Whole-plant material coordination control method and system in polyvinyl chloride production process

Abstract

The invention discloses a whole-plant material coordination control method and system in a polyvinyl chloride production process, and belongs to the technical field of automatic control, and the method comprises the following steps: S01, calculating the average flow of consumed vinyl chloride monomers and the average flow of produced polyvinyl chloride of a polymerization production line; s02, calculating the balance value of the flow of polyvinyl chloride entering a stripping tower and the flow of polyvinyl chloride entering a drying bed in the polymerization production line; s03, calculating the balance value of acetylene flow and hydrogen chloride flow entering the converter from the conversion production line; step S04, calculating the flow balance value of hydrogen and chlorine entering a synthetic furnace in a synthetic production line and the flow of saline water required for preparing the hydrogen and the chlorine; and S05, calculating the calcium carbide flow entering the acetylene generator from the acetylene production line, and carrying out balanced distribution on the feeding load of the generator. By coordinating the material balance among the production lines, the coordination control of the materials of the whole plant in the polyvinyl chloride production process is realized, and the stability and safety of the production process are ensured.

Description

Technical Field

[0001] The invention belongs to the technical field of automatic control, and in particular relates to a method and system for coordinated control of materials in the whole plant during a polyvinyl chloride production process. Background Art

[0002] Polyvinyl chloride, PVC for short, is the world's largest-volume general-purpose plastic, widely used in building materials, household appliances, cables, pipes and other fields. The production process of PVC is mainly divided into calcium carbide method and ethylene method. Since my country has relatively abundant coal resources, calcium carbide method is mainly used to produce PVC in China.

[0003] The production process of calcium carbide method mainly includes: calcium carbide reacts with water to generate acetylene in the generator; salt water is electrolyzed in the electrolytic cell to produce hydrogen and chlorine, which react in the synthesis furnace to generate hydrogen chloride (such as "A method for controlling the dynamic balance of chlorine-hydrogen ratio in the process of preparing hydrogen chloride [P] (Chinese patent: CN114185369A)"); acetylene and hydrogen chloride react in the converter to generate vinyl chloride; vinyl chloride generates slurry-like polyvinyl chloride in the polymerization kettle (such as "A control system for the batch production process of polyvinyl chloride [P] (Chinese patent: CN10258 5059A)”), and then through the stripping tower and drying bed to produce powdered polyvinyl chloride (such as “A heat control method for PVC drying device [P] (Chinese patent: CN115157481A)”, “A soft measurement method for PVC moisture content in PVC drying device [P] (Chinese patent: CN115284484A)”, “A PVC drying bed powder conveying device and control method [P] (Chinese patent: CN114229485A)”), and finally transported to packaging to form products.

[0004] Since the PVC production process involves multiple production lines and the materials between the production lines are interrelated, if the material matching is unbalanced, it will cause large fluctuations in process parameters and affect the stability and safety of the production process. In addition, the PVC polymerization process is an intermittent production process, and the intermittent production data needs to be converted into continuous production data. Therefore, it is necessary to design a reasonable PVC production process for coordinated material control of the entire plant to balance the materials between the production lines and ensure the stability and safety of the production process. Summary of the invention

[0005] To solve the above problems, the present invention provides a method and system for coordinated material control in the whole plant of a polyvinyl chloride production process, the purpose of which is to achieve coordinated material control in the whole plant of a polyvinyl chloride production process by coordinating the material balance among the production lines, thereby ensuring the stability and safety of the production process.

[0006] A method for coordinated control of materials in the whole plant during the production process of polyvinyl chloride comprises the following steps:

[0007] Step S01: Calculate the average flow rate of vinyl chloride monomer consumed and the average flow rate of polyvinyl chloride produced by the polymerization production line by converting the intermittent production process into continuous production process data;

[0008] Step S02: Calculate the balance value of the polyvinyl chloride flow rate entering the stripping tower and the polyvinyl chloride flow rate entering the drying bed of the polymerization production line according to the average flow rate of the vinyl chloride monomer calculated in step S01;

[0009] Step S03: Calculate the balance value of acetylene flow and hydrogen chloride flow entering the converter of the conversion production line according to the average flow of vinyl chloride monomer, the liquid level of the vinyl chloride gas tank, and the liquid level of the vinyl chloride monomer spherical tank calculated in step S01;

[0010] Step S04: according to the hydrogen chloride flow rate required for preparing vinyl chloride calculated in step S03, calculate the balance value of the flow rates of hydrogen and chlorine entering the synthesis furnace of the synthesis production line, as well as the brine flow rate required for preparing hydrogen and chlorine, and balance the feed load distribution of the synthesis furnace and the electrolytic cell;

[0011] Step S05: Based on the acetylene flow rate required for preparing vinyl chloride calculated in step S03, the calcium carbide flow rate entering the acetylene generator from the acetylene production line is calculated, and the feed load of the generator is balanced and distributed.

[0012] Furthermore, the step S01 includes the following steps:

[0013] Step S101: Obtain the production grades of the first W polymerization kettles currently being scheduled for production on the polymerization production line, the total amount of vinyl chloride monomer added to each production grade, the time for adding vinyl chloride monomer to each production grade, and the time for discharging polyvinyl chloride produced by each production grade.

[0014] The PVC polymerization process is an intermittent production process, that is, a certain amount of PVC monomer and additives are added to the polymerization kettle, and then the polymerization reaction is carried out in the polymerization kettle. After the reaction is completed, the material is discharged to obtain PVC in a slurry state. Since the PVC polymerization process is an intermittent process, in order to improve production efficiency, the PVC polymerization process is often completed in parallel by multiple polymerization kettles. After one polymerization kettle is fed, another polymerization kettle is fed. Therefore, the whole process can be roughly regarded as a continuous production process composed of multiple intermittent processes.

[0015] General chemical reaction equation for polymerization: nC 2 H 3 Cl→-(CH 2 -CHCl)n-.

[0016] Step S102: Calculate the average flow rate of vinyl chloride monomer into the polymerization kettle according to the following formula:

[0017]

[0018] in, represents the average flow rate of vinyl chloride monomer into the polymerization kettle, W represents the first W polymerization kettles scheduled for production, represents the name of the i-th brand, It indicates the average time of adding vinyl chloride monomer to each production grade. Indicates the discharge time of polyvinyl chloride produced by each production grade, It indicates the duration during which no vinyl chloride monomer is added to any polymerization reactor.

