indicator 35-1 electrochemical reactor ER-04, ZIP 04, and (razor) position indicator converter 35-1 electrochemical reactor ER-04.

[0405] Washed 1-9 clean polymer floating stream 5 A, FIC 05A, rate indicator controller stream 5 A is used to hold FIT 05 A, and rate indicator stream 5 A is at the set point, by control valve V-05 A.

[0406] The agitation speed is measured by the washer WP-05 A and is maintained at the set point by the speedometer converter SIT 05 A, which is connected to the speedometer controller SIC 05 A, which controls the mixer.

[0407] The staying level in the irrigator WP-05 A is measured by LIT 05 A and controlled by the level indicator transmitter irrigator WP-05 A and LIC 05 A, and the level indicator controller irrigator WP-05 A.

[0408] Regarding fresh 21-2 detergent, 5 B flows into the washer, FIC 05B, flow meter controller flow 5 B, FIT 05 B is used to maintain the flow, rate meter 5 B, at the set point, controlled by control valve V-05 B.

[0409] For 21-2 detergent flow 5B, AIT 05B, (component) analytical indicator flow 5B, measured 1-14 waste electrolyte concentration is in flow 5B, and (component) analytical indicator controller flow 5B through AIC 05B, which keeps the limit at the set point.

[0410] Fresh detergent is poured into the detergent tank and flows through the 5H, FIC 05H, the flow of the rate indicator controller 5H is maintained at FIT 05H in sequence, and the rate indicator stream 5H passes through the control valve V-05H at the set point.

[0411] Flow 5 L for discharge from detergent tank, FIC 05 L, rate indicator controller flow 5 L holds FIT 05 L, rate indicator stream 5 L controls V-05 L at set point.

[0412] The level of the clean polymer precipitates 1-9 is measured by LIT 06. The level indicator is controlled by the level indicator precipitator SP-06 and the level indicator controller SP-06.

[0413] For 1-9, clean polymer precipitate stream 6 A, FIC 06A, rate indicator controller stream 6 A, FIT 06 A is maintained, and rate indicator stream 6 A is the set point, controlled by control valve V-06 A.

[0414] For the above 21-2 detergent flows 6 B, FIC 06B, rate indicator controller 6 B is used to hold FIT 06 B, rate indicator stream 6 B is at the set point, by control valve V-06 B.

[0415] For 1-9 clean polymer powder stream 7A, SIC 07A, (conveying) speed indicator controller stream 7A holds SIT 07A, (conveying) speed meter transmitter stream 7A is at the set point. In fact, this is the key part 7-7 control.

[0416] For steam flow 7 B, FIC 07B, rate indicator controller flow 7 B holds FIT 07 B, and rate indicator stream 7 B passes through control valve V-07 B at the set point.

[0417] The refrigerant flow 7 C is condenser X-07 B, holds FIC 07C, flow meter controller flow 7 C, FIT 07 C, and rate indicator flow 7 C is at the set point, by control valve V-07 C.

[0418] The operating speed is the molding machine MP-08, SIC 08, the speed indicator controller molding machine MP-08 is used to control the SIT 08, the speed meter converter molding machine MP-08 is a direct method.

[0419] Operation speed is polymer packaging machine unit PP-09,SIC 09,speed indicator controller polymer packaging machine unit PP-09 controls packaging speed SIT 09,speed meter inverter polymer packaging machine unit PP-09.

[0420] For the absorbent regenerator SR-10 B, SIC 10B, (conveyor) speed meter controller absorbent regenerator SR-10 B, SIT 10 B is held, (conveyor) speed meter converter absorbent regenerator SR-10 B, and at the set point, it absorbs into the absorbent regenerator SR-10 B by controlling the motor / engine.

[0421] The agitation speed is supplied to the solvent extractor XB-11 by controlling the motor / engine at the set point.

[0422] LIT 11, the level indicator transmitter of the solvent extractor XB-11, measures the level of the solvent extractor, and maintains the set point through LIC 11, the level indicator controller of the solvent extractor XB-11.

[0423] For the solvent extraction stream 11 A, FIC 11 A, flow meter controller stream 11 A, FIT 11 A are held, and the rate indicator stream 11 A is at the set point, by control valve V-11 A.

[0424] 1-7 electrolyte flow 11B, 11B, flow meter controller flow 11B, FIT 11B, hold rate indicator stream 11B, at set point passes through control valve V-11B.

[0425] AIT 11B, analyzes Component Indicator Transmitter Stream 11B and is held at setpoint by AIC 11B, analyzes Component Indicator Controller Stream 11B.

[0426] For solvent supply 12 A, FIC 12 A, rate indicator controller stream 12 A, FIT 12 A, and rate indicator stream 12 A are maintained at the set point by control valve V-12 A.

[0427] For solvent overflow 12 B, FIC 12 B, rate indicator controller stream 12 B, FIT 12 B is held, and rate indicator stream 12 B is at set point, by control valve V-12 B.

[0428] The tank level is measured through LIT 13 and transmitted to the level indicator transmitter DB-13 of the distillation column, and maintained at the set point via LIC 13, which is connected to the level indicator controller DB-13 of the distillation column.

[0429] The number of feed layers is measured by ZT 13, the position indicator transmitter is fed to XB-13, which is held at the set point, and through ZIP 13, the position indicator controller is fed to XB-13, and the feed position by the control input is the distillation column XB-13.

[0430] For 1-15, by-product H stream 13A, FIC 13A, rate indicator controller stream 13A, FIT 13A are maintained, and rate indicator stream 13A is set at the control valve V-13A by the control valve V-13A.

[0431] The purity of the 1-15 by-product is measured in the AIT 13 A, via the (component) analytical indicator transmitter stream 13 A, held at set point via the AIC 13 A, via the (component) analytical indicator controller stream 13 A.

[0432] For the solvent recycle stream 13B, the FIC 13B, rate indicator controller stream 13B, control FIT 13B, rate indicator stream 13B flows through control valve V- 13B at a set point.

[0433] AIT 13B, the component indicator transmitter stream 13B, analyzes and is held at a set point by AIC 13B, the component analyzer indicator controller stream 13B.

[0434] Refrigerant stream 13 D is condenser X-13 C, holds FIC 13 D, rate indicator controller stream 13 D, FIT 13 D, and rate indicator stream 13 D is at set point, by control valve V-13 D.

[0435] 13 H for distillation reflux, FIC 13 H, rate indicator controller stream 13 H, FIT 13 H, rate indicator stream 13 H, at the set point, by control valve V-13 H.

[0436] The bottoms product is passed through the distillation column stream 13 L, the FIC stream 13 L, the rate indicator controller stream 13 L, the FIT stream 13 L, and the rate indicator stream 13 L, which passes through the control valve V-13 L at the set point.

