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    • 专利摘要:
    method for producing compost and system for producing a compost used in the production method. The present invention relates to a method for producing a compound using a continuous tank reactor which is provided with two or more reaction tanks for producing a compound and with a reaction liquid feed pipe that feeds a liquid of the reaction of an upstream reaction tank to a downstream reaction tank, wherein said method is characterized by the fact that the number of reynolds of the reaction liquid flowing in the reaction liquid feed pipe is set to be from 1,800 to 22,000. furthermore, such a compost production system is used in said method for making a compost, and is formed by housing at least one of the reaction tanks in a portable container.
    公开号:BR112016026871B1
    申请号:R112016026871-7
    申请日:2015-07-03
    公开日:2021-08-10
    发明作者:Makoto Kano；Takamitsu Kariya；Hiroyasu Banba；Tomohiko Mawatari；Takeshi Kato；Tsutomu HIRACHI；Keizo TACHIBANA；Masahiro KAMIDE；Megumu MORIMOTO
    申请人:Mitsubishi Chemical Corporation；
    IPC主号:
    专利说明:

    TECHNICAL FIELD
    [001] The present invention relates to a method for producing a compound and a compound production system used in the production method.
    [002] The present patent application claims priority based on Japanese Patent Application no. 2014-142688, filed July 10, 2014. The contents of the patent application are incorporated herein by reference in their entirety. BACKGROUND TECHNIQUE
    [003] A method for producing a target compound using a biocatalyst has the advantages that reaction conditions are mild, a level of purity of a reaction product is high with fewer by-products, and a production process can be simplified. Therefore, such a method is used for the production of various compounds. For example, in the production of an amide compound such as acrylamide, since a nitrile hydratase, which is an enzyme for the conversion of a nitrile compound such as acrylonitrile to an amide compound, is found, the production of an amide compound that uses the enzyme has been widely realized.
    [004] Furthermore, in recent years, the production of acrylamide has been carried out through the continuous reaction using a nitrile hydratase. As an example of the methods for producing acrylamide by continuous reaction, a method for producing acrylamide described in Patent Publication 1 which is aimed at obtaining low costs, energy savings, and low environmental loads is mentioned. In Patent Publication 1, it is described that, in the production of acrylamide by the continuous reaction using a nitrile hydratase, the enzyme reaction is carried out under the conditions of a predetermined agitation energy and a predetermined Froude number. LIST OF QUOTES PATENT PUBLICATION
    [005] Patent Publication 1: WO 09/113654 A SUMMARY OF THE INVENTION PROBLEM TO BE SOLVED BY THE INVENTION
    [006] From the point of view of space limitation which is a general problem, also in the production of acrylamide by continuous reaction when using a nitrile hydratase, it is also desirable that space savings be obtained by improving the production efficiency.
    [007] In this regard, an object of the invention is to provide a method for the production of a compound using continuous reaction in which space savings are obtained by improving production efficiency (without a decrease in production efficiency. production). MEANS TO SOLVE THE PROBLEM
    [008] The authors of the present invention performed intensive studies and, as a consequence, found that when a Reynolds number of a reaction liquid flowing in a reaction liquid feed pipe is adjusted to be in a predetermined range, the The problem described above can be solved, thereby completing the invention.
    [009] That is, the invention includes the following configurations.[1] A method for producing a compound using a continuous tank reactor that is provided with two or more reaction tanks for the production of a compound and a reaction liquid feed pipe that feeds a reaction liquid from a tank upstream reaction tank in a downstream reaction tank, where a Reynolds number of the reaction liquid flowing in the reaction liquid feed piping is set from 1800 to 22,000.[2] A compost production system that is used in the method for making a compost described in [1], wherein at least one tank of reaction tanks is accommodated in a portable container.[3] The compound production system described in [2], wherein when at least one tank of reaction tanks is accommodated in the portable container, a total volume of at least one tank of reaction tanks accommodated in the portable container is 1/ 6 to 3/5 of an internal volume of the portable container.[4] The method for producing a compost described in [1], where the method uses the compost production system described in [2], and a value obtained by dividing an internal volume (m3) of the portable container by a flow rate (m3/h) of the reaction liquid flowing in the reaction tank accommodated in the portable container is 5 to 70 hours.[5] The system for producing a compound described in [2] or [3], in which another portable container is disposed in the portable container in which the reaction tank is accommodated.[6] A method for producing acrylamide using the method for producing a compound described in [1], wherein the method for producing acrylamide includes: a step of feeding a liquid containing acrylonitrile to at least one tank of tanks of reaction; a step of feeding natural water to at least one tank of the reaction tanks; and a step of feeding an aqueous dispersion of biocatalyst to at least one tank of the reaction tanks.[7] The compost production system described in [2], in which a reaction tank volume accommodated in the portable container is from 6.4 m3 to 22.9 m3.[8] The production system for a compound described in [2], wherein the compound is an amide compound.[9] The production system for a compound described in [2], wherein the compound is acrylamide. EFFECT OF THE INVENTION
    [0010] According to the invention, it is possible to provide a method for producing a compound using continuous reaction in which space savings are obtained without a decrease in production efficiency. Furthermore, a production system of the invention can run in a place where there is a demand for the use of the production system and can start industrial production of a compost in a short time. BRIEF DESCRIPTION OF THE DRAWINGS
    [0011] Figure 1 is a schematic cross-sectional view illustrating an embodiment of a continuous tank reactor used in a method for producing a compound of the invention; and
    [0012] Figure 2 is a schematic cross-sectional view illustrating another embodiment of a system for producing a compound used in the method for producing a compound of the invention. WAY TO CARRY OUT THE INVENTION Modality of the Method for Production of a Compost
    [0013] Hereinafter, as an embodiment of a method for producing a compound of the invention, an embodiment in which acrylamide is produced using a continuous tank reactor 1 by the hydration of acrylonitrile which serves as a raw material in the presence of a biocatalyst will be described using Figure 1. Continuous Tank Reactor
    [0014] The continuous tank reactor 1 illustrated in Figure 1 is provided with eight reaction tanks 10 for the production of a compound. In addition, the continuous tank reactor 1 is provided with an acrylonitrile feed line 21 that feeds a liquid containing acrylonitrile to the reaction tank 10, a catalyst feed line 22 that feeds an aqueous dispersion of biocatalyst to the reaction tank. reaction 10, and a natural water feed pipe 23 which feeds natural water to the reaction tank 10. In addition, the continuous tank reactor 1 can be provided with an acid/alkali solution feed pipe 25 which feeds acid or alkali in order to control a pH of the reaction liquid in the reaction tank 10.
    [0015] Furthermore, the continuous tank reactor 1 is provided with a stirring paddle 24 which stirs the reaction liquid obtained by mixing the liquid containing acrylonitrile, the aqueous biocatalyst dispersion, and the natural water. In addition, the continuous tank reactor 1 is provided with a reaction liquid feed piping 26 which feeds the reaction liquid coming from the upstream reaction tank to the downstream reaction tank between the reaction tanks 10. In addition, the continuous tank reactor 1 is provided with a reaction product collection pipe 27 which collects an aqueous solution containing acrylamide from the reaction tank further downstream between the reaction tanks 10.