[0019] Step S103: Calculate the average flow rate of polyvinyl chloride out of the polymerization kettle according to the following formula:

[0020]

[0021] in, represents the average flow rate of polyvinyl chloride slurry out of the polymerization kettle, W represents the first W polymerization kettles in production, represents the name of the i-th brand, Indicates the time of adding vinyl chloride monomer to each production grade. It indicates the conversion coefficient of the total amount of PVC produced by each production grade. It indicates the average time of discharging PVC for each production grade. It indicates the duration during which no polymerization reactor discharges polyvinyl chloride.

[0022] Furthermore, the step S02 includes the following steps:

[0023] Step S201: Obtain the set value of the polyvinyl chloride flow rate entering the stripping tower and the set value of the polyvinyl chloride flow rate entering the drying bed of the polymerization production line.

[0024] The main function of PVC stripping is to effectively remove and recover vinyl chloride monomer from PVC slurry, reduce VCM consumption, improve the quality of PVC resin, and reduce the pollution to the environment and harm to the human body during the processing and use of its products. The main function of the PVC drying process is to dry the PVC in slurry state to form PVC in powder state.

[0025] Step S202: Calculate the flow balance value of polyvinyl chloride into the stripping tower according to the following formula:

[0026]

[0027] in, It represents the flow balance value of polyvinyl chloride into the stripping tower. Indicates the current value of the polyvinyl chloride flow rate into the stripping tower. It represents the weighted coefficient of the PVC flow balance control into the stripping tower, It indicates the current value of the average flow rate of polyvinyl chloride in the polymerization kettle. It shows the average flow rate of polyvinyl chloride in the polymerization kettle in the previous cycle.

[0028] Step S203: Calculate the flow balance value of polyvinyl chloride into the drying bed according to the following formula:

[0029]

[0030] in, Indicates the flow balance value of polyvinyl chloride into the drying bed, Indicates the current value of the set value of the polyvinyl chloride flow entering the drying bed. represents the weighting coefficient of the drying balance controller, It indicates the current value of the average flow rate of polyvinyl chloride in the polymerization kettle. It shows the average flow rate of polyvinyl chloride in the polymerization kettle in the previous cycle.

[0031] Furthermore, the step S03 includes the following steps:

[0032] Step S301: Obtain the set values ​​of the acetylene flow rate and hydrogen chloride flow rate entering the converter of the conversion production line, the liquid level of the vinyl chloride gas tank, and the liquid level of the vinyl chloride monomer spherical tank.

[0033] Vinyl chloride is the raw material for producing polyvinyl chloride. It is mainly produced by the reaction of acetylene and hydrogen chloride under catalytic action in a converter, and then through compression, distillation and other processes to produce high-purity vinyl chloride monomer for the production of polyvinyl chloride. The vinyl chloride gas holder is used to buffer the vinyl chloride gas in the process of preparing vinyl chloride, and the vinyl chloride monomer storage tank is used to store high-purity vinyl chloride for the production of polyvinyl chloride.

[0034] Preparation of vinyl chloride reaction equation: C 2 H 2 +HCl→C 2 H 3 Cl.

[0035] Step S302: Calculate the relative remaining amount of the vinyl chloride monomer spherical tank liquid level, which is the sum of the vinyl chloride monomer spherical tank liquid level change rate and the vinyl chloride monomer spherical tank liquid level deviation from the set value.

[0036] Calculate the rate of change of liquid level in the vinyl chloride monomer spherical tank:

[0037]

[0038] Calculate the deviation of the liquid level of the vinyl chloride monomer spherical tank from the set value:

[0039]

[0040] in, Indicates the rate of change of the liquid level in the vinyl chloride monomer spherical tank, Indicates the current value of the liquid level in the vinyl chloride monomer spherical tank. Indicates the last cycle value of the liquid level in the vinyl chloride monomer spherical tank. Indicates the deviation of the liquid level of the vinyl chloride monomer spherical tank from the set value. Indicates the liquid level setting value of the vinyl chloride monomer spherical tank.

[0041] Step S303: Calculate the relative remaining amount of the vinyl chloride gas tank liquid level, which is the sum of the vinyl chloride gas tank liquid level change rate and the vinyl chloride gas tank liquid level deviation from the set value.

[0042] Calculate the rate of change of the liquid level in the vinyl chloride gas tank:

[0043]

[0044] Calculate the deviation of the vinyl chloride gas tank liquid level from the set value:

[0045]

[0046] in, Indicates the rate of change of the liquid level in the vinyl chloride tank. Indicates the current value of the vinyl chloride gas tank liquid level. Indicates the last cycle value of the vinyl chloride gas tank liquid level. Indicates the deviation of the liquid level of the vinyl chloride gas tank from the set value. Indicates the set value of the vinyl chloride gas tank liquid level.

[0047] Step S304: Calculate the flow balance value of acetylene into the converter required for preparing vinyl chloride according to the following formula:

[0048]

[0049] in, Indicates the output of the set value of the acetylene flow rate into the vinyl chloride converter. Indicates the current value of the acetylene flow setting value entering the vinyl chloride converter. The acetylene weighting coefficient of the rate of change of the liquid level in the vinyl chloride monomer spherical tank is expressed as: Indicates the rate of change of the liquid level in the vinyl chloride monomer spherical tank, Indicates the acetylene weighting coefficient of the deviation of the liquid level of the vinyl chloride monomer spherical tank from the set value. Indicates the deviation of the liquid level of the vinyl chloride monomer spherical tank from the set value. Indicates the acetylene weighting coefficient of the rate of change of the vinyl chloride gas tank liquid level, Indicates the rate of change of the liquid level in the vinyl chloride tank. Indicates the acetylene weighting coefficient of the ethylene chloride tank liquid level deviation from the set value. Indicates the deviation of the liquid level of the vinyl chloride gas tank from the set value. represents the weighted coefficient of the average flow rate change of vinyl chloride monomer, Indicates the current value of the average flow rate of vinyl chloride monomer, Indicates the average flow rate of vinyl chloride monomer in the previous cycle.

[0050] Step S305: Calculate the flow balance value of hydrogen chloride entering the converter required for preparing vinyl chloride according to the following formula:

[0051] It can be seen from the reaction equation for preparing vinyl chloride that, ideally, acetylene and hydrogen chloride need to react in a 1:1 ratio. However, in actual production, in order to ensure that the produced vinyl chloride does not contain acetylene, the amount of hydrogen chloride must be greater than the amount of acetylene.