[0437] For 15 A flowing into the storage tank, FIC 15 A, the rate indicator controller stream 15 A holds FIT 15 A, and the rate indicator stream 15 A flows through control valve V- 15 A at the set point.

[0438] And for outflow from the tank, 15B, FIC 15B, rate indicator controller 15B holds FIT 15B, and the rate indicator stream 15B passes through control valve V- 15B at the set point.

[0439] LIT 16, level indicator controller for coolant tank D-16, is maintained at the set point through LIC 16, level indicator for coolant tank D-16.

[0440] For cooling air supply 16 B, FIT 16 B, rate indicator stream 16 B, held at set point passes through FIC 16 B, rate indicator controller flow is 16 B via control valve V-16 B.

[0441] The coolant material flow 16 C is maintained at the set point by the FIT 16 C, the rate indicator flow 16 C, and the FIC 16 C flows through the rate indicator controller 16 C via the control valve.

[0442] In addition to the above, there is also a simple 48-2 feedforward control, 48-2 feedforward can also be used in 48-1 series mode, to select other controllers to control downstream.

[0443] LIT 03A, level direction indicator transmitter 1-2 normal reactor CR-03 A also affects SIC 03 A (agitation) speed meter controller 1-2 normal reactor CR-03 A.

[0444] The IIT 04, the (electrical) current indicator controller 35-1 for the electrochemical reactor ER-04, is the setpoint for the reaction progress of the ER-04 and is therefore used to control most of the components related to the ER-04. The IIT 04 provides the setpoint for the (electrical) current indicator inverter 35-1 for the electrochemical reactor ER-04. The EIC 04 also controls the SIC 04, the (electrode) speed indicator controller 35-1 for the electrochemical reactor ER-04, the ZIP 04 (blade) position indicator controller 35-1 for the electrochemical reactor ER-04, and the ZIC 04 (cutting edge) and ZIP 04 (blade) position indicator controller 35-1 for the electrochemical reactor ER-04.

[0445] IIC 04, (electrical) current indicator controller 35-1 also controls the electrochemical reactor ER-04, FIC 03 B, flow meter controller flows downstream.

[0446] The point is set to SIC 05 A, the (agitation) speedometer controller cleaner WP-05 A also depends on LIT 05 A, the level direction indicator converter cleaner WP-05 A.

[0447] FIC 06A, Rate Indicator Controller Stream 6 A, Control FIC 06 B, Rate Indicator Controller Stream 6 B.

[0448] TIC 07, thermometer controller dryer DP-07, inlet flow rate controlled by FIC 06 A, rate indicator controller stream 6 A.

[0449] FIC 07C, flow meter controller flow 7 C, controlled by TIC 07, thermometer controller dryer DP-07, FIC 07 B, and rate indicator controller flow 7 B.

[0450] SIC 08, (operation) speed indicator controller molding machine MP-08 also controls SIC 09, (operation) speed indicator controller polymer packaging machine unit PP-09 is further downstream.

[0451] FIC 11A, flow meter controller stream 11 A, FIC 13 B, rate indicator controller stream 13 B.

[0452] LIT 11, level direction indicator converter solvent extractor XB-11, also sends a signal to SIC 11, speed indicator controller solvent extractor XB-11.

[0453] AIT 11A, (component) analytical indicator controller stream 11 A, sends a signal to AIC 13 A, (component) analytical indicator controller stream 13 A.

[0454] TIT 13C, thermometer transmitter flow is 13 C, measures the inlet temperature at the condenser and FIT 13 C, rate indicator stream 13 C measures the rate, doubles and sends a signal to FIC 13 D, rate indicator controller stream 13 D.

[0455] FIT 16A, rate indicator stream 16 A, sends a signal to FIC 16 B, rate indicator controller flow 16 B.

[0456] LIC 16, level indicator controller for coolant tank D-16, FIC 16 C, rate indicator controller flow 16 C.

[0457] TIT 16A, thermometer transmitter 16 A, held at set point is TIC 16 A, thermometer controller flow 16 A, double blower B-16 B and FIC 16 B, through rate indicator controller flow 16 B.

[0458] 48-3 Feedback Feedback control (48-3) is used when reliability is required, such as when parameter response is slow and the interference is complex. For electrochemical processes (7-5), feedback control (48-3) is used because process parameters depend on more complex phenomena and are difficult to control through feedforward control (48-2). Deviations affect productivity and quality. Figure 53 shows an example of feedback control (48-3). AIC 05 B receives a signal downstream from AIT 05 B and then sends it to the upstream FIC 05 L for further response. The characteristic of feedback control is that it sends a signal from downstream to the upstream unit for response.

[0459] The 7-5 process, which adjusts between units for the purpose and feeds back to the 48-3 electrochemistry, is primarily used as a 48-1 serial type:

[0460] FIC 00A, flow 0 of the rate indicator controller A is controlled by FIC 02, and flow 2 of the flow meter controller is downstream.

[0461] FIC 00B, flow 0 of the rate indicator controller B is controlled by FIC 02, and flow 2 of the flow meter controller is downstream.

[0462] FIC 01A, rate indicator controller stream 1 A, as a limited quantity reagent, is controlled by FIC 02, and flow meter controller flow 2 is downstream.

[0463] FIC 01B, rate indicator controller stream 1 B is controlled by FIC 02, and flow meter controller flow 2 is downstream.

[0464] Upstream, FIC 02, flow meter controller flow 2 controls FIC 00 A, rate indicator controller flow 0 A, FIC 00B, rate indicator controller flow 0 B, FIC 01A, rate indicator controller stream 1 A, FIC 01B, rate indicator controller stream 1 B and FIC 02 R, rate indicator controller stream 2 R.

[0465] Flow together with FIC 02 flow meter controller. AIC 02 (component) analytical indicator controller flow 2 controls FIC 00 A, rate indicator controller flow 0 A, FIC 00B, rate indicator controller flow 0 B, FIC 01A, rate indicator controller stream 1 A, FIC 01B, rate indicator controller stream 1 B and FIC 02 R, rate indicator controller stream 2 R.

[0466] FIC 02R, Rate Indicator Controller Stream 2 R also controls FIC 11 B, Rate Indicator Controller Stream 11 B.

[0467] The temperature is measured by the TIT 03 A thermometer inverter, and the 1-2 normal reactor CR-03 A maintains the set point. Through the TIC 03 A thermometer controller, the 1-2 normal reactor CR-03 A controls the upstream heater H-02.

[0468] TIC 03A, thermometer controller 1-2Normal reactor CR-03 A also depends on the downstream outlet temperature TIT 03 B, thermometer transmitter flows 3 B.

[0469] PIT 03A, pressure meter inverter 1-2 of normal reactor CR-03 A is maintained at the set point through PIC 03 A, pressure meter controller 1-2 of normal reactor CR-03 A controls the upstream 40-3 pump / compressor Q-02.