    [0016] The liquid feed into the reaction liquid feed pipe 26 and the reaction product collection pipe 27 can be performed by using the potential energy generated by a difference between a height of the liquid surface of the reaction tank to upstream and a height of the liquid surface of the downstream reaction tank (hereafter referred to simply as the "liquid surface difference") or can be performed using pressure energy generated by a liquid feed pump. From the point of view of obtaining the simplification of the continuous tank reactor 1 and energy savings in production, the liquid feed is preferably carried out using potential energy.
    [0017] In the following, each configuration of continuous tank reactor 1 will be described in detail. Reaction Tank
    [0018] The reaction tanks 10 are further classified into a reaction tank 11 provided with at least one piping of the acrylonitrile feed pipe 21, the catalyst feed pipe 22, the natural water feed pipe 23, and the acid/alkali solution feed piping; a reaction tank 12 provided with reaction product collection piping 27; and a reaction tank 13 not provided with any such piping. Reaction tank 11 is typically positioned on the upstream side of the reaction liquid flow. In addition, reaction tank 12 is typically positioned on the downstream side of the reaction liquid flow and preferably positioned on the more downstream side. Furthermore, the reaction tank 13 can be provided in a case where the reaction tanks 10 are three or more in number, and in the case of the provision of the reaction tank 13, the reaction tank 13 is typically positioned between the reaction tank 11 and reaction tank 12 in the reaction liquid flow.
    [0019] Incidentally, the reaction tank 10 may be provided with a liquid surface sensor that measures the liquid surface of the reaction liquid in the tank.
    [0020] In addition, each reaction tank of the reaction tanks10 can be an independent reaction tank, or it can be a reaction tank obtained by dividing a larger reaction tank with a partition. In a case where each reaction tank is a reaction tank divided with a partition, in this mode, each space divided with a partition is counted as a tank.
    [0021] In addition, the 10 reaction tanks are two or more in number, and all the reaction tanks can be connected with each other. The reaction tanks 10 can be configured in such a way that at least some reaction tank can be connected in series or a reaction tank to be connected in parallel can be provided.
    [0022] The material of the reaction tank 10 is not particularly limited as long as it is not corroded by the reaction liquid, and stainless steel or the like is preferable.
    [0023] The shape of the reaction tank 10 is not particularly limited, as long as the reaction liquid in the reaction tank is agitated by the stirring paddle 24 and, for example, a cube shape, a cuboid shape, a cylindrical shape and still others are mentioned.
    [0024] The volume of the reaction tank 10 is not particularly limited and can be appropriately selected depending on the range or the like of the continuous tank reactor 1. For example, in a case where the reaction tank is accommodated in the portable container and used , the volume of the reaction tank as described later on can be selected. The shape and volume of reaction tank 10 is preferably adjusted in such a way that each tank or two or more tanks can be accommodated in the portable container.
    [0025] In a case where the production of the aqueous acrylamide solution is performed by continuous reaction, the aqueous acrylamide solution is produced in a continuous manner without collecting the entire reaction mixture in the reaction vessel while maintaining continuous introduction or intermittent feedstocks for the reaction (eg containing the aqueous dispersion of biocatalyst, natural water, and the liquid containing acrylonitrile) to the reaction vessel and the continuous or intermittent recovery of the reaction mixture (eg containing the acrylamide produced) from the reaction vessel. Acrylonitrile Feed Pipe and Natural Water Feed Pipe
    [0026] In this modality, a step of feeding the liquid containing acrylonitrile to the reaction tank and a step of feeding natural water to the reaction tank are included. These steps are carried out using the acrylonitrile feed piping 21 and the natural water feed piping 23, respectively.
    [0027] The material of the acrylonitrile feed piping 21 is not particularly limited, as long as it is not corroded by the liquid containing acrylonitrile. The material of the acrylonitrile feed pipe 21 is preferably, for example, stainless steel or the like.
    [0028] The inner diameter of the acrylonitrile feed pipe 21 is preferably 1 to 5 cm. When the inside diameter of the acrylonitrile feed pipe 21 is equal to or greater than the lower limit, the liquid containing acrylonitrile can be efficiently provided. On the other hand, when its internal diameter is equal to or smaller than the upper limit, space saving is also obtained.
    [0029] The internal diameter of the natural water supply pipe 23 is preferably from 2 to 10 cm. When the inner diameter of the natural water supply pipe 23 is equal to or greater than the lower limit, the pressure loss in the natural water supply pipe 23 can be decreased. On the other hand, when its internal diameter is equal to or smaller than the upper limit, space saving is also obtained.
    [0030] In order to control the amount of acrylamide production, it is preferable that each of the acrylonitrile feed pipe 21 and the natural water feed pipe 23 have a means of adjusting the flow rate of the acrylonitrile source ( for example, an acrylonitrile source flow adjustment unit) and a means of adjusting the natural water feed flow rate (for example, a natural water feed flow adjustment unit). As such an adjustment means, a method using a flow adjustment valve (eg a unit having a flow adjusting valve), a method of controlling the power of the liquid feed pump (eg a unit control of the power of the liquid feed pump) and the like are mentioned. The schemes of these adjustment means may be schemes that perform automatic control in such a way that the flow rate of the aqueous acrylamide solution flowing out of the reaction product collection pipe 27 by the excess flow is adjusted to be in cooperation with these adjusting means so that the flow rate of the aqueous acrylamide solution flowing out of the reaction product collection pipe 27 is adjusted to a predetermined range.
    [0031] An acrylonitrile feed port 28 in the acrylonitrile feed pipe 21 is preferably positioned in the vicinity of the stirring paddle 24 so that the acrylonitrile concentration in the reaction tank 11 is not partially increased. Catalyst Feed Pipe
    [0032] In this modality, a step of feeding the aqueous dispersion of biocatalyst to the reaction tank is included. The step is performed using catalyst feed line 22.
    [0033] The material of the catalyst feed pipe 22 is not particularly limited, as long as it is not corroded by the aqueous dispersion of biocatalyst. The material of the catalyst feed line 22 is preferably, for example, stainless steel or the like.
    [0034] The inside diameter of the catalyst feed pipe 22 is preferably 0.4 to 3 cm. When the inside diameter of the catalyst feed line 22 is equal to or greater than the lower limit, enzyme inactivation over time caused by long-term retention of the biocatalyst in the line can be suppressed. On the other hand, when its internal diameter is equal to or smaller than the upper limit, space saving is also obtained. It is preferred that the catalyst feed line 22 has a means of adjusting the catalyst source flow rate in order to control the rate of the reaction of acrylonitrile to acrylamide. As a means of adjusting the flow rate of the catalyst source (for example, a catalyst source flow adjustment unit), a method that uses a flow adjustment valve (a unit that has a flow adjustment valve), a liquid feed pump power control method (eg a liquid feed pump power control unit) and others are still mentioned. The scheme of the catalyst source flow adjustment means can be a scheme that performs the automatic control in such a way that the acrylamide concentration in the aqueous acrylamide solution that flows out of the reaction product collection pipe 27 and such as necessary, the acrylonitrile concentration is adjusted to be in cooperation with the catalyst source flow adjustment means so that the reaction rate of acrylonitrile in acrylamide is adjusted within a predetermined range.