[0052]

[0053] in, Indicates the output of the hydrogen chloride flow rate setting value of the converter. represents the ratio coefficient of hydrogen chloride to acetylene, Indicates the acetylene flow setting value.

[0054] Furthermore, the step S04 includes the following steps:

[0055] Step S401: Obtain the set values ​​of the chlorine flow rate and hydrogen flow rate entering the synthesis furnace of the synthesis production line, and the set value of the brine flow rate entering the electrolytic cell.

[0056] Hydrogen chloride is the raw material for the production of vinyl chloride. It is mainly produced by the reaction of chlorine and hydrogen in a synthesis furnace, where chlorine and hydrogen are produced by electrolyzing brine in an electrolytic cell.

[0057] The reaction equation for electrolysis of salt water is: 2NaCl+2H 2 O→NaOH+Cl 2 +H 2

[0058] Hydrogen chloride synthesis reaction equation: Cl 2 +H 2 →2HCl.

[0059] Step S402: Calculate the flow balance value of chlorine gas entering the synthesis furnace required for preparing hydrogen chloride according to the following formula:

[0060]

[0061] in, Indicates the balance value of chlorine flow required to enter the synthesis furnace, Indicates the current value of the total set value of the chlorine gas flow required to enter the synthesis furnace. It represents the conversion coefficient of hydrogen chloride flow into chlorine flow, Indicates the set value of hydrogen chloride flow into the vinyl chloride converter. Represents the loss bias caused by pipeline resistance.

[0062] Step S403: Based on the flow balance value of chlorine gas into the synthesis furnace required for preparing hydrogen chloride calculated in step S402, according to the adjustable load margin of each synthesis furnace, 2 Balance the feed load distribution of each synthesis furnace.

[0063] (1) When hour

[0064] Calculate M 2 Each synthesis furnace can adjust the chlorine gas flow load upper margin:

[0065]

[0066] Calculate M 2 The chlorine gas flow load is allocated to each synthesis furnace:

[0067]

[0068] in, Indicates the upper margin of chlorine flow rate of each synthesis furnace, Indicates the upper limit of chlorine flow rate for each synthesis furnace. Indicates the current value of the chlorine flow setting value of each synthesis furnace. Indicates the output value of the chlorine flow setting value of each synthesis furnace, Indicates M 2 Total set value of chlorine gas flow rate for each synthesis furnace.

[0069] (2) When hour

[0070] Calculate M 2 Adjustable chlorine flow rate under load margin of each synthesis furnace:

[0071]

[0072] Calculate M 2 Each synthesis furnace is assigned chlorine gas flow load:

[0073]

[0074] in, Indicates the margin of chlorine flow rate of each synthesis furnace, Indicates the lower limit of chlorine flow rate for each synthesis furnace, Indicates the current value of the chlorine flow setting value of each synthesis furnace. Indicates the output value of the chlorine flow setting value of each synthesis furnace, Indicates M 2 Total set value of chlorine gas flow rate for each synthesis furnace.

[0075] Step S404: Calculate the flow balance value of hydrogen entering the synthesis furnace required for preparing hydrogen chloride according to the following formula:

[0076] From the hydrogen chloride synthesis reaction equation, we can know that under ideal conditions, chlorine and hydrogen react in a 1:1 ratio to produce hydrogen chloride. However, in the actual production process, the produced hydrogen chloride cannot contain chlorine, so the amount of hydrogen must be greater than the amount of chlorine.

[0077]

[0078] in, Indicates entry 2 The output value of the hydrogen flow setting value required by the synthesis furnace, It represents the ratio coefficient of chlorine flow rate to hydrogen flow rate, Indicates the current value of the chlorine gas flow setpoint for each synthesis furnace.

[0079] Step S405: Calculate the brine flow rate required to prepare the chlorine flow rate according to the following formula:

[0080]

[0081] in, It indicates the incremental output value of the total set value of the brine flow required to prepare the hydrogen flow. Indicates the current value of the total set value of the brine flow required to prepare the hydrogen flow. Indicates the conversion coefficient of hydrogen flow into brine flow, Indicates the chlorine gas flow setting value, Represents the loss coefficient caused by pipeline resistance.

[0082] Step S406: Based on the total set value increment output value of the brine flow calculated in step S405, according to the adjustable load margin of each electrolyzer, 3 Feed load balancing is performed on each electrolytic cell.

[0083] (1) When hour

[0084] Calculate M 3 Each electrolyzer can adjust the upper margin of brine load:

[0085]

[0086] Calculate M 3 Each electrolyzer is assigned brine load:

[0087]

[0088] in, Indicates the upper margin of brine flow rate for each electrolytic cell, Indicates the upper limit of brine flow rate for each electrolyzer, Indicates the current value of the brine flow setting value of each electrolytic cell, Indicates the output value of the brine flow setting value of each electrolytic cell, Indicates M 3 The total set value of brine flow rate for each electrolyzer.

[0089] (2) When hour

[0090] Calculate M 3 Each electrolyzer has adjustable brine load margin:

[0091]

[0092] Calculate M 3 Each electrolyzer is assigned brine load:

[0093]

[0094] in, Indicates the lower margin of brine flow rate for each electrolyzer, Indicates the lower limit of brine flow rate for each electrolyzer, Indicates the current value of the brine flow setting value of each electrolytic cell, Indicates the output value of the brine flow setting value of each electrolytic cell, Indicates M 3 The total set value of brine flow rate for each electrolyzer.

[0095] Furthermore, the step S05 includes the following steps:

[0096] Step S501: Obtain the carbide flow setting value of the acetylene production line and the liquid level of the acetylene gas tank.

[0097] Calcium carbide is the raw material for producing acetylene. Calcium carbide reacts with water in the generator to produce acetylene gas.

[0098] The reaction equation for preparing acetylene from calcium carbide: CaC 2 +2H 2 O→C 2 H 2 +Ca(OH) 2 .

[0099] Step S502: Calculate the rate of change of the acetylene gas tank liquid level according to the following formula:

[0100]

[0101] Calculate the deviation of the acetylene gas tank liquid level from the set value according to the following formula:

[0102]

[0103] in, Indicates the rate of change of the acetylene gas tank liquid level. Indicates the current value of the acetylene gas tank liquid level. Indicates the last cycle value of the acetylene gas tank liquid level. Indicates the deviation of the acetylene gas tank liquid level from the set value. Indicates the acetylene gas tank liquid level setting value.