[0470] Upstream, the flow meter controller flow 5 A of FIC 05 A controls the dual FIC 05 B, rate indicator controller flow 5 B and FIC 04, rate indicator controller flow 4.

[0471] AIC 05 B (Component) Analytical Indicator Controller Flow 5 B works by controlling the FIC 05 L Rate Indicator Controller Flow 5 L.

[0472] FIC 05L, then the rate indicator controller flow 5 L controls FIC 05 H, and the rate indicator controller flow 5 H.

[0473] FIC 06A, Rate Indicator Controller Stream 6 A is controlled by SIC 07 A, (Conveying) Speed ​​Indicator Controller Stream 7 A.

[0474] Upstream, FIC 06A, rate indicator controller flow 6 A controls FIC 05 A, rate indicator controller flow 5 A.

[0475] Stay level LIT 07, level indicator converter dryer DP-07, also affect SIC 07 A, (conveying) speed meter controller dryer DP-07 is controlled by LIC 07, level indicator controller dryer DP-07.

[0476] The temperature is fixed by TIT 07, thermometer inverter DP-07, set point through TIC 07, thermometer controller dryer DP-07, control heating system to the dryer.

[0477] The TIT 10A, the thermometer transducer absorption unit SB-10A measures the temperature and maintains it at the set point by the TIC 10A, the temperature indicator controller absorption unit SB-10A controls the SIC 10B (conveyor) speed indicator controller to absorb the absorbent regenerator SR-10B.

[0478] FIC 11A, Rate Indicator Controller Stream 11 A depends on FIC 13 A, Rate Indicator Controller Stream 13 A.

[0479] The LIC 11 level indicator controller of the solvent extractor XB-11 works by controlling the FIC 03 B, flow meter controller flow 3 B.

[0480] The temperature is measured by TIT 13, the thermometer transmitter of the distillation column DB-13 is maintained at the set point through TIC 13, the thermometer controller of the distillation column DB-13, and the control reboiler H-13 L.

[0481] Upstream, FIC 13A, the rate indicator controller stream 13 controls FIC 11A, the flow meter controller stream 11A.

[0482] AIC 13 A (component) analytical indicator controller stream 13 A controls the supply of AIC 13 B (component) analytical indicator controller stream 13 B and ZAC 13 position indicator controller upstream from XB-13.

[0483] 48-4 scale 48-4 Proportional control involves monitoring and controlling the ratio of 48-11 multiples of 7-5 process parameters, usually limited to specific stoichiometric ratios at different flow rates. For electrochemical 1-8 polymer production 5-1 electroGreen processes, 48-4 proportional control is primarily used to monitor and control 1-7 electrolyte components.

[0484] Figure 54 shows the flow rate control for the distillation column. FIC 13A, FIC 13B, and AIT 11A send signals to RIY 13A to control FIC 13H based on the flow rate. FIC 13B sends signals to AIC 13B and AIC 13A to control FIC 13L.

[0485] RIY11, Proportional Indicator Relay Electrolyte 1-5 Recovery, is used to monitor and control 1-7 electrolyte components by controlling either 45-1 absorption stream or 44-1 solvent extraction. RIY11 Proportional Indicator Relay Electrolyte 1-5 Recovery is controlled by FIC 03 B flow meter controller flow 3 B, AIC 03 B (component) analyze indicator transmitter stream 3 B, FIC 11 B flow rate indicator controller stream 11 B, AIC 11 B (component) analyze indicator controller stream 11 B, and AIC 13 B (component) analyze indicator controller stream 13 B.

[0486] For the absorption path, the RIY 11 proportional indicator relay has been replaced with a 1-7 electrolyte-controlled SIC 10 B (conveyor) speed indicator controller and absorbent regenerator.For the solvent extraction path, the RIY 11 proportional indicator relay has been replaced with a 1-7 electrolyte-controlled FIC 13 B flowmeter controller.

[0487] In the solvent extraction route, a 48-4 proportional controller is also employed in distillation column DB-13 as RIY 13 A and RIY 13 B to control the dual distillation return stream and distillation bottoms, respectively. FIC 13 A flow rate indicator controller 1-15 controls byproduct stream 13 A, which controls the RIY 13 A scale indicator relay distillation return stream and the RIY 13 B scale indicator relay distillation bottoms.

[0488] For distillation reflux, the RIY 13 A proportional indicator relay distillation reflow is controlled by the solvent stream 13 B of the rate indicator controller of FIC 13 B. The AIT 11 A (component) analytical indicator transmitter extract stream 11 A also signals the RIY 13 A scale indicator relay distillation echo. The RIY 13 A scale indicator relays the distillation reflow and controls the reflow of the FIC 13 H flow indicator controller 13 H.

[0489] For the RIY 13 B scale indicator relay distillation bottoms, the FIC 13 L flowmeter controller controls bottoms stream 13 L. The AIC 13 A (component) analytical indicator controllers 1-15 byproduct stream 13 A also control the RIY 13 B scale indicator relay distillation bottoms.

[0490] 48-5 minutes distance The 48-5 shunt control is used to determine the different responses required when a controller is employed to control two final control elements, such as two 40-6 valves, as shown in Figure 56. In some embodiments, the 48-5 shunt control is visible for 7-7 control levels, temperature, and 1-12 pressure. In some embodiments, the 48-5 distance control includes a dead zone near the set point, i.e., a range that prevents the controller from responding when the deviation from the set point is below a certain limit, as shown in Figure 56.

[0491] Figure 55 is a diagram outlining the 48-5 distance control. LIC 05 B sends a signal to either FIC 05 L or FIC 05 H, which are in different ranges at T-05 B depending on the liquid accumulation level. If the level is in the higher range (range B), FIC 05 L (control B) is controlled to drain the liquid. If the level is in the lower range (range A), FIC 05 H control (control A) is controlled to add some liquid from the 40-5 facility to T-05 B.

[0492] For electrochemical production, the 5-1 ElerGreen process uses 1-8 polymers, 48-5 shunt controls are used for tank level control and storage, including the M-02 mixing tank and the T-15 storage tank, the T-05 detergent tank B, and the 40-5 facility, as well as the XB-11 solvent extractor and the D-12 solvent tank.

[0493] The tank level was measured by the LIT 02 level indicator conveyor on the mixing tank M-02 and adjusted by the LIC 02 level indicator controller on the mixing tank M-02. The LIC 02 level indicator controller on the mixing tank M-02 sequentially controlled, through -485 minutes course, the dual FIC 15 A, rate indicator controller stream 15 A and FIC 15 B, rate indicator controller flow 15 B.

[0494] The tank level is measured in the detergent tank T-05 B by the LIT 05 B level indicator and controlled in the detergent tank T-05 B by the LIT 05 B level indicator controller, which also works to control the FIC 05 H, rate indicator controller Flow 5 H and FIC 05 L, rate indicator controller Flow 5 L.