    [0035] In the invention, the concentration of acrylamide in the aqueous acrylamide solution (which flows out of the reaction product collection pipe 27) after completion of the reaction is preferably 30 to 65% by mass, more preferably from 35 to 60% by mass, and even more preferably from 40 to 55% with respect to the mass of the aqueous acrylamide solution.
    [0036] When the acrylamide concentration is higher than 65% by mass, the acrylamide crystals easily precipitate at an almost normal temperature and thus a heating apparatus is required so that not only the installation costs are increased but also temperature control and other operations are complicated. Therefore, the concentration of acrylamide in the aqueous acrylamide solution in the invention is not particularly limited, as long as it is within a range in which the acrylamide crystals do not precipitate even at an almost normal temperature, and is preferably 65% by mass. or less, more preferably 60% by mass or less, and even more preferably 55% by mass or less.
    [0037] On the other hand, when the concentration of acrylamide is lower than 30% by mass, it is economically disadvantageous from an industrial point of view, since the volume of a tank to be used for storage or maintenance is excessive large or shipping costs are increased. Therefore, the concentration of acrylamide in the aqueous acrylamide solution is preferably 30% by mass or more, more preferably 35% by mass or more, and even more preferably 40% by mass or more.
    [0038] The concentration of unreacted acrylonitrile in the aqueous acrylamide solution is preferably 200 ppm or less and more preferably 100 ppm or less.
    [0039] When the concentration of unreacted acrylonitrile in the aqueous acrylamide solution is adjusted to 200 ppm or less, the quality of an acrylamide-based polymer obtained by the polymerization of acrylamide can be improved, and the above-described range of concentration is industrially preferable, since a yield of converting acrylonitrile to acrylamide is high.
    [0040] In order to adjust the concentration of unreacted acrylonitrile in the aqueous acrylamide solution to 200 ppm or less, the amount of feed or the like of the biocatalyst to be fed to the reaction tank can be appropriately adjusted. For example, when the unreacted acrylonitrile concentration in the aqueous acrylamide solution collected by the reaction product collection piping 27 is higher than 200 ppm, the amount of biocatalyst feed to be fed to the reaction tank can be increased.
    [0041] A biocatalyst feed port 29 in the catalyst feed pipe 22 is preferably positioned in the vicinity of the agitation paddle 24 so that the concentration of biocatalyst in reaction tank 10 is not partially increased. However, the biocatalyst can be fed from the upper surface of the reaction liquid. agitation paddle
    [0042] The material of the stirring blade 24 is not particularly limited, as long as it is not corroded by the reaction liquid and a predetermined stirring power can be obtained. As the material of the stirring blade 24, for example, stainless steel or the like is preferable. In addition, the stirring power will be described in the reaction condition to be described later.
    [0043] The shape of the agitation blade 24 is not particularly limited and, for example, blades, disc turbines, propellers, helical ribbons, anchors, Pfaudler agitators, fan turbines and others are still mentioned. Reaction Liquid Feed Pipe
    [0044] The material of the reaction liquid feed piping 26 is not particularly limited, as long as it is not corroded by the reaction liquid. Furthermore, as the material of the liquid feed pipe, reaction 26, for example, stainless steel or the like is preferable.
    [0045] The inside diameter of the reaction liquid feed pipe 26 will be described in the section "Reaction Condition" to be described later.
    [0046] The reaction liquid feed pipe 26 is preferably inclined such that the upstream side of the reaction liquid is higher from the point of view of preventing the retention of solid matter or the like of bacterial cells, which produced enzyme in the reaction liquid. Reaction Product Collection Pipe
    [0047] The material of the reaction product collection pipe 27 is not particularly limited, as long as it is not corroded by the aqueous solution containing acrylamide. As the material of the reaction product collection pipe 27, for example, stainless steel or the like is preferable.
    [0048] The inner diameter of the reaction product collection pipe 27 is preferably 5 to 20 cm. When the inner diameter of the reaction product collection pipe 27 is equal to or greater than the lower limit, the collection flow rate of the aqueous solution containing acrylamide can be fixed without requiring a large power for the liquid feed of the reaction liquid. On the other hand, when the inner diameter of the reaction product collection pipe 27 is equal to or less than the upper limit, space saving is also obtained. Liquid Containing Acrylonitrile
    [0049] The liquid containing acrylonitrile is not particularly limited, and commercially available products can be used, or produced products can be used. In order to decrease the amount of biocatalyst consumption at the time of the reaction, a liquid containing acrylonitrile that has a cyano in acrylonitrile concentration of 3 ppm or less is preferable.
    [0050] The concentration of acrylonitrile in the liquid containing acrylonitrile is preferably 90% by mass or more and more preferably 95% by mass or more with respect to the liquid containing acrylonitrile.
    [0051] When the concentration of acrylonitrile in the liquid containing acrylonitrile is adjusted to 90% by mass or more, the amount of impurities in the acrylonitrile is small and the impurities in the aqueous acrylamide solution produced by the hydration of the liquid containing acrylonitrile are also decreased . Thereby, the quality of the aqueous acrylamide solution is improved. Aqueous Biocatalyst Dispersion
    Biocatalysts include animal cells, plant cells, organelles, bacterial cells (living cells or dead cells), or their treated products that contain enzymes to catalyze targeted reactions. Examples of treated products include crude or purified enzymes extracted from cells; and animal cells, plant cells, organelles, bacterial cells (living cells or dead cells), or the enzymes themselves immobilized using a broad method, a cross-linking method, a carrier binding method, or the like.
    [0053] Here, the detailed method is a method of wrapping bacterial cells or enzymes in a fine mesh of a polymer gel or coating bacterial cells or enzymes with semipermeable polymer membranes. In addition, the crosslinking method is an enzyme crosslinking method that uses a reagent that has two or more functional groups (polyfunctional crosslinking agent). In addition, the carrier binding method is a method of binding enzyme to a water-insoluble carrier.
    [0054] Examples of enzyme-producing bacteria include microorganisms belonging to the genus Nocardia, the genus Corynebacterium, the genus Bacillus, the genus Pseudomonas, the genus Micrococcus, the genus Rhodococcus, the genus Acinetobacter, the genus Xantobacter , to the genus Streptomyces, to the genus Rhizobium, to the genus Klebsiella, to the genus Enterobacter, to the genus Erwinia, to the genus Aeromonas, to the genus Citrobacter, to the genus Achromobacter, to the genus Agrobacterium, and to the genus Pseudonocardia.
    [0055] Among them, microorganisms belonging to the genus Rhodococcus are preferable. The types of microorganisms belonging to the genus Rhodococcus are not limited and, for example, the J1 strain of Rhodococcus rhodochrous (accession number: FERM BP-1478; internationally deposited with the International Patent Organism Depositary, National Institute of Advanced Industrial Science and Technology (Chuo 6, Higashi 1-1-1, Tsukuba-shi, Ibaraki, Japan) on September 18, 1987) and others are even more preferable.
    [0056] As microorganisms used in the invention, not only the microorganisms described above, but also those subjected to genetic modification from these microorganisms can be used. There is no limitation on methods or types of genetic modification, as long as a desired compound can be produced.
    Enzymes are not particularly limited as long as they can produce a desired compound and, for example, a nitrile hydratase produced by the microorganisms described above is preferable.