[0104] Step S503: Calculate the carbide flow balance value required for preparing acetylene according to the following formula:

[0105]

[0106] in, Indicates the incremental output of the set value of the acetylene preparation flow into the generator calcium carbide flow. Indicates the current value of the setting value of the calcium carbide flow rate for preparing acetylene into the generator. Indicates the conversion coefficient of acetylene flow into calcium carbide flow. It indicates the calculation of the acetylene flow rate into the converter for preparing vinyl chloride. Indicates the weighted coefficient of the rate of change of the acetylene gas tank liquid level, Indicates the rate of change of the acetylene gas tank. Indicates the weighted coefficient of the acetylene gas tank liquid level deviation from the set value. Indicates the deviation of the acetylene gas tank liquid level from the set value.

[0107] Step S504: Based on the calcium carbide flow balance value of the generator calculated in step S503, according to the adjustable load margin of each generator, 1 The feed load is balanced among the generators.

[0108] (1) When hour

[0109] Calculate M 1 Each generator has an adjustable calcium carbide load upper margin:

[0110]

[0111] Calculate M 1 Each generator is assigned calcium carbide load:

[0112]

[0113] in, Indicates the upper margin of calcium carbide flow rate of each generator. Indicates the upper limit of calcium carbide flow rate of each generator. Indicates the current value of the calcium carbide flow setting value of each generator. Indicates the output value of the calcium carbide flow setting value of each generator, Indicates M 1 The total set value of calcium carbide flow rate for each generator.

[0114] (2) When hour

[0115] Calculate M 1 Each generator has adjustable calcium carbide flow rate under load margin:

[0116]

[0117] Calculate M 1 Each generator is assigned a calcium carbide flow load:

[0118]

[0119] in, Indicates the lower margin of calcium carbide flow rate for each generator. Indicates the lower limit of calcium carbide flow rate for each generator. Indicates the current value of the calcium carbide flow setting value of each generator. Indicates the output value of the calcium carbide flow setting value of each generator, Indicates M 1 The total set value of calcium carbide flow rate for each generator.

[0120] A plant-wide material coordination control system for a polyvinyl chloride production process executes the steps in the plant-wide material coordination control method for a polyvinyl chloride production process.

[0121] Compared with the prior art, this technical solution has the following characteristics:

[0122] (1) The coordinated material control of the acetylene production line, synthesis production line, conversion production and polymerization production line in the polyvinyl chloride production process is realized, making the production process more stable.

[0123] (2) The polymerization production line converts intermittent production data into continuous production data, which is conducive to coordinating the balance of upstream and downstream material quantities.

[0124] (3) For the polymerization production line, the set values ​​of the PVC flow rate into the stripping tower and the PVC flow rate into the drying bed are obtained by the average flow rate of PVC out of the polymerization kettle, and the incremental control method is adopted.

[0125] (4) For the conversion production line, the set value of the acetylene flow rate entering the converter is obtained by the average flow rate of vinyl chloride entering the polymerization reactor, the liquid level of the gas holder, and the liquid level of the spherical tank, and the incremental control method is adopted. The set value of the hydrogen chloride flow rate is obtained based on the proportional relationship with acetylene.

[0126] (5) For the synthesis production line, the chlorine flow set value is calculated by the conversion production line and balanced. The hydrogen set value is obtained based on the ratio with chlorine. The brine and electricity required for electrolysis are calculated based on chlorine and balanced.

[0127] (6) For acetylene production line, the carbide flow set value is calculated from the conversion production line and the gas tank liquid level, and balanced distribution is performed. BRIEF DESCRIPTION OF THE DRAWINGS

[0128] Figure 1 This is a schematic diagram of the material flow chart of the whole plant for producing PVC in the present invention;

[0129] Figure 2 It is a schematic diagram of the coordinated control system of the present invention;

[0130] Figure 3 It is a schematic flow chart of the whole plant material coordination control method of the polyvinyl chloride production process of the present invention;

[0131] Figure 4 It is a schematic diagram of calculating the average flow rate of vinyl chloride monomer consumed and the average flow rate of polyvinyl chloride produced by the polymerization production line of the present invention;

[0132] Figure 5 A schematic diagram of the balance value of the polyvinyl chloride flow rate into the stripping tower and the polyvinyl chloride flow rate into the drying bed of the polymerization production line according to the present invention;

[0133] Figure 6 A schematic diagram of calculating the balance value of acetylene flow and hydrogen chloride flow into the converter of the conversion production line of the present invention;

[0134] Figure 7 A schematic diagram of calculating the flow rates of hydrogen and chlorine entering the synthesis furnace of the synthesis production line of the present invention, and the flow rate of brine required for preparing hydrogen and chlorine;

[0135] Figure 8 The present invention is a schematic diagram of calculating the calcium carbide flow rate of an acetylene production line entering an acetylene generator. DETAILED DESCRIPTION

[0136] In order to better explain the present invention and facilitate understanding, the present invention is described in detail below through specific implementation modes in conjunction with the accompanying drawings.

[0137] like Figure 1As shown, a material coordination control method and system for the whole plant of the polyvinyl chloride production process is to perform material balance control on each polyvinyl chloride production line. The basic process flow is: in the acetylene production line, calcium carbide reacts with water in the generator to generate acetylene; in the synthesis production line, salt water is electrolyzed in the electrolytic cell to produce hydrogen and chlorine, which react in the synthesis furnace to generate hydrogen chloride; in the conversion production line, acetylene and hydrogen chloride react in the converter to generate vinyl chloride; in the polymerization production line, vinyl chloride generates slurry-like polyvinyl chloride in the polymerization kettle, which is then passed through the stripping tower and drying bed to produce powdered polyvinyl chloride, which is finally transported to packaging to form a product. In order to ensure the stable operation of the production process, it is necessary to balance the material quantity of each production line in real time.

[0138] like Figure 2 As shown, a method for coordinated control of materials in the whole plant of a polyvinyl chloride production process of the present invention can be implemented on an independent server (high-performance desktop computer), and an intelligent control platform (which can be implemented using Python) is deployed on the independent server to perform the algorithm design of the present invention, and data acquisition and control are performed through the OPC communication protocol with the acetylene production line, synthesis production line, conversion production line, polymerization production line, and control system.