[0495] The LIC 11 level indicator controller also works with the solvent extractor XB-11. The 48-5 shunt is a dual FIC 12 A flowmeter controller for flow 12 A and FIC 12 B, and a rate indicator controller for stream 12 B.

[0496] 48-6 override selection 48-6 override selective control is generally used to balance 48-13 flexibility and safety in process systems during periods of high fluctuation in the 7-5 process, and 7-7 secondary control is occasionally required. This is usually, but not exclusively, for the safety purposes of the 7-5 process, such as maintaining 1-12 pressure, tank level, and temperature.

[0497] Figure 57 shows the 48-6 override selection control. During normal operation, when LIT 13 is at an acceptable level, FIC 13 B is taken over to control FIC 11 A. When LIT 13 exceeds the threshold, LIC 13 is controlled by FIC 11 A instead of FIC 13 B.

[0498] In an electrochemical 1-8 polymer production 7-5 process, the 48-6 override selective control is used to maintain the tank level due to the complex upstream and downstream settings, making distance control difficult. When the tank level is within the operating range, the 40-6 valve is controlled by the flow controller. However, when the tank level is below the threshold, the 7-7 control is controlled by the level, not the 40-6 valve.

[0499] For 1-2 normal reactor CR-03 A, if the tank level is in the desired range, it sets a point on SIC 07 A as a reference and remotely controls the flow meter controller flow 2 on FIC 02. If the tank level is outside the expected range, LIC 03 A level indicator controller 1-2 normal reactor CR-03 A controls the rate indicator controller flow 2 on FIC 02.

[0500] For 35-1 electrochemical reactor ER-04, if the tank level is within the desired range, set point to SIC 07 A, coupled with IIC 04 (electrical) current indicator controller, 35-1 electrochemical reactor ER-04 controls FIC 02, flow meter controller Flow 2 is upstream. If the tank level is outside the expected range, LIC 04, level indicator controller 35-1 electrochemical reactor ER-04 controls FIC 02, rate indicator controller Flow 2.

[0501] For distillation column DB-13, if the tank level is within the desired range, FIC 11A, rate indicator controller stream 11 A is controlled to FIC 13A, rate indicator controller stream 13A and FIC 13B, rate indicator controller stream 13B. If the tank level is not within range, LIC 13 level indicator controller distillation column DB-13 controls FIC 11A's flow meter controller stream 11A.

[0502] 48-7 Indicators / Alarms Based on first principles, Process 7-7 control is based on the idea that if a 7-5 process parameter changes every time a disturbance occurs, this change cannot be eliminated, and only be transferred through Process 7-7 control. For the 5-1 ElerGreen process of interest, the Process 7-7 control strategy is intended to transfer all disturbances to the chemistry. The 7-5 process, for example, is designed to reduce the productivity of polymers. Some "48-14 disturbance reservoir variables" have a large tolerance for disturbances, such as the level of the material tank.

[0503] Figure 58 shows the 48-7 indicator / alarm control method. This is the simplest variation, LI 00 A, used to measure and report tank level. There are two limits. In the first limit, it only shows the level value and reminds the operator to manually manage inventory. In the second limit, a stronger alarm sounds and the process can be turned off for safety reasons.

[0504] The 48-7 indicator / alarm is used as a "48-14 stabilization reservoir," for example, because the storage tank level is designed with a large tolerance and long time span. For example, a sudden temperature fluctuation can cause a 1-2 conventional reactor or a 35-1 electrochemical reactor to reach productivity within minutes. However, by cooling the 7-7 control system, such a fluctuation can be transferred to the coolant flow of the 40-5 facility, resulting in an increase in the facility's bill, which is relatively unimportant.

[0505] Storage tanks are typically sized to be large enough for the 1-6 reactants to operate for more than a day. Consequently, Process 7-7 control trials refer to these as "48-14 stem storage tanks." In many cases, the process of Jammer 7-5 eventually shifts to a faster rate of consumption within the tank, which offers several advantages. Longer response times available More tolerable results 7-5 Process Safety

[0506] Other "48-14 Stem Cells" are not adjusted, but are at a stationary level that is only monitored by the operator. WI 09, weight indicator is on polymer packaging machine PP-09. ·LI 00A, level indicator auxiliary solvent tank D-00 A LI 00 B, the level indicator is located in the additive tank D-00 B. ·LI 01 A, level indicator is supply tank A T-01 A. LI 01 B, level indicator is supply tank B T-01 B. The LI 12 level indicator is located in solvent reservoir D-12. The LI 14 level indicator is located on the by-product tank TB-14. LI 15, Level Indicator Tank T-15

[0507] Operation 7-8 process The 7-8 flow is subdivided as shown in Figure 59, which includes 59-1 stack, 59-2 department, 34-3 modification, 59-3 maintenance, and finally 34-4 scrap management.

[0508] 59-1 stack In industrial practice, 35-1 electrochemical reactors are stacked in matrices or arrays to minimize space requirements. Because 9-20 vessels are rectangular in the horizontal plane, 59-1 stacks are highly efficient as arrays and are very efficient in their use of space.

[0509] Figure 60 shows a highly effective method for placing electrodes. First, the electrodes can be arranged in an alternating or grouped arrangement. While grouped arrangements are easier to fabricate, the alternating arrangement is more efficient and energy-efficient. The distance between the 3-2 anode and the 3-3 cathode is lower, so less energy is dissipated in the resistor. To achieve this configuration, a rigid 60-3 insulator can be used as a bracket to secure the double 3-2 anode and 3-3 cathode together on the same stent, eliminating the need for short circuits. This strategy is used with the 9-3 rotating disk electrode and the 9-4 spiral / screw electrode.

[0510] In some embodiments, the electrochemical reactors 35-1 are stacked in a 2x1 matrix, as shown in Figure 61. This means that the electrochemical reactors 35-1 are represented as a pair, with one side 61-4 being the stack side. The third side 61-3 provides a maintenance side 61-1 for personnel to maintain the equipment. The second side 61-2 provides a transparent surface for the 9-20 vessel, allowing personnel to view the 9-20 vessel.

[0511] In some embodiments, the electrochemical reactors 35-1 are stacked in a 2x2 matrix with two sides, as shown in Figure 62. Stack-side 61-4 is a common configuration; this is a trade-off between compactness and usability, so at least two sides are provided, with a maintenance-side 61-1 and a maintenance-side 61-3, to arrange for debugging and maintenance of the electrochemical reactors 35-1.

[0512] In some embodiments, the electrochemical reactors 35-1 are stacked in a 2xn matrix, as shown in Figure 63, with three stacked sides 61-4. Except for the end, the electrochemical reactors 35-1 have two maintenance sides 61-3, which provide only one maintenance side 61-3. However, this one maintenance side 61-3 is usually sufficient to maintain the electrochemical reactor 35-1, especially for removing the stays 9-13.