    [0058] The amount of biocatalyst used varies depending on the types or forms of the biocatalyst, but it is preferable that the activity of a biocatalyst to be introduced into a reaction vessel be adjusted to be about 50 to 500 U (units) per 1 mg of bacterial cells dried at a reaction temperature of 10°C. In this document, the term "U (unit)" refers to the activity of the enzyme to produce 1 μmol/1 minute of acrylamide from acrylonitrile, and represents a value measured when using acrylonitrile to be used in production .
    [0059] The concentration of the biocatalyst in the aqueous dispersion of biocatalyst is preferably from 1 to 20% by mass and more preferably from 5 to 15% by mass with respect to the aqueous dispersion of biocatalyst.
    [0060] When the concentration of the biocatalyst in the aqueous dispersion is adjusted to 1% or more, a volume of a storage tank of the aqueous biocatalyst dispersion 32 can be decreased and the compaction capacity of a production apparatus is obtained. On the other hand, when the concentration of the biocatalyst in the aqueous dispersion is adjusted to 20% or less, a viscosity of the aqueous biocatalyst dispersion can be suppressed, and a large amount of energy is not required for the liquid feed. Thereby, energy savings can be obtained.
    [0061] Incidentally, aqueous dispersion indicates an aqueous dispersion obtained by dispersing a biocatalyst in a solvent. As a solvent, water is exemplified. The same material as natural water can be used. Natural water
    [0062] Natural water is used for the hydration reaction with acrylonitrile when acrylamide is produced. Examples of natural water include water or aqueous solutions obtained by dissolving acids or salts in water. Examples of acids include phosphoric acid, acetic acid, citric acid and boric acid. Examples of the salts include sodium salts, potassium salts and ammonium salts of the acids described above. Specific examples of natural water include, but are not particularly limited to, water such as plain water, city water, and tap water; and buffer solutions such as a Tris buffer solution, a phosphate buffer solution, an acetate buffer solution, a citrate buffer solution, and a borate buffer solution. The pH (at 25°C) of natural water is preferably from 5 to 9.
    [0063] The ratio between the liquid containing acrylonitrile and the natural water that are fed to the reaction tank is expressed as [volume of liquid containing acrylonitrile]/[volume of natural water] and is preferably from 0.4 to 1, two.
    [0064] When a value of [volume of liquid containing acrylonitri-la]/[volume of natural water] is set to 0.4 or more, the concentration of the aqueous solution of acrylamide produced by hydrating acrylonitrile can be easily set to 30 % or more. On the other hand, when a value of [volume of liquid containing acrylonitrile]/[volume of natural water] is set to 1.2 or less, the concentration of the aqueous solution of acrylamide produced by hydration of acrylonitrile can be easily suppressed until 65% or less.
    [0065] A ratio of the liquid containing acrylonitrile and the aqueous dispersion of biocatalyst that are fed to the reaction tank is expressed as [volume of liquid containing acrylonitrile]/[volume of the aqueous dispersion of biocatalyst] and is preferably from 50 to 800 .
    [0066] When a value of [volume of liquid containing acrylonitri-la]/[volume of aqueous dispersion of biocatalyst] is set to 50 or more, the used amount of the biocatalyst can be suppressed and deterioration of the quality of the aqueous solution of acrylamide caused by incorporating a large amount of biocatalyst-derived impurities into the aqueous acrylamide solution can be prevented. On the other hand, when a value of [volume of liquid containing acrylonitrile]/[volume of aqueous dispersion of biocatalyst] is set to 800 or less, the amount of biocatalyst used is decreased and the concentration of unreacted acrylonitrile in the aqueous solution of acrylamide can be suppressed to less than 200 ppm. Reaction Condition
    [0067] The method for producing acrylamide of this modality is carried out in a state where the Reynolds number of the reaction liquid flowing in the reaction liquid feed pipe 26 is within a predetermined range. Furthermore, the temperature of the reaction liquid in the reaction tank 10 and the stirring power are adjusted accordingly. Reynolds Number
    [0068] In this mode, the Reynolds number of the reaction liquid flowing in the reaction liquid feed pipe 26 is 1,800 to 22,000. The Reynolds number is preferably from 2,000 to 20,000, more preferably from 3,000 to 15,000, and most preferably from 5,000 to 10,000.
    [0069] When the Reynolds number is equal to or greater than the lower limit, the efficiency of acrylamide production can be improved. In addition, since the prevention of retention of the reaction mixture in the reaction liquid feed pipe 26, the suppression of acrylamide coloration, and the prevention of polymerization of acrylamide, which is easily polymerized, are obtained, the quality of acrylamide produced can be increased. On the other hand, when the Reynolds number is equal to or less than the upper limit, the liquid surface difference of the reaction liquid between the upstream reaction tank 10 and the downstream reaction tank 10 is also decreased, and the volume of reaction liquid in reaction tank 10 is also increased. In this way, space saving of continuous tank reactor 1 and improvement in reaction efficiency are obtained.
    [0070] The Reynolds number (Re) is obtained by the following equation. Re = V x d x p/μ
    [0071] Re: Reynolds Number
    [0072] V: Flow velocity (m/s) of the reaction liquid in the reaction liquid supply pipe 26
    [0073] d: Inner diameter (m) of the reaction liquid feed pipe 26
    [0074] p: Density (kg/m3) of the reaction liquid
    [0075] μ: Viscosity (Pa.s) of the reaction liquid
    [0076] Here, the density of the reaction liquid and the viscosity of the reaction liquid may vary depending on the temperature or the like of the reaction liquid, but once the ideal temperature of the biocatalyst is maintained, it is difficult to change much the temperature of the reaction liquid so that it is difficult to artificially change the density of the reaction liquid and the viscosity of the reaction liquid. Therefore, in this mode, the Reynolds number of the reaction liquid flowing in the reaction liquid feed pipe 26 is mainly adjusted by the flow velocity of the reaction liquid in the reaction liquid feed pipe 26 and the inner diameter of the pipe. feeding the reaction liquid 26.
    [0077] Incidentally, generally speaking, the density of the reaction liquid is preferably 1.0 to 1.2 kg/m3, and the viscosity of the reaction liquid is preferably 1.5 to 5 Pa.s.
    [0078] In this descriptive report, for density measurement, measurement methods using a pycnometer, measurement using a liquid weighing method, measurement using a hydrometer, measurement using an oscillating densitometer , and measurement using a magnetic levitation densitometer can be used. Viscosity can be measured by methods such as a capillary tube viscometer method and a rotary viscometer method. Reaction liquid flow velocity in the reaction liquid feed pipe 26:
    [0079] For the adjustment of the flow velocity of the reaction liquid in the reaction liquid supply piping 26, a liquid supply pump or a flow adjustment valve may be used or may not be used. When the liquid feed pump is used, pressure energy is generated in the reaction liquid and thereby the flow velocity of the reaction liquid in the reaction liquid feed pipe 26 can be increased. However, from the point of view of energy saving, space saving, cost reduction and simplification of an apparatus, it is preferable that the flow speed be adjusted without using the liquid feed pump.
    [0080] The flow velocity of the reaction liquid is preferably from 0.1 to 1.5 m/s and more preferably from 0.5 to 1.1 m/s.