[0139] To facilitate the description of the implementation process of the present invention, general data are used in the description of the implementation process. The main purpose is to describe the calculation process of the method of the present invention. The specific data depends on the circumstances. It is known that a polyvinyl chloride factory is equipped with 18 sets of acetylene generators, 6 sets of synthesis furnaces, 4 sets of electrolytic cells, 15 sets of converters, 6 sets of polymerization kettles, 1 stripping tower, and 1 set of drying bed.

[0140] According to the method proposed by the present invention, Figure 3 As shown, the following calculations are performed respectively:

[0141] Step S01: Calculate the average flow rate of vinyl chloride monomer consumed and the average flow rate of polyvinyl chloride produced by the polymerization production line by converting the batch production process into continuous production process data.

[0142] Step S02: Calculate the balance value of the polyvinyl chloride flow rate entering the stripping tower and the polyvinyl chloride flow rate entering the drying bed of the polymerization production line according to the average flow rate of the vinyl chloride monomer calculated in step S01.

[0143] Step S03: Calculate the balance value of acetylene flow and hydrogen chloride flow entering the converter of the conversion production line according to the average flow of vinyl chloride monomer, the liquid level of the vinyl chloride gas tank, and the liquid level of the vinyl chloride monomer spherical tank calculated in step S01.

[0144] Step S04: Based on the hydrogen chloride flow rate required for preparing vinyl chloride calculated in step S03, calculate the hydrogen and chlorine flow rates entering the synthesis furnace of the synthesis production line, as well as the brine flow rate required for preparing hydrogen and chlorine.

[0145] Step S05: Calculate the calcium carbide flow rate of the acetylene production line entering the acetylene generator according to the acetylene flow rate required for preparing vinyl chloride calculated in step S03.

[0146] Furthermore, if Figure 4 As shown, step S01 includes the following functions:

[0147] Step S101: Obtain the first W=10 polymerization kettle production brands currently being scheduled for production on the polymerization production line, the total amount of vinyl chloride monomer added to each production brand, the time for adding vinyl chloride monomer to each production brand, and the time for discharging polyvinyl chloride produced by each production brand.

[0148] It is known that there are 5 production formulas for polymerization. The formula of each polymerization kettle can be the same or different. Get the production grades of the first W=10 polymerization kettles:

[0149]

[0150]

[0151] Formula value of total amount of vinyl chloride monomer added to each production grade:

[0152]

[0153] Conversion coefficient of the total amount of PVC output produced by each production grade, which represents the output of PVC slurry under each grade:

[0154]

[0155] The time for adding vinyl chloride monomer to each production brand is calculated based on the historical data of each brand:

[0156]

[0157] Discharging time of PVC produced by each production grade:

[0158]

[0159] Step S102: Calculate the average flow rate of vinyl chloride monomer entering the polymerization reactor.

[0160] It is known that the duration of not adding vinyl chloride monomer to the current polymerization reactor Calculate the average flow rate of vinyl chloride monomer entering the polymerization kettle at the current moment:

[0161]

[0162] Step S103: Calculate the average flow rate of polyvinyl chloride out of the polymerization reactor.

[0163] Duration of time when all polymerization reactors do not discharge PVC The calculation formula for the average flow rate of polyvinyl chloride out of the polymerization kettle is:

[0164]

[0165] Furthermore, if Figure 5 As shown, step S02 includes the following functions:

[0166] Step S201: Obtain the set value of the polyvinyl chloride flow rate entering the stripping tower and the set value of the polyvinyl chloride flow rate entering the drying bed of the polymerization production line.

[0167] It is known that the current set value of the polyvinyl chloride flow rate into the stripping tower is PVC flow setting value into the drying bed Current value of average flow rate of polyvinyl chloride out of polymerization kettle The average flow rate of PVC out of the polymerization kettle in the last cycle

[0168] Step S202: Calculate the flow balance value of polyvinyl chloride entering the stripping tower.

[0169] Setting controller parameters The flow rate of polyvinyl chloride into the stripping tower is:

[0170]

[0171] Step S203: Calculate the flow balance value of polyvinyl chloride into the drying bed.

[0172] Setting controller parameters The flow rate of polyvinyl chloride entering the drying bed is:

[0173]

[0174] Furthermore, if Figure 6 As shown, step S03 includes the following functions:

[0175] Step S301: Obtain the set values ​​of the acetylene flow rate and hydrogen chloride flow rate entering the converter of the conversion production line, the liquid level of the vinyl chloride gas tank, and the liquid level of the vinyl chloride monomer spherical tank.

[0176] It is known that the current set value of the acetylene flow into the converter is Current setting value of hydrogen chloride flow Current value of the liquid level of vinyl chloride gas tank Last cycle value of the liquid level of vinyl chloride gas tank Vinyl chloride gas tank liquid level setting value Current value of liquid level of vinyl chloride monomer spherical tank Last cycle value of the liquid level of the vinyl chloride monomer spherical tank Vinyl chloride monomer spherical tank liquid level setting value Current value of vinyl chloride monomer flow into polymerization reactor The last cycle value of the vinyl chloride monomer flow into the polymerization kettle The ratio of hydrogen chloride to acetylene is

[0177] Step S302: Calculate the relative remaining amount of the vinyl chloride monomer spherical tank liquid level.

[0178] Calculate the rate of change of liquid level in the vinyl chloride monomer spherical tank:

[0179]

[0180] Calculate the deviation of the liquid level of the vinyl chloride monomer spherical tank from the set value:

[0181]

[0182] Step S303: Calculate the relative remaining amount of the vinyl chloride gas tank liquid level.

[0183] Calculate the rate of change of the liquid level in the vinyl chloride gas tank:

[0184]

[0185] Calculate the deviation of the vinyl chloride gas tank liquid level from the set value:

[0186]

[0187] Step S304: Calculate the flow balance value of acetylene entering the converter required for preparing vinyl chloride.

[0188] Known, set the controller parameters Calculate the balance value of acetylene flow into the converter required for the preparation of vinyl chloride:

[0189]

[0190] Step S305: Calculate the flow balance value of hydrogen chloride entering the converter required for preparing vinyl chloride.

[0191] The balance value of the flow rate of hydrogen chloride into the converter required for the preparation of vinyl chloride is calculated as follows:

[0192]

[0193] Furthermore, if Figure 7 As shown, step S04 includes the following functions:

[0194] Step S401: Obtain the set values ​​of the chlorine flow rate and hydrogen flow rate entering the synthesis furnace of the synthesis production line, and the set values ​​of the brine flow rate entering the electrolytic cell and the amount of electricity in the electrolytic cell.