[0513] Figure 64 shows the actual implementation of a 2xn matrix array, consisting of 35-1 electrochemical reactors and 9-2 belt electrode variants. To save cost and space, the 9-9 solid transport unit can be combined, and the components such as 9-20 vessels, 9-13 stays, and 9-17 gas removal units can be modularized for easy placement and maintenance.

[0514] In some embodiments, stacking the electrochemical reactors 59-1 facing outward as shown in Figure 65 reduces maintenance issues 59-3 but is not compact and space-efficient.

[0515] In some embodiments, the electrochemical reactors are stacked in an nxn matrix, as shown in Figure 66. This maximizes compactness at the expense of accessibility. In some situations, this may be acceptable, especially in larger factories where the system is installed on columns suspended from the ceiling, preventing direct access to the equipment. 66-1 is located on the surrounding unit.

[0516] 59-2 Department Due to the modular nature and assembly design, there is a convenient way to arrange the 35-1 electrochemical reactor, 59-2 deployment is shown in Figure 67.

[0517] As shown in Figure 67, the first step is to place the reactor vessels (67-1), of which vessels (9-20) are placed in their designated locations and the pipeline (7-6) is connected to the outlet tank. When there are multiple electrochemical reactors (35-1), they are stacked in the required order (59-1).

[0518] The second step is to place the electrode holder 67-2, of which the electrode 9-13 support bracket is then placed in the tank. Note that the electrode 9-13 bracket must be in the top position when placing the electrode 59-2 in place to prevent it from hitting the tank.

[0519] The third step is to adjust the electrode position (67-3). The movable 9-14 bracket (9-13) can be adjusted by manually pushing it into the tank, for example, using the 23-4 housing and the 23-3 wheel. If the position is fixed, the electrode is then dropped into the tank using the dome to position it vertically in the appropriate direction, allowing the electrode to be submerged in the electrolyte (1-7). The 9-15 bracket incorporates a deformable bracket, eliminating the need for a double clamp to adjust the electrode position (67-2 and 67-3).

[0520] The fourth step is to install 67-4 solid transport channels, of which 9-12 channels will connect the 7-6 pipelines that supply the scrubber to the 35-1 electrochemical reactor, which will then be installed.

[0521] The final step is to install the 67-5 gas removal unit, of which the 9-17 gas removal unit is installed if suitable for electrochemical polymerization reactions. First, the 9-17 gas removal belt 24-2 cap is placed on the electrode, and its position, along with the 24-3 cover and 24-4 weight, is then adjusted and combined. The 7-6 gas pipeline is then connected to the 24-1 ventilation port, and the 9-17 gas is removed to the upper ventilation cabinet, usually through the 7-6 end hanging from the ceiling.

[0522] 7-6 The pipeline is connected to other operational units.

[0523] 34-3 Kaizo 34-3 Kaizo Standard 1-8 Polymer 7-5 Process is the following general-purpose 7-8 process.

[0524] The 35-1 electrochemical reactor, ER-04, is first installed in parallel with 1-2 conventional reactors, CR-03A, and then arranged according to the 59-2 configuration, including C-04, V-04, Stream 4, ventilation cabinet unit, and 7-6 pipeline. If a 59-1 stack is required, the 35-1 electrochemical reactors are stacked in an array.

[0525] The Regular 1-8 Polymer 7-5 process is temporarily closed. The fluid in the 7-5 process is then emptied and the following sections are disconnected: Valve V-02 and 1-2 normal reactor CR-03 A Filter CF-03 B and pump P-03 B Filter CF-03 B and washer WP-05 A

[0526] For the above sections, each switching valve has been installed and the following connections have been completed. S-03 A to 35-1 electrochemical reactor ER-04 liquid inlet S-03 B to C-04 are the liquid outlets of 35-1 electrochemical reactor ER-04 Cleaning outlet of ER-04 electrochemical reactor from S-04 to 35-1

[0527] For the regular 7-5 process, the 1-5 recovery is the same (double before the 45-1 absorption stream and 34-3 modified, or double before the 44-1 solvent extraction and after the 34-3 modified), and the debug is installed immediately. For the regular 7-5 process, the related 1-5 recovery method is different, and a 34-3 modified 1-5 recovery unit is required. For the 34-3 modified 1-5 recovery unit, the fluid will be discharged to the following section, which will be disconnected. V-03 B and SB-10 A / XB-11 P-11 B and SB-10 A / XB-11

[0528] For the above sections, each switching valve was installed between them and the following connections were completed. S-10 A-SB-10 A / XB-11 S-10 B-SB-10 A / XB-11

[0529] If so, the 7-5 step is related to the DB-13 distillation column and involves a key change. The 34-3 distillation column also needs to be remodeled. The fluid will be diverted to the following section, which will be disconnected. The distillation column reflux is up to V-13 A. From the bottom of the distillation column to P-13 B

[0530] For the above sections, each switching valve has been installed and the following connections have been completed. S-13 H and S-13 A to V-13 A S-13 L and S-13 B to P-13 B

[0531] The additional connection is complete. S-13 H to C-13 B to S-13 B S-13 L to C-13 A to S-13 A

[0532] If not, you need 21-2 laundry liquid, which can replace T-05B, WP-05A, SP-06, DP-07, and other detergents.

[0533] The electrochemical 37-1 bypass was operated and tested, and compared with the 1-2 conventional reactor.

[0534] The remaining 7-5 process is adjusted to accommodate the 35-1 electrochemical reactor. Debugging can involve minor changes to the 7-5 process parameters, or more major changes such as changing the mixture composition, or even replacing equipment parts.

[0535] 59-3 Maintenance According to the 7-1 equipment design, the selection of 59-3 maintenance ratio 1-2 compared with the conventional reactor and conventional electrolyzer is more convenient.

[0536] Compared to conventional reactors, the electrochemical reactor features the ability to remove electrodes from the top for new ones, which offers particular advantages for maintenance. This feature avoids the time and complexity involved in draining and refilling the solution tank, resulting in lower downtime and lower costs for maintenance.

[0537] To perform maintenance on 59-3, the flow in 59-2 is operated in contrast to that in Figure 67. First, the electrochemical reaction and 4-1 moving electrodes are turned off, and all double reactions and mechanical movements are stopped. Fluid inflow and outflow are also recommended, but operation can be maintained if the flow is not disturbed, especially considering process safety. The ventilation cabinet is then closed, and 9-17 gas removal is lifted from the electrode and placed elsewhere. 67-5 gas removal is installed in reverse. One small difference from 59-2 is that the solid transport system in 9-9 can be held in place instead of removed, and the electrode can be pushed up at the same time. After adjusting the electrode position and removing it from the tank, reverse operation 67-3, solid transport in the reverse operation 67-4, can be omitted. 9-13 The electrode with the top of the stay is pushed aside as a reverse step. 67-2 The electrode holder is placed back into the tank. 59-3 Maintenance includes cleaning and replacing parts used on the electrode surface, including, but not limited to, blunt blades. Vessel 9-20 is usually stationary and can be omitted except for reactor vessel 67-1, which operates in the reverse direction. For operator convenience, vessel 9-20 is reached. For maintenance, electrodes are released downwards as needed.