    [0081] In addition, the flow rate can be measured by using a differential pressure flow meter, an electromagnetic flow meter, an area flow meter, an ultrasonic flow meter, an impeller flow meter, a flow meter. thermal flow, a Coriolis flowmeter, a volumetric flowmeter, a vortex flowmeter, a turbine flowmeter, a Pitot tube flowmeter, and the like. The flow velocity of the reaction liquid can be obtained by dividing the measured flow by a cross-sectional area of the reaction liquid supply piping 26.
    [0082] In a case where the liquid feed pump is not used, the flow of reaction liquid from the upstream reaction tank to the downstream reaction tank is generated by using potential energy. Specifically, when the liquid surface of the upstream reaction tank is held to be higher than the liquid surface of the downstream reaction tank, the reaction liquid flow in the reaction liquid feed pipe 26 towards the downstream is generated (see the dotted line in Figure 1 and the liquid surface of each reaction tank 10).
    [0083] The flow velocity of the reaction liquid in the reaction liquid feed pipe 26 is further increased as the liquid surface difference is further increased, and the flow velocity thereof is further decreased as the that the surface difference of the liquid is further diminished. The difference in the liquid surface is appropriately controlled by adjusting the feed flow of the liquid containing acrylonitrile to the reaction tank 11, the feed flow of the aqueous biocatalyst dispersion, the natural water feed flow, or the inner diameter of the pipe feeding the reaction liquid.
    [0084] In a case where reaction tanks that have the same shape and the same internal capacity are used, when the downstream reaction tank is arranged in the lower position than that of the upstream reaction tank, the volume of the reaction in reaction tank 10 can be increased further. In this way, more space savings and improvement in reaction efficiency are obtained.
    [0085] In this mode, from the point of view of obtaining more space saving, it is preferable that the liquid surface difference is further decreased and the reaction volume in the reaction tank 10 is further increased.
    [0086] Specifically, the liquid surface difference between two reaction tanks directly connected to each other is preferably 0.05 to 10 cm, more preferably 0.08 to 5 cm, and even more preferably 0 , 1 to 3 cm.
    [0087] In addition, the liquid surface difference between the most upstream reaction tank and the most downstream reaction tank is preferably from 0.1 to 80 cm, more preferably from 0.3 to 50 cm , and even more preferably from 0.5 to 20 cm.
    [0088] When the liquid surface difference is equal to or greater than the lower limit, the reaction liquid can be fed from the reaction tank 10 upstream to the reaction tank 10 downstream by the potential energy. Furthermore, since the flow velocity of the reaction liquid in the reaction liquid feed pipe 26 is increased and a sufficient Reynolds number can be obtained, the retention of the reaction liquid in the reaction liquid feed pipe 26 can be suppressed. On the other hand, when the liquid surface difference is equal to or less than the upper limit, since the flow velocity is not increased too much and the Reynolds number is not increased too much, a sufficient volume of the reaction can be assured. Internal Diameter of Reaction Liquid Feed Pipe 26:
    [0089] The reaction liquid feed pipe 26 is preferably cylindrical in shape, and the inner diameter of the reaction liquid feed pipe 26 is preferably from 2 to 80 m, more preferably from 3 to 50 m, and even more preferably from 5 to 30 m. When the inside diameter of the reaction liquid feed pipe 26 is equal to or greater than the lower limit, a desired Reynolds number can be obtained without using the pressure energy generated by the liquid feed pump and the surface difference of the liquid can also be decreased. On the other hand, when the inner diameter of the reaction liquid feed pipe 26 is equal to or less than the upper limit, the reaction volume in the reaction tank 10 can be increased even more, and thus space and improvements in reaction efficiency are also obtained.
    [0090] Incidentally, in a case where the reaction liquid feed pipe 26 does not have a cylindrical shape, an equivalent diameter can be used as the inside diameter. The equivalent diameter can be calculated using the following calculation formula.De = 4Af/Wp [m]
    [0091] From: Equivalent diameter [m]
    [0092] Af: Cross-sectional area of the passage [m2]
    [0093] Wp: Length of the wet perimeter [m]
    [0094] The internal diameter of the reaction liquid feed pipe 26 with respect to the internal volume of the reaction tank 10 is preferably from 3 to 30 cm/m3 and more preferably from 5 to 15 cm/m3. When the inner diameter of the reaction liquid feed pipe 26 with respect to the inner volume of the reaction tank 10 is equal to or greater than the lower limit, a desired Reynolds number can be obtained without using the pressure energy generated by the pump liquid feed and the liquid surface difference can also be decreased. On the other hand, when the inner diameter of the reaction liquid feed pipe 26 is equal to or less than the upper limit, space saving is also obtained. Reaction Liquid Temperature
    [0095] The temperature of the reaction liquid is preferably from 15 to 40°C and more preferably from 20 to 35°C. When the reaction liquid temperature is equal to or greater than the lower limit, it is easy to sufficiently increase the biocatalyst reaction activity. On the other hand, when the temperature of the reaction liquid is equal to or less than the upper limit, inactivation of the biocatalyst is prevented. Agitation Power
    [0096] The stirring power of the reaction liquid per unit volume by stirring paddle 24 is preferably from 0.08 to 0.7 kW/m3, more preferably from 0.09 to 0.6 kW/m3, and even more preferably from 0.1 to 0.4 kW/m3.
    [0097] When the stirring power is equal to or greater than the lower limit, the contact or dispersivity between the acrylonitrile and the biocatalyst is improved and the efficiency of converting acrylonitrile to acrylamide is increased. Furthermore, a reduction in heat transfer performance in reaction tank 10 can be suppressed, the temperature controllability of the reaction liquid is improved, and the energy consumption of a chiller is decreased. On the other hand, when the stirring power is equal to or less than the upper limit, deterioration of the biocatalyst is suppressed, and the reaction efficiency of acrylonitrile in acrylamide catalyst is increased. Another Modality of the Method for the Production of a Compound Compound Production System
    [0098] In the following, as another embodiment of the method for producing a compound of the invention, a system for producing a compound 2 will be described by means of Figure 2.
    [0099] The production system 2 illustrated in Figure 2 is provided with an alkaline solution storage tank 31, an aqueous biocatalyst dispersion storage tank 32, a portable container 33, an alkaline solution feed pipe 34, a catalyst feed piping 35, an acrylonitrile feed piping 36, a natural water feed piping 37, and an engine 38, in addition to continuous tank reactor 1 configurations.
    [00100] Incidentally, the same configurations in the production system 2 as the configurations in the continuous tank reactor 1 are the same as in the above-mentioned method embodiment for the production of acrylamide, and its description is thereby omitted. Also, in Figure 2, the same symbols as in Figure 1 are applied to the same configurations as the configurations illustrated in Figure 1.
    [00101] Next, the alkaline solution storage tank 31, the aqueous biocatalyst dispersion storage tank 32 and the portable container 33 in Figure 2 will be described in detail. Alkaline Solution Storage Tank
    [00102] The alkaline solution storage tank 31 is a tank that stores an alkaline solution used to control the pH of the reaction liquid in the reaction tank 10. In the embodiment of Figure 2, the alkaline solution to be stored in the storage tank of alkaline solution 31 is fed to two reaction tanks 11 through the alkaline solution feed line 34.