[0195] It is known that the current value of the chlorine flow setting is The hydrogen flow rate is set to The ratio of hydrogen flow to chlorine flow is Electrolyzer brine flow rate, electrolyzer power setting value

[0196] Step S402: Calculate the flow rate of chlorine gas entering the synthesis furnace required for preparing hydrogen chloride.

[0197] Known controller parameters Controller bias parameters The flow balance calculation formula for calculating the chlorine gas entering the synthesis furnace required for the preparation of hydrogen chloride is:

[0198]

[0199] Step S403: For the total set value of the chlorine flow rate calculated in step S402, according to the adjustable load margin of each synthesis furnace, 2 =6 synthesis furnaces for balanced feed load distribution.

[0200] because

[0201] It is known that the lower limit of the chlorine flow rate of the synthesis furnace is

[0202] The setting value of chlorine gas flow rate in the synthesis furnace is

[0203] Calculate M 2 = 6 synthesis furnaces with adjustable chlorine flow rate under load margin, the calculation results for each synthesis furnace are as follows:

[0204] Station 1:

[0205] Station 2:

[0206] Station 3:

[0207] Channel 4:

[0208]

[0209] Channel 5:

[0210]

[0211] Channel 6:

[0212]

[0213] Calculate M 2 = 6 synthesis furnaces, each of which is assigned chlorine flow load:

[0214] Station 1:

[0215]

[0216] Station 2:

[0217]

[0218] Station 3:

[0219]

[0220] Channel 4:

[0221]

[0222] Channel 5:

[0223]

[0224] Channel 6:

[0225]

[0226] Step S404: Calculate the flow rate of hydrogen entering the synthesis furnace required for preparing hydrogen chloride.

[0227] Calculate the flow balance of hydrogen into the synthesis furnace required for the preparation of hydrogen chloride:

[0228] Station 1:

[0229] Station 2:

[0230] Station 3:

[0231] Channel 4:

[0232] Channel 5:

[0233] Channel 6:

[0234] Step S405: Calculate the brine flow rate into the electrolytic cell required for preparing the chlorine flow rate.

[0235] It is known that the current total brine flow setting value is

[0236] Setting controller parameters Calculate the brine flow rate required to produce chlorine flow:

[0237]

[0238] Step S406: For the total brine set value increment output value calculated in step S405, according to the adjustable load margin of each electrolytic cell, 3 =4 electrolytic cells for balanced feed load distribution.

[0239] Because when hour

[0240] Calculate M 3 = 4 electrolytic cells, each with adjustable brine load margin:

[0241] It is known that the lower limit of the chlorine flow rate of the synthesis furnace is The setting value of chlorine gas flow rate in the synthesis furnace is

[0242] Station 1:

[0243] Station 2:

[0244] Station 3:

[0245] Channel 4:

[0246] Calculate M 3 =4 electrolytic cells, each with its own brine load:

[0247] Station 1:

[0248] Station 2:

[0249] Station 3:

[0250] Channel 4:

[0251] Furthermore, if Figure 8 As shown, step S05 includes the following functions:

[0252] Step S501: Obtain the carbide flow setting value of the acetylene production line and the liquid level of the acetylene gas tank.

[0253] It is known that the calcium carbide flow setting value Current value of acetylene gas tank liquid level Acetylene gas tank liquid level last cycle value Acetylene gas tank liquid level setting value

[0254] Step S502: Calculate the rate of change of the acetylene gas tank liquid level.

[0255] Calculate the rate of change of the acetylene tank liquid level:

[0256]

[0257] Calculate the deviation of the acetylene gas tank liquid level from the set value:

[0258]

[0259] Step S503: Calculate the calcium carbide flow balance value required for preparing acetylene.

[0260] Known, the control coefficient Calculate the incremental output of the set value of the acetylene flow rate into the generator:

[0261]

[0262] Step S504: Output the incremental value of the calcium carbide flow rate of the generator calculated in step S503, and adjust the M according to the adjustable load margin of each generator. 1 The feed load is balanced among the generators.

[0263] because

[0264] It is known that the lower limit of the acetylene generator calcium carbide flow rate is Calcium carbide flow setting value

[0265] Calculate M 1=18 generators, each with adjustable calcium carbide flow rate, load margin:

[0266] Station 1:

[0267]

[0268] Station 2:

[0269]

[0270]

[0271] And so on

[0272] Channel 18:

[0273]

[0274] Calculate M 1 = 18 generators, each with its own carbide flow load:

[0275] Station 1:

[0276] Station 2:

[0277] And so on, the 18th station:

Claims

1. A method for coordinated control of materials in the whole plant during the production process of polyvinyl chloride. It is characterized in that The steps include: Step S01: converting the batch production process into continuous production process data to calculate the average flow rate of vinyl chloride monomer consumed by the polymerization production line and the average flow rate of polyvinyl chloride produced; Step S02: Calculate the balance value of the polyvinyl chloride flow rate entering the stripping tower and the polyvinyl chloride flow rate entering the drying bed of the polymerization production line according to the average flow rate of the vinyl chloride monomer calculated in step S01; Step S03: Calculate the balance value of acetylene flow and hydrogen chloride flow entering the converter of the conversion production line according to the average flow of vinyl chloride monomer, the liquid level of the vinyl chloride gas tank, and the liquid level of the vinyl chloride monomer spherical tank calculated in step S01; Step S04: according to the hydrogen chloride flow rate required for preparing vinyl chloride calculated in step S03, calculate the balance value of the flow rates of hydrogen and chlorine entering the synthesis furnace of the synthesis production line, as well as the brine flow rate required for preparing hydrogen and chlorine, and balance the feed load distribution of the synthesis furnace and the electrolytic cell; Step S05: Based on the acetylene flow rate required for preparing vinyl chloride calculated in step S03, the calcium carbide flow rate entering the acetylene generator from the acetylene production line is calculated, and the feed load of the generator is balanced and distributed.