[0538] After maintenance, the electrode is pressed against the vessel 9-20 and set in the top position as shown in Figure 59-3. The electrode holder is then placed in position 67-2. The subsequent process for preparing the electrochemical reactor 35-1 is similar to that of Figure 59-2.

[0539] 34-4 Scrap Management For 34-4 scrap management, the extractor needs to be installed before the feed tank. In some embodiments, it is completed for attachment to the upstream electrochemical equipment in the 1-8 polymer 7-5 process to extract the active ingredient. In other embodiments, it is completed in a separate 34-4 waste management plant, which may be owned by ElerGreen, or it may be separated and sent to another plant for easy transport to the electrochemical 1-8 polymer production plant.

[0540] In many cases, purification facilities must separate the active ingredients upstream of 5-2 chemical waste. For example, paint sludge 5-2 chemical waste must be separated from ethylene glycol.

[0541] Examples and Experiments

[0542] General Experiment This scheme includes three main parts: 1-1 preparation, 35-1 electrochemical reactor operation, and sampling.

[0543] 1-1 preparation. 1-1 Preparation of 1-7 Electrolytes involves mixing materials, i.e., liquid 1-6 reactants and solid solutes, to produce 1-7 electrolytes with the desired composition. If 68-2 B is mixed with 68-2 B in a beaker (as in a serving vessel) in 69-1, mixing is the first step in 1-1 Preparation. In particular, if 68-2 B is mixed first, the stoichiometry between 68-1 A and 68-2 B is very easy to control. Liquid mixtures (68-1 Materials A and B) or liquid 68-1 A (if 68-2 B is not involved) are then mixed (depending on the calculated composition) with 31-1 co-solvents, such as water, especially if thinners are used as co-solvents for solid solutes. Mechanical agitation is used each time to ensure uniform mixing throughout the liquid phase.

[0544] The liquid, including 68-1 Material A, 68-2 Material B (if applicable), and 31-1 Cosolvent (if applicable), is mixed with a quantitative solute, often an ionic salt compound. Often, the solute is in solid form, such as a powder or granule, making uniform solid distribution difficult. In this situation, achieving uniform mixing takes a long time due to the slower dissolution process. The mixture can be moderately heated to accelerate the dissolution of the solid, and then the mixture is cooled to room temperature.

[0545] In some cases, the solute exhibits a liquid state, e.g., ionic liquids do not participate in dissolution, and the solute is then mixed and stirred by simple mechanical means, similar to the method 68-1 of materials A and B, or a mixture with a thinner.

[0546] Ingredients are quantified through volume, weight or parts by weight. For quantification, liquids are measured by weight (using a balance) or volume (using measuring cylinders or volumetric bottles, or a combination thereof), and solids are weighed.

[0547] 35-1 Operation of electrochemical reactors. For ease of measurement, the reaction setup is a batch reaction setup for batch operation. This experiment consists of a simple batch electrolysis device. The experimental setup consists of a 9-20 reactor container (typically a 68-6 conical bottle as shown in Figure 68 or a 69-1 beaker as shown in Figure 69) containing conductive materials (3-3 cathode and 3-2 anode) such as a 70-1 working electrode and a 10-1 pair of electrodes, a 3-1 power supply connected to a direct current, and a liquid immersion mixture (1-7 electrolyte), which is continuously stirred and heated when applied. The 9-20 reactor also has a 68-9 pipe connected to a 68-7 bubble flow meter to measure the flow rate of any gas escape from the electrochemical reaction. The 9-20 reactor and 68-7 bubble flow meter are fixed in position and clamped onto a support.

[0548] The electrodes consist of two conductive plates, often made of copper, nickel, zinc, or stainless steel, immersed in a 1-7 electrolyte at one end and connected to a 3-1 DC power supply at the other end. The positive (+) terminal of the 3-1 DC power supply is called the 3-2 anode, and the negative (-) terminal of the 3-1 DC power supply is called the 3-3 cathode. The 1-7 electrolyte is stirred and heated, typically using a 68-5 magnetic mixer or a 68-4 heating plate mixer, respectively.

[0549] When an electrochemical reaction occurs, current passes through the 1-7 electrolyte. The 1-8 polymer product P is solid, and deposits on the electrode surface as a 3-5 solid deposit. The 1-15 by-product H becomes liquid and diffuses into the 1-7 electrolyte. Depending on the 1-7 electrolyte used, the 1-15 by-product H can be electrochemically decomposed into gases and escape from the electrode. For example, water decomposes into hydrogen and oxygen. These gases are too small to be flammable and non-toxic, but the device is typically installed and operated in a ventilated cabinet.

[0550] The 1-7 electrolyte consists of at least 68-1 Material A, 1-6 Reactant, and 68-3 Salt, which dissolve and provide conductivity to facilitate the electrochemical reaction. Depending on the specific situation, 68-2 Material B may be required as a separate component of the 1-6 Reactant, or 32-1 Additives, such as 31-1 Cosolvents, may be used. The specific 1-6 Reactants are detailed in Table 24 below.

[0551] [Table 24]

[0552] a.Start: To start the 35-1 electrochemical reactor, inject the prepared 1-7 electrolyte into the 9-20 reaction vessel and slowly filter it. The electrode belt 68-8 is then attached to the 9-20 reaction vessel, and the other end of the electrode is connected to the DC 3-1 power supply. The DC 3-1 power supply plug is then opened, and the fixed-point current (constant current operation) and / or 6-5 applied voltage (constant 6-5 applied voltage operation) are adjusted to the desired values. Another "on" button (usually present for timing accuracy and process safety) is then pressed to turn on the DC 3-1 power supply and start a timer (a stopwatch or handheld timer can also be used) to record the time.

[0553] b. Close To close the reactor after the experiment, the DC3-1 power supply was first turned off and the timer was stopped; this order is not dependent on a specific sequence. The 68-4 heated plate agitator was then closed. The 68-4 heated plate agitator was then shut down. The DC3-1 power outlet was then turned off, and the reactor was allowed to gradually cool to room temperature. Once the reactor had cooled to a safe temperature, the 68-8 stoppered electrode was removed from the reactor. The 1-14 waste electrolyte was then poured into a labeled container and stored. Finally, the 68-8 stoppered electrode and the 9-20 reactor were both washed, dried, and stored.