    [00103] The material of the alkaline solution storage tank 31 is not particularly limited, as long as it is not corroded by the alkaline solution. The material of the alkaline solution storage tank 31 is preferably, for example, stainless steel or the like.
    [00104] The volume of the alkaline solution storage tank 31 is appropriately adjusted according to the speed of the process, but is preferably such a volume as to allow each tank or two or more tanks to be accommodated in the portable container 33. Biocatalyst Aqueous Dispersion Storage Tank
    [00105] The aqueous biocatalyst dispersion storage tank 32 is a tank that stores the aqueous biocatalyst dispersion. When acrylamide is produced, the aqueous biocatalyst dispersion to be stored in the aqueous biocatalyst dispersion storage tank 32 is fed to some of the reaction tanks 10 through catalyst feed piping 35. In the embodiment of Figure 2, the dispersion Aqueous biocatalyst is only fed into the 10 most upstream reaction tank.
    [00106] The biocatalyst 32 aqueous dispersion storage tank material is not particularly limited, as long as it is not corroded by the biocatalyst. For example, stainless steel or the like can be used as the storage tank material for the aqueous dispersion of biocatalyst 32.
    [00107] The volume of the storage tank of the aqueous biocatalyst dispersion 32 is appropriately adjusted according to the speed of the process, but is preferably such a volume as to allow each tank or two or more tanks to be accommodated in the portable container 33. Portable Container
    [00108] The portable container 33 is used to accommodate and transport the reaction tank 10, the alkaline solution storage tank 31 and the aqueous biocatalyst dispersion storage tank 32. The portable container 33 is used, such as necessary, to accommodate and transport an acrylamide purification apparatus.
    [00109] The portable container 33 can accommodate any one or more tanks among the reaction tank 10, the alkaline solution storage tank 31 and the aqueous biocatalyst dispersion storage tank 32. It is preferable that the portable container 33 accommodates by the minus one tank from the 10 reaction tanks.
    [00110] In addition, the volume of the reaction tank 10 to be accommodated in each portable container is preferably from 6.4 m3 to 22.9 m3, more preferably from 7.7 to 19.2 m3, and still with more preferably from 11.5 to 15.3 m3. When the volume of the reaction tank to be accommodated in the portable vessel is set to 6.4 m3 or more, the production efficiency with respect to space can be further improved. When the volume of the reaction tank to be accommodated in the portable vessel is set to 22.9 m3 or less, the effects of improving operability in the portable vessel and maintenance properties are obtained.
    [00111] In a case in which the reaction tanks 10 are accommodated in a plurality of portable containers, the volume of the reaction tank 10 refers to the volume of the reaction tank 10 in each portable container.
    [00112] Furthermore, in the system for producing a compost 2 of this modality, only one portable container 33 can be provided or else two or more portable containers 33 can be provided. In a case where two or more portable containers 33 are provided, the portable containers 33 can be arranged horizontally and used or can be stacked and used when acrylamide is produced.
    [00113] From the point of view of energy saving, it is preferable that the liquid containing acrylonitrile, the aqueous dispersion of biocatalyst, the reaction liquid and the like are fed using potential energy without using the liquid feed pump. From a space saving point of view, it is preferable that the portable containers 33 are stacked and used as illustrated in Figure 2. Furthermore, when the motor 38 which rotates the agitation paddle 24 is disposed in the portable container stack 33 on the side higher, compared to a case in which the engine 38 is arranged directly on the reaction tank 10, the volume of the reaction tank 10 is easily increased and maintenance is easily carried out.
    [00114] The size of the portable container 33 is not particularly limited, as long as it is a size in which some of the above mentioned tanks can be accommodated and transport can be carried out, but a standard portable container that can be transported by trailers, trains. cargo, ships, and the like is preferable. For example, a portable container standardized in accordance with ISO 668 or similar is mentioned. With regard to specific size, a portable container that has a size of about 2.4 m (width) x about 2.9 m (height) x about 13 m (depth), and others is still exemplified, and as specific standardized examples, a 20-foot container, a 40-foot container, a 45-foot container, and still others are mentioned.
    [00115] The volume of the reaction tank in each portable vessel 33 (the total volume of the plurality of reaction tanks in a case in which a plurality of reaction tanks is accommodated in each portable vessel) is preferably from 1/6 to 3 /5 of the internal volume of each portable container 33, and more preferably 1/4 to 1/2 the internal volume of each portable container 33. When the volume of the reaction tank in each portable container 33 is equal to or greater than the lower limit, the production efficiency with respect to space is further improved. On the other hand, when the volume of the reaction tank in each portable vessel 33 is equal to or less than the upper limit, the operation space can be sufficiently ensured.
    [00116] In the production of acrylamide, the value obtained by dividing the internal volume (m3) of the portable container by the flow (m3/h) of the reaction liquid flowing in the reaction tank accommodated in the portable container is preferably from 5 to 70 hours and more preferably from 15 to 65 hours. When the value is equal to or greater than the lower limit, a more sufficient concentration of the aqueous solution containing acrylamide is obtained, and the concentration of unreacted acrylonitrile in the aqueous solution containing acrylamide obtained is further lowered. Thereby, the quality of the aqueous solution containing acrylamide is further improved. On the other hand, when the value is equal to or less than the upper limit, the production efficiency with respect to space is further improved. Incidentally, the flow measurement method is as described above. Compound to be Produced
    [00117] The method for producing a compound of the invention is characterized by the fact that when the Reynolds number of the reaction liquid flowing in the reaction liquid feed pipe is set to be within a predetermined range, the economy of space is obtained without a decrease in production efficiency. Therefore, a compound to be produced by the method for producing a compound of the invention is not limited to the aforementioned acrylamide, and may be another compound that is known to be industrially produced.
    [00118] The compound to which the method for producing a compound of the invention is applied is not particularly limited, as long as it is a compound to be produced by chemical reaction, but a compound to be produced by chemical reaction in the presence of the biocatalyst.
    [00119] Specific examples of a compound to be produced include amide compounds that have an amide group in the molecule, and specifically, acryl compounds such as acrylamide, nicotinamide, 5-cyanovaleramide and methacrylamide are exemplified, and in in particular acrylamide is preferable.
    Examples of raw materials that produce these compounds include acrylonitrile, 3-cyanopyridine, 1,4-dicyanobutane, and methacrylonitrile. In particular, acrylonitrile is preferable. Effect of the Invention
    [00121] Above, according to the invention, it is possible to provide a method for producing a compound by using continuous reaction in which space savings are obtained without a decrease in production efficiency. Furthermore, a production system of the invention can be run in a place where there is a demand as to the use of the production system and can start industrial production of a compost in a short time.
    [00122] Since the reaction tank used in the method for producing a compound of the invention entails a space saving, that is, it is reduced in size, the reaction tank can also be accommodated in the portable container. Then, the portable container can be transported by trailers, freight trains, ships, and so on while the reaction tank is accommodated. For such reasons, the production system of a compound of the invention can be opportunely brought into a place where there is a demand to use the used and compounded production system, and in a case where there is no demand to use the production system. Compost, the composite production system can be run at a next place where there is a demand as to the use of a compost production system.