2. A method for coordinated control of materials in the whole plant of a polyvinyl chloride production process according to claim 1, It is characterized in that The step S01 comprises the following steps: Step S101: obtaining the production grades of the first W polymerization kettles currently being scheduled for production in the polymerization production line, the total amount of vinyl chloride monomer added to each production grade, the time for adding vinyl chloride monomer to each production grade, and the time for discharging polyvinyl chloride produced by each production grade; Step S102: Calculate the average flow rate of vinyl chloride monomer into the polymerization kettle according to the following formula: in, represents the average flow rate of vinyl chloride monomer into the polymerization kettle, W represents the first W polymerization kettles scheduled for production, represents the name of the i-th brand, It indicates the average time of adding vinyl chloride monomer to each production grade. Indicates the discharge time of polyvinyl chloride produced by each production grade, It indicates the duration of time when no vinyl chloride monomer is added to any polymerization reactor; Step S103: Calculate the average flow rate of polyvinyl chloride out of the polymerization kettle according to the following formula: in, represents the average flow rate of polyvinyl chloride slurry out of the polymerization kettle, W represents the first W polymerization kettles in production, represents the name of the i-th brand, Indicates the time of adding vinyl chloride monomer to each production grade. It indicates the conversion coefficient of the total amount of PVC produced by each production grade. It indicates the average time of discharging PVC for each production grade. It indicates the duration during which no polymerization reactor discharges polyvinyl chloride.

3. A method for coordinated control of materials in the whole plant of polyvinyl chloride production process according to claim 1, It is characterized in that The step S02 comprises the following steps: Step S201: obtaining the set value of the polyvinyl chloride flow rate entering the stripping tower and the set value of the polyvinyl chloride flow rate entering the drying bed of the polymerization production line; Step S202: Calculate the flow balance value of polyvinyl chloride into the stripping tower according to the following formula: in, It represents the flow balance value of polyvinyl chloride into the stripping tower. Indicates the current value of the polyvinyl chloride flow rate into the stripping tower. It represents the weighted coefficient of the PVC flow balance control into the stripping tower, It indicates the current value of the average flow rate of polyvinyl chloride in the polymerization kettle. It shows the average flow rate of polyvinyl chloride in the polymerization kettle in the last cycle; Step S203: Calculate the flow balance value of polyvinyl chloride into the drying bed according to the following formula: in, Indicates the flow balance value of polyvinyl chloride into the drying bed, Indicates the current value of the set value of the polyvinyl chloride flow entering the drying bed. represents the weighting coefficient of the drying balance controller, It indicates the current value of the average flow rate of polyvinyl chloride in the polymerization kettle. It shows the average flow rate of polyvinyl chloride in the polymerization kettle in the previous cycle.

4. A method for coordinated control of materials in the whole plant of a polyvinyl chloride production process according to claim 1, It is characterized in that The step S03 comprises the following steps: Step S301: obtaining the set values ​​of the acetylene flow rate and hydrogen chloride flow rate entering the converter of the conversion production line, the liquid level of the vinyl chloride gas tank, and the liquid level of the vinyl chloride monomer spherical tank; Step S302: Calculate the relative remaining amount of the liquid level of the vinyl chloride monomer spherical tank, where the relative remaining amount of the liquid level of the vinyl chloride monomer spherical tank is the sum of the rate of change of the liquid level of the vinyl chloride monomer spherical tank and the deviation of the liquid level of the vinyl chloride monomer spherical tank from the set value; Calculate the rate of change of liquid level in the vinyl chloride monomer spherical tank: Calculate the deviation of the liquid level of the vinyl chloride monomer spherical tank from the set value: in, Indicates the rate of change of the liquid level in the vinyl chloride monomer spherical tank, Indicates the current value of the liquid level in the vinyl chloride monomer spherical tank. Indicates the last cycle value of the liquid level in the vinyl chloride monomer spherical tank. Indicates the deviation of the liquid level of the vinyl chloride monomer spherical tank from the set value. Indicates the liquid level setting value of the vinyl chloride monomer spherical tank; Step S303: Calculate the relative remaining amount of the vinyl chloride gas tank liquid level, where the relative remaining amount of the vinyl chloride gas tank liquid level is the sum of the vinyl chloride gas tank liquid level change rate and the vinyl chloride gas tank liquid level deviation from the set value; Calculate the rate of change of the liquid level in the vinyl chloride gas tank: Calculate the deviation of the vinyl chloride gas tank liquid level from the set value: in, Indicates the rate of change of the liquid level in the vinyl chloride tank. Indicates the current value of the vinyl chloride gas tank liquid level. Indicates the last cycle value of the vinyl chloride gas tank liquid level. Indicates the deviation of the liquid level of the vinyl chloride gas tank from the set value. Indicates the set value of the liquid level of the vinyl chloride gas tank; Step S304: Calculate the flow balance value of acetylene into the converter required for preparing vinyl chloride according to the following formula: in, Indicates the output of the set value of the acetylene flow rate into the vinyl chloride converter. Indicates the current value of the acetylene flow setting value entering the vinyl chloride converter. The acetylene weighting coefficient of the rate of change of the liquid level in the vinyl chloride monomer spherical tank is expressed as: Indicates the rate of change of the liquid level in the vinyl chloride monomer spherical tank, Indicates the acetylene weighting coefficient of the deviation of the liquid level of the vinyl chloride monomer spherical tank from the set value. Indicates the deviation of the liquid level of the vinyl chloride monomer spherical tank from the set value. Indicates the acetylene weighting coefficient of the rate of change of the liquid level in the vinyl chloride gas tank, Indicates the rate of change of the liquid level in the vinyl chloride tank. Indicates the acetylene weighting coefficient of the ethylene chloride tank liquid level deviation from the set value. Indicates the deviation of the liquid level of the vinyl chloride gas tank from the set value. represents the weighted coefficient of the average flow rate change of vinyl chloride monomer, Indicates the current value of the average flow rate of vinyl chloride monomer, It indicates the value of the average flow rate of vinyl chloride monomer in the previous cycle; Step S305: Calculate the flow balance value of hydrogen chloride entering the converter required for preparing vinyl chloride according to the following formula: in, Indicates the output of the hydrogen chloride flow rate setting value of the converter. represents the ratio coefficient of hydrogen chloride to acetylene, Indicates the acetylene flow setting value.