[0554] iii) Sampling and Measurement: Sampling For the sample, first turn off the DC power supply 3-1 and stop the timer. The exact reaction time is recorded when the timer stops. Lift and open the stopper 68-8 and place the sample in the container 9-20 on a clean surface for a while.

[0555] For liquid sampling, a small amount of 1-14 waste electrolyte is extracted from the 9-20 container using a drip tube, which is then used to drain the sampled 1-14 waste electrolyte into a sample bottle, which is carefully sealed and marked accordingly. If necessary, the vial is carefully sealed and marked accordingly.

[0556] For samples containing 3-5 solid deposits, especially 1-8 polymers, the 3-5 solid deposits were removed from the electrode using a tool knife. The 3-5 solid deposits were collected on a filter with a bottom container (for collecting the filter) and carefully washed with distilled / deionized water. The 3-5 solid deposits were then left to dry and collected in a sample bottle.

[0557] After sampling, the 68-8 stopper is re-tightened and the reaction vessel 9-20 is opened. The DC 3-1 power button is restarted and the timer is restored to the same time.

[0558] b.Measurement 68-7 Bubble Flow Meter Settings Before gas flow can be measured, the 68-7 Bubble Flow Meter must be set up for readiness. First, a bubble fluid (such as soap or detergent diluted with water) is added to the 68-7 Bubble Flow Meter until enough fluid is added to the bubble to submerge the gas outlet of the reactor. The bubbles are then pushed out, temporarily submerging the reactor's gas outlet and releasing back to the original, unsubmerged level. The bubble layer is then observed to rise to the initial mark (0 ml), a later mark (usually 5 ml), and another later mark (usually 10 ml). When the bubbles first rise to the top and burst, the inner walls of the 68-7 Bubble Flow Meter are wet with the fluid (soapy water) and are ready for gas flow measurement.

[0559] Gas flow measurement: To perform gas flow measurements, the 68-7 bubble flow meter is prepared as described below. A ball bubble temporarily submerges the reactor gas outlet and is then released to its original, unsubmerged position. The bubble layer slowly rises, and when the timer is started, the bubble layer rises to the initial mark (0 ml) 68-10. The timer is stopped, the time is recorded, and when the bubble rises to any second (5 ml) or third (10 ml) mark 68-11 or any subsequent mark. The gas flow rate can then be calculated using the 68-7 bubble flow meter data base equation 35.

[0560]

number

[0561] For this situation V1=5ml and V2=10ml.

[0562] One of the marks, 68-11 and later, works well. As long as this volume is consistent, the last marking, 68-11 and later, usually results in a more accurate measurement with a lower relative uncertainty due to human reaction time errors. Timing and parallax errors are both relatively low when reading the markings.

[0563] Example 1: Ethylene The first example is the 7-3 polymer, the simplest modification being electrochemical polymerization of vinyl to form polyethylene, as shown in Equation 36. In this situation, 68-1 material A is ethylene and 68-2 material B is not required, and 1-8 polymer P is polyethylene, but 1-15 is not a by-product. Note, however, that the 1-15 by-product is not present in the polymerization reaction route, and is not a side effect. The conductive 68-3 soluble salt is lithium chloride (LiCl) due to its solubility in the organic phase. 31-1 cosolvent is acetone, due to its miscibility with ethylene.

[0564]

number

[0565] Example 2, Ethylamine The second example, a more complex modification of 7-3 polymer (see Equation 37), involves electrochemically polymerizing ethylamine with 1-15 as a by-product to form polyethylene. In this case, 68-1 material A is ethylamine and 68-2 material B is not required; 1-8 polymer P is polyethylene, but this time the 1-15 by-product is ammonia (6-9). The conductive soluble salt in 68-3 was chosen as lithium chloride (LiCl) due to its solubility in the organic phase. 31-1 cosolvent was chosen due to its miscibility with acetone and ethylamine.

[0566]

number

[0567] Example 3: Ethanol Acid The third example is the simplest modification of the 7-4 condensation polymer, shown in Equation 38, where ethanolic acid is electrochemically polymerized to form polyethanolic acid using the same monomeric material. In this situation, 68-1, material A is ethanolic acid and 68-2, material B is not required. 1-8 Polymer P is polyethanolic acid, and the by-product formed in 1-15 is water. Sodium chloride was chosen as the conductive soluble salt in 68-3. NaCl has abundant solubility in the polar phase through hydrogen bonding to the -OH groups of ethanolic acid. 31-1, water was chosen as the cosolvent due to its miscibility with ethanolic acid.

[0568]

number

[0569] Example 4, Ethylene glycol and succinic acid A fourth example is a slightly more complex variation of the 7-4 condensation polymer, shown in Equation 39, in which electrochemical polymerization occurs between two different monomeric materials: ethylene glycol and succinic acid to form poly(ethylene glycol succinate). In this situation, in 68-1, material A is acetic acid and in 68-2, material B is succinic acid, while in 1-8, polymer P is poly(ethylene glycol succinate), and the by-product formed in 1-15 is water. In 68-3, sodium chloride was chosen as the soluble salt, as NaCl's solubility in the polar phase is due to the abundant hydrogen bonding of -OH groups present in both ethylene glycol and succinic acid. In 31-1, water was chosen as the cosolvent, due to its miscibility with ethylene glycol and succinic acid.

[0570]

number

[0571] Example 5: Phthaldiamine and phthalic acid A fifth example is a more complex variation of the 7-4 condensation polymer, electrochemically polymerizing benzenediamine and terephthalic acid to form a polyaromatic amide, containing functional groups other than -OH between the two different monomer species, as shown in Equation 40. In this situation, Material A in 68-1 is benzenediamine, Material B in 68-2 is phthalic acid, Polymer P in 1-8 is polyphenylamide, and the by-product formed in 1-15 is water. Sodium chloride was chosen as the dissolving salt in Conductive 68-3, due to its solubility in the polar phase, resulting from abundant hydrogen bonding between the -OH groups of terephthalic acid and the -NH groups of phenyldiamine. Water was chosen as the cosolvent in 31-1 due to its miscibility with benzoic acid and benzoic acid.

[0572]

number

[0573] Example 6, 6-2 Phenol A and 6-1 Urea A sixth example is a more complex modification of the 7-4 condensation polymer, as shown in Equation 41, in which the -OH group between two different monomers is electrochemically polymerized to form the non-aqueous 1-15 byproduct, 6-2 phenol A and 6-1 urea, forming 6-7 polycarbonate. In this case, Material A is 6-2 phenol A and Material B is 6-1 urea, while Polymer P is 6-7 polycarbonate and the 1-15 byproduct formed is 6-9 ammonia. The conductive 68-3 soluble salt was chosen as sodium chloride (NaCl), due to its solubility in the polar phase and its self-rich hydrogen bonding between the -OH group of 6-2 bisphenol A and the -NH group of 6-1 urea. The cosolvent 31-1 was chosen as 6-9 ammonia, due to the miscibility of 6-2 phenol A and 6-1 urea.