    [00123] Furthermore, the system of producing a compost is only completed by properly disposing the portable container when the reaction tank is accommodated in the portable container, and by installing the pipelines between containers. For this reason, when industrial production of a compound is started, since there is no fundamental construction need in the continuous tank reactor installation, the construction period can be shortened and the construction costs are suppressed.
    [00124] In the production system of a compound of the invention, when the portable containers that accommodate the reaction tanks are stacked and used, space savings are also obtained.
    [00125] When the portable container that accommodates the tank positioned on the most upstream side in the reaction process is stacked on another upper side, the reaction liquid can be fed using potential energy without using the liquid feed pump, and in this way energy savings are also obtained.
    [00126] A member skilled in the art who performs the method for the production of a compound and does not have a reaction tank can recently arrange the continuous tank reactor or the production system used in the method for the production of a compound in the invention without requiring construction costs and a construction period, and thereby can perform the method for producing a compound of the invention. In addition, an element versed in the state of the art that already has the continuous tank reactor can appropriately expand or replace a reaction tank or a reaction liquid feed pipe, and thus can perform the method for producing a compound of the invention. EXAMPLES
    [00127] In the following, the invention will be described in more detail by way of examples; however, the invention is not limited to these examples. Example 1 Biocatalyst Preparation
    [00128] The J1 strain of Rhodococcus rhodochrous which has nitrile hydratase activity (accession number: FERM BP-1478; internationally deposited with the International Patent Organism, National Institute of Advanced Industrial Science and Technology (Chuo 6, Higashi 1-1) -1, Tsukuba-shi, Ibaraki, Japan) on September 18, 1987) was cultivated aerobically in a medium (pH 7.0) containing 2% by mass glucose, 1% by mass urea, 0.5% by mass of peptone, 0.3% by mass of yeast extract, and 0.01% by mass of cobalt chloride hexahydrate at 30°C.
    [00129] After cultivation, the culture obtained was subjected to harvest using a centrifuge. Then, the bacterial cells were suspended in 0.1% by mass of an aqueous solution of sodium acrylate (pH 7.0) and the harvesting and washing operation was performed five times using a centrifuge again. Then, the bacterial cells were suspended in 0.1% by mass of an aqueous solution of sodium acrylate (pH 7.0), thereby preparing a bacterial cell suspension containing 15% by mass of dry bacterial cells. . The bacterial cell suspension was transferred to the storage tank of the aqueous biocatalyst dispersion in the portable container which has a size of 2.5 m (width) x 2.5 m (height) x 6 m (depth) and was cooled down to 5°C until the next reaction, and the bacterial cell suspension was then used as an aqueous biocatalyst dispersion for the next reaction. Reaction of Acrylonitrile in Acrylamide
    [00130] The reaction was performed using a production system illustrated in Figure 2.
    [00131] Specifically, SUS reaction tanks that have an internal volume of 2 m3 (1.3 m (width) x 1.3 m (depth) x 1.3 m (height)) were connected in series through a pipeline of the reaction liquid feed which has an inner diameter of 5 cm and a length of 1 m, and the reaction was carried out using a continuous tank reactor in which a stirring paddle (blade type, blade diameter: 45 cm ) was provided in each reaction tank. Four reaction tank tanks were accommodated in each of two portable containers which have a size of 2.5 m (width) x 2.5 m (height) x 6 m (depth) with the exception of the portable container that accommodates the tank of storage of the aforementioned aqueous biocatalyst dispersion, and the eight tanks were then connected in series. The proportion of reaction tanks (four tanks) in a vessel was adjusted to 23%. The reaction tanks were designated as a first tank, a second tank, a third tank, a fourth tank, a fifth tank, a sixth tank, a seventh tank, and an eighth tank (hereinafter, the eighth tank is indicated as " downstream reaction tank") on the upstream side of the reaction liquid.
    [00132] The first tank was provided with the acrylonitrile feed piping, the natural water feed piping, the catalyst feed piping and the alkaline solution feed piping. The second tank was provided with the acrylonitrile feed piping and the alkaline solution feed piping. The third tank and the fourth tank were provided with only the acrylonitrile feed piping. The further downstream reaction tank was provided with the overflow reaction product type collection piping.
    [00133] In this example, the aqueous biocatalyst dispersion cooled in the storage tank of the aqueous biocatalyst dispersion in the portable container was fed to the first tank through the catalyst feed piping.
    [00134] In this example, the alkaline solution storage tank was also accommodated in the portable container that accommodates the storage tank of the aqueous biocatalyst dispersion. Then, the alkaline solution stored in the alkaline solution storage tank was fed to the first tank and the second tank through the alkaline solution feed piping.
    [00135] In addition, the aqueous acrylonitrile solution stored in the acrylonitrile storage tank disposed outside the portable container was fed from the first tank to the fourth tank through the acrylonitrile feed pipe.
    [00136] In addition, the natural water stored in the natural water storage tank arranged outside the portable container was fed to the first tank through the natural water supply pipe.
    [00137] In this example, 1.8 m3 of 50% by mass of the aqueous solution of acrylamide was introduced into the first tank to the seventh tank beforehand before starting the reaction.
    [00138] The reaction was started by feeding the aqueous solution of acrylonitrile (concentration: 99.6% by mass, manufactured by MITSUBISHI RAYON CO., LTD.), the natural water, and the aqueous dispersion of biocatalyst to the tanks of reaction from the first tank to the fourth tank at the total feed rate (the aqueous solution of acrylonitrile: the natural water: the aqueous dispersion of biocatalyst) of 1.00:1.32:0.01. In this example, the total flow rates of the aqueous acrylonitrile solution, natural water, and the aqueous biocatalyst dispersion were designated as a raw material feed amount. The raw material feed rate was adjusted in such a way that the Reynolds number in each reaction liquid feed pipe step from 2,000 to 2,500.
    [00139] The value obtained by dividing the internal volume (m3) of the portable container by the flow (m3/h) of the reaction liquid flowing in the reaction tank accommodated in the portable container was adjusted in about 50 hours.
    [00140] During the reaction, 2% by mass of an aqueous solution of sodium hydroxide was added to the alkaline solution storage tank in such a way that the pH of the reaction mixture in the first to fourth reaction tanks was adjusted to 7, 0. The feeding of the liquid at the time of feeding the aqueous dispersion of biocatalyst and 2% by mass of an aqueous solution of sodium hydroxide was carried out without using the liquid feeding pump by the potential energy obtained when stacking the portable container that accommodates the storage tank for the aqueous dispersion of biocatalyst and the storage tank for the alkaline solution in the portable container that accommodates the first tank to the fourth tank. Furthermore, the operation was carried out in such a way that the height of the liquid surface of the reaction liquid in the first tank occupied about 90% of the internal volume.
    [00141] The reaction was carried out under conditions which include a reaction liquid temperature of 25°C and a stirring power of 0.2 kW/m3.
    [00142] During the reaction, the liquid surface difference between the reaction tanks of the first tank and the second tank was 5 mm or less.
    [00143] In addition, the flow rate of the aqueous acrylamide solution flowing out of the overflow type reaction product collection piping during one hour from the start of the reaction under this condition was 99% or more of the amount of feed of raw material.