5. The whole-plant material coordination control method for polyvinyl chloride production process according to claim 1, It is characterized in that The step S04 comprises the following steps: Step S401: obtaining the set values ​​of chlorine flow rate and hydrogen flow rate into the synthesis furnace of the synthesis production line, and the set value of brine flow rate into the electrolytic cell; Step S402: Calculate the flow balance value of chlorine gas entering the synthesis furnace required for preparing hydrogen chloride according to the following formula: in, Indicates the balance value of chlorine flow required to enter the synthesis furnace, Indicates the current value of the total set value of the chlorine gas flow required to enter the synthesis furnace. It represents the conversion coefficient of hydrogen chloride flow into chlorine flow, Indicates the set value of hydrogen chloride flow into the vinyl chloride converter. Indicates the loss bias caused by pipeline resistance; Step S403: Based on the flow balance value of chlorine gas into the synthesis furnace required for preparing hydrogen chloride calculated in step S402, according to the adjustable load margin of each synthesis furnace, 2 Balance the feed load distribution for each synthesis furnace: (1) When hour Calculate M 2 Each synthesis furnace can adjust the chlorine gas flow load upper margin: Calculate M 2 Each synthesis furnace is assigned chlorine gas flow load: in, Indicates the upper margin of chlorine flow rate of each synthesis furnace, Indicates the upper limit of chlorine flow rate for each synthesis furnace. Indicates the current value of the chlorine flow setting value of each synthesis furnace. Indicates the output value of the chlorine flow setting value of each synthesis furnace, Indicates M 2 Total set value of chlorine gas flow rate of each synthesis furnace; (2) When hour Calculate M 2 Adjustable chlorine flow rate under load margin of each synthesis furnace: Calculate M 2 Each synthesis furnace is assigned chlorine gas flow load: in, Indicates the margin of chlorine flow rate of each synthesis furnace, Indicates the lower limit of chlorine flow rate for each synthesis furnace, Indicates the current value of the chlorine flow setting value of each synthesis furnace. Indicates the output value of the chlorine flow setting value of each synthesis furnace, Indicates M 2 Total set value of chlorine gas flow rate of each synthesis furnace; Step S404: Calculate the flow balance value of hydrogen entering the synthesis furnace required for preparing hydrogen chloride according to the following formula: in, Indicates entry 2 The balance value of hydrogen flow required for each synthesis furnace, It represents the ratio coefficient of chlorine flow rate to hydrogen flow rate, Indicates the current value of the chlorine gas flow setting value of each synthesis furnace; Step S405: Calculate the brine flow rate required to prepare the chlorine flow rate according to the following formula: in, Indicates the incremental output value of the total set value of the brine flow required to prepare the hydrogen flow. Indicates the current value of the total set value of the brine flow required to prepare the hydrogen flow. Indicates the conversion coefficient of hydrogen flow into brine flow, Indicates the chlorine gas flow setting value, Indicates the loss coefficient caused by pipeline resistance; Step S406: Based on the total set value increment output value of the brine flow calculated in step S405, according to the adjustable load margin of each electrolyzer, 3 Feed load balancing distribution for each electrolyzer: (1) When hour Calculate M 3 Each electrolyzer can adjust the upper margin of brine load: Calculate M 3 Each electrolyzer is assigned brine load: in, Indicates the upper margin of brine flow rate for each electrolytic cell, Indicates the upper limit of brine flow rate for each electrolyzer, Indicates the current value of the brine flow setting value of each electrolytic cell, Indicates the output value of the brine flow setting value of each electrolytic cell, Indicates M 3 Total set value of brine flow rate of each electrolyzer; (2) When hour Calculate M 3 Each electrolyzer has adjustable brine load margin: Calculate M 3 Each electrolyzer is assigned brine load: in, Indicates the margin of brine flow rate for each electrolyzer, Indicates the lower limit of brine flow rate for each electrolyzer, Indicates the current value of the brine flow setting value of each electrolytic cell, Indicates the output value of the brine flow setting value of each electrolytic cell, Indicates M 3 The total set value of brine flow rate for each electrolyzer.

6. A method for coordinated control of materials in the whole plant of polyvinyl chloride production process according to claim 1, It is characterized in that The step S05 comprises the following steps: Step S501: obtaining the carbide flow setting value of the acetylene production line and the liquid level of the acetylene gas tank; Step S502: Calculate the rate of change of the acetylene gas tank liquid level according to the following formula: Calculate the deviation of the acetylene gas tank liquid level from the set value according to the following formula: in, Indicates the rate of change of the acetylene gas tank liquid level. Indicates the current value of the acetylene gas tank liquid level. Indicates the last cycle value of the acetylene gas tank liquid level. Indicates the deviation of the acetylene gas tank liquid level from the set value. Indicates the set value of the acetylene gas tank liquid level; Step S503: Calculate the carbide flow balance value required for preparing acetylene according to the following formula: in, It indicates the balance value of the flow rate of acetylene into the generator. Indicates the current value of the setting value of the calcium carbide flow rate for preparing acetylene into the generator. Indicates the conversion coefficient of acetylene flow into calcium carbide flow. It indicates the calculation of the acetylene flow rate into the converter for preparing vinyl chloride. Indicates the weighted coefficient of the rate of change of the acetylene gas tank liquid level, Indicates the rate of change of the acetylene gas tank. Indicates the weighted coefficient of the acetylene gas tank liquid level deviation from the set value. Indicates the deviation of the acetylene gas tank liquid level from the set value; Step S504: Based on the calcium carbide flow balance value calculated in step S503, according to the adjustable load margin of each generator, 1 Generators for feed load balancing distribution: (1) When hour Calculate M 1 Each generator has an adjustable calcium carbide load upper margin: Calculate M 1 Each generator is assigned calcium carbide load: in, Indicates the upper margin of calcium carbide flow rate of each generator, Indicates the upper limit of calcium carbide flow rate of each generator. Indicates the current value of the calcium carbide flow setting value of each generator. Indicates the output value of the calcium carbide flow setting value of each generator, Indicates M 1 The total setting value of calcium carbide flow rate of each generator; (2) When hour Calculate M 1 Each generator has adjustable calcium carbide flow rate under load margin: Calculate M 1 Each generator is assigned a calcium carbide flow load: in, Indicates the lower margin of calcium carbide flow rate for each generator, Indicates the lower limit of calcium carbide flow rate for each generator. Indicates the current value of the calcium carbide flow setting value of each generator. Indicates the output value of the calcium carbide flow setting value of each generator, Indicates M 1 The total set value of calcium carbide flow rate for each generator.

7. A material coordination control system for the whole plant in the polyvinyl chloride production process. It is characterized in that Execute the steps in the whole-plant material coordination control method for the polyvinyl chloride production process as described in any one of claims 1-6.

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