[0574]

number

[0575] Example 7, vinyl carbonate The seventh example is a unique example of a 7-4 condensation polymer. A simple modification is shown in Equation 42, but ring-opening involves the same monomeric material, and electrochemical polymerization of vinyl carbonate to form polycarbonate is used. In this case, 68-1 material A is vinyl carbonate and 68-2 material B is not required, and 1-8 polymer P is not polyvinyl carbonate; 1-15 is a by-product. Note, however, that there are no side effects from the polymerization reaction route of 1-15. 68-3: The dissolved salt was chosen to be lithium chloride (LiCl), primarily due to the solubility of vinyl carbonate in the organic phase. 31-1: Acetone was chosen as the cosolvent due to its miscibility with vinyl carbonate:

[0576]

number

[0577] Example 8, Dimethylsilane Glycol An eighth example is a unique but different type of 7-4 condensation polymer. A simple modification is shown in Formula 43, but the adjacent atoms in the main chain of the 7-4 condensation polymer are not carbon atoms. For example, polysilicone, polysulfone, polyphosphinate, polynitrate, and 33-15 polysilicone are not carbon atoms. The electrochemical polymerization of dimethylsilane glycol (DMSG) forms 33-15 polysilicone. In this situation, 68-1 material A is dimethylsilane glycol and 68-2 material B is not required. 1-8 polymer P is 33-15 polysilicone and the resulting 1-15 by-product is water. Sodium chloride was chosen as the conductive salt in 68-3. NaCl's solubility in the polar phase is due to abundant hydrogen bonding to the -OH groups of dimethylsilane glycol. Water was chosen as the cosolvent in 31-1 due to its miscibility with dimethylsilane glycol.

[0578]

number

[0579] Observation Overview Figure 70 summarizes an example of an observed reaction. During the reaction, the 1-8 polymer is attached to the working electrode (70-1), typically with the 3-5 solid deposits, which can be removed as shown on the left. However, if the 1-8 polymer is in a liquid state or can be dissolved in the electrolyte phase (70-2), the 70-2 liquid polymer will diffuse freely into the 1-7 electrolyte. Depending on the type of 1-8 polymer, the adhesion strength to the electrode surface varies. In some cases, the 3-5 solid deposits can be removed with a slight shaking; in others, the solid deposits are so hard that they require tweezers or a knife to remove them.

[0580] Some 70-3 bubbles also form on the surfaces of the 3-2 anode and 3-3 cathode. In most cases, the 3-3 cathode has smaller particles, but the 70-3 bubbles are stronger than the 3-2 plate. This is because the 3-3 cathode releases more moles of gas than the 3-2 anode, resulting in more gas leaking from the reaction, which is a stoichiometric property. For example, water decomposition, as shown in Equation 44, always occurs when water is present in the 1-7 electrolyte, as a by-product H, or as a co-solvent in 1-15.

[0581]

number

[0582] The by-product H, normally a colorless, transparent liquid (visible only to the 1-7 electrolyte due to its different refractive index), diffuses into the 1-7 electrolyte. In this reaction, the 3-3 cathode is the 3-2 plate, causing more gas to escape.

[0583] Results and Analysis Products can be identified by chemical analysis methods such as GC-MS (Gas Chromatography-Mass Spectrometry), FTIR (Fourier Transform Infrared Spectroscopy) and UV-Vis (Ultraviolet-Visible Spectrophotometry).

[0584] As shown in Figure 71, this identification works by comparing the signal parameters to the scanned parameters, between electrolyte 1-7, waste electrolyte 1-14, and known products. Such comparisons, where the signal corresponds to a known substance with a known reaction, can be further quantified as a concentration, and the conversion factor is then calculated using Equation 45.

[0585]

number

[0586] where v is the final volume of 1-7 electrolyte, V0 is the initial volume of 1-7 electrolyte, and C0 is the concentration of material A in 1-7 electrolyte when it was first prepared. In fact, due to the liquid phase properties of the system, the final volume of 1-7 electrolyte did not change significantly from its initial volume.

[0587] The conversion rate, X, can then be compared to the relative accumulated charge as shown in Figure 72. This accumulated charge is the total charge in the 35-1 electrochemical reactor over a short period of time. The experiment assumes constant current operation, and the accumulated charge is simply the current times time, as shown in Equation 46.

[0588]

number

[0589] It is noted that the conversion rate is linear at low stored charges but then tends to plateau at higher stored charges. This is because the conversion rate is also limited by the concentration of the 1-6 reactant in the 9-20 vessel. At low stored charges, the effect of this concentration is not significant, so the curve appears linear. At higher stored charges, significant 1-6 reactant is depleted in the reaction, lowering the concentration sufficiently to reduce the reactivity of the 1-6 reactant.

[0590] The number of moles reacted can be easily calculated using Equation 47

[0591]

number

[0592] The number of electrons is found via the stored charge basis, Equation 48.

[0593]

number

[0594] Of these, F≒96485 C / mol is Faraday's constant, which represents the number of electron charges per mole. The number of electrons in each reaction can be obtained from the slope of Figure 73.

[0595] On the other hand, the curve diagram, Figure 74, shows a nearly linear relationship between applied voltage and current. Below the threshold voltage, there is no reaction; the energy barrier to reaction has not yet been overcome. Above the threshold voltage, the applied voltage follows a linear relationship with current, resulting in the operating range shown in Figure 74. The slope of the diagram represents the resistance of the electrochemical reactor (35-1). The higher the slope, the higher the required current. As the applied voltage increases, the higher the required current becomes, and the more electrical energy dissipates into resistive heating of the electrochemical reactor (35-1, particularly the electrolyte (1-7)). This is where design considerations come in. The design of the electrochemical reactor (35-1) involves reducing the resistance of the electrolyte (1-7), reducing energy dissipation to thermal energy.

[0596] Finally, the gas flow rate is essentially linear with respect to current, as shown in Figure 75. This takes into account the gas emergence rate, which is proportional to the current through the electrodes, based on stoichiometry.

Claims

[Claim 1] 1. A reactor for an electrochemical reaction, the reactor comprising: a container for carrying an electrolyte solution; At least one electrode, at least one counter electrode, the electrode being provided in the container; the first portion of the electrode and the counter electrode are immersed in the electrolyte solution; a second portion of the electrode is not immersed in the electrolyte solution, and the electrode is moved to maintain its position, and the size of the surface area of ​​the first portion immersed in the electrolyte solution and the second portion not immersed in the electrolyte solution is maintained, while a product formed by the electrochemical reaction is deposited on the surface area of ​​the electrode; An electrode; a removal device configured to contact the electrode and remove deposited product from the electrode; a reactor comprising:

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