    [00144] The concentration of acrylamide in the aqueous solution containing acrylamide flowing out of the reaction product collection pipe was measured using a digital refractometer (manufactured by ATAGO CO., LTD.). In addition, the concentration of unreacted acrylonitrile in the aqueous solution containing acrylamide was measured using gas chromatography (column: manufactured by Waters, PoraPack-PS, 1 m, 180°C, carrier gas: helium, detector: FID).
    [00145] From the point of view of acrylamide quality, it is desirable that the concentration of acrylamide in the aqueous solution containing acrylamide that flows out of the reaction product collection pipe is 50% by mass or more and that the concentration of unreacted acrylonitrile is less than 100 ppm.
    [00146] In this example, the concentration of acrylamide in the aqueous solution containing acrylamide flowing out of the reaction product collection pipe was 50.5% by mass, the concentration of acrylonitrile was 10 ppm or less, and it was possible perform a stable operation for three weeks or more from the start of the reaction. Example 2
    [00147] An aqueous solution containing acrylamide was collected in the same manner as in Example 1, except that the raw material feed rate was adjusted in such a way that the Reynolds number of the reaction liquid flowing in each pipeline feeding the reaction liquid at 5,000 to 5,500, and then its concentration was measured.
    [00148] The value obtained by dividing the internal volume (m3) of the portable container by the flow (m3/h) of the reaction liquid flowing in the reaction tank accommodated in the portable container was adjusted in about 20 hours.
    [00149] Incidentally, during the reaction, the difference in liquid surface between the reaction tanks of the first tank and the second tank was 10 to 20 mm.
    [00150] In addition, the flow rate of the aqueous acrylamide solution flowing out of the excess flow type reaction product collection piping during one hour from the start of the reaction under this condition was 95% or more of the amount of feed of raw material.
    [00151] In this example, the acrylamide concentration in the aqueous solution containing acrylamide flowing out of the reaction product collection pipe was 50.4% by mass, the acrylonitrile concentration was 10 ppm or less, and it was possible perform a stable operation for three weeks or more from the start of the reaction. Example 3
    [00152] An aqueous solution containing acrylamide was collected in the same manner as in Example 1, except that the feed rate of raw material was adjusted in such a way that the Reynolds number of the reaction liquid flowing in each pipeline. feeding the reaction liquid at 10,000 to 11,000, and then its concentration was measured.
    [00153] The value obtained by dividing the internal volume (m3) of the portable container by the flow (m3/h) of the reaction liquid flowing in the reaction tank accommodated in the portable container was adjusted in about 10 hours.
    [00154] Incidentally, during the reaction, the difference in liquid surface between the reaction tanks of the first tank and the second tank was 30 to 45 mm.
    [00155] In addition, the flow rate of the aqueous acrylamide solution flowing out of the overflow type reaction product collection piping during one hour from the start of the reaction under this condition was 93% or more of the amount of feed of raw material.
    [00156] In this example, the acrylamide concentration in the aqueous solution containing acrylamide flowing out of the reaction product collection pipe was 50.3% by mass, the acrylonitrile concentration was 25 ppm, and it was possible to perform a stable operation for three weeks or more from the onset of the reaction. Example 4
    [00157] An aqueous solution containing acrylamide was collected in the same manner as in Example 1, except that the feed rate of raw material was adjusted in such a way that the Reynolds number of the reaction liquid flowing in each pipeline. feeding the reaction liquid at 18,000 to 20,000, and then its concentration was measured.
    [00158] The value obtained by dividing the internal volume (m3) of the portable container by the flow (m3/h) of the reaction liquid flowing in the reaction tank accommodated in the portable container was adjusted in about 5 hours.
    [00159] Incidentally, during the reaction, the difference in liquid surface between the reaction tanks of the first tank and the second tank was 90 to 100 mm.
    [00160] In addition, the flow rate of the aqueous acrylamide solution flowing out of the overflow type reaction product collection piping during one hour from the start of the reaction under this condition was 90% or more of the amount of feed of raw material.
    [00161] In this example, the acrylamide concentration in the aqueous solution containing acrylamide flowing out of the reaction product collection pipe was 50.1% by mass, the acrylonitrile concentration was 50 ppm, and it was possible to perform a stable operation for three weeks or more from the onset of the reaction. Comparative Example 1
    [00162] An aqueous solution containing acrylamide was collected in the same manner as in Example 1, except that the feed rate of raw material was adjusted in such a way that the Reynolds number of the reaction liquid flowing in each pipeline feeding the reaction liquid at 1,000 to 1,500, and then its concentration was measured.
    [00163] The value obtained by dividing the internal volume (m3) of the portable container by the flow (m3/h) of the reaction liquid flowing in the reaction tank accommodated in the portable container was adjusted in about 100 hours.
    [00164] Incidentally, during the reaction, the difference in liquid surface between the reaction tanks of the first tank and the second tank was 10 mm or less.
    [00165] In addition, the flow rate of the aqueous acrylamide solution flowing out of the overflow type reaction product collection piping during one hour from the start of the reaction under this condition was 99% or more of the amount of feed of raw material.
    [00166] In this example, the concentration of acrylamide in the aqueous solution containing acrylamide flowing out of the reaction product collection pipe was 50.5% by mass, and the concentration of acrylonitrile was 10 ppm or less. However, 3 days after the start of the reaction, the sedimentation of the biocatalyst occurred in the reaction liquid feeding pipe. In addition, the aqueous acrylamide solution flowing out of the reaction product collection pipe was colored pale yellow, and a small amount of a popcorn-type acrylamide polymer was mixed. Comparative Example 2
    [00167] An aqueous solution containing acrylamide was collected in the same manner as in Example 1, except that the feed rate of raw material was adjusted in such a way that the Reynolds number of the reaction liquid flowing in each pipeline. feed the reaction liquid at 23,000 to 25,000, and then its concentration was measured.
    [00168] The value obtained by dividing the internal volume (m3) of the portable container by the flow (m3/h) of the reaction liquid flowing in the reaction tank accommodated in the portable container was adjusted in about 4 hours.
    [00169] Incidentally, during the reaction, the liquid surface difference between the reaction tanks of the first tank and the second tank was 200 mm or more.
    [00170] In addition, the flow rate of the aqueous acrylamide solution flowing out of the overflow type reaction product collection piping during one hour from the start of the reaction under this condition was 70% or less of the amount of feed of raw material. In addition, the reaction liquid in the first tank reached 98% or more of the internal volume of the reaction tank.
    [00171] In addition, the acrylamide concentration in the aqueous solution containing acrylamide flowing out of the reaction product collection pipe was 49.5% by mass, and the acrylonitrile concentration was 2,000 ppm or most.
    [00172] In this comparative example, the acrylamide concentration and the acrylonitrile concentration in the aqueous acrylamide solution flowing out of the reaction product collection pipe were not in the range that was desirable in terms of quality, and there was an interest that the reaction liquid from the reaction tank of the first tank could overflow. For these reasons, the operation was stopped one hour after the start of the reaction. INDUSTRIAL APPLICABILITY
    [00173] According to the invention, it is possible to provide a method for producing a compound by using continuous reaction in which space savings are obtained without a decrease in production efficiency. Furthermore, a production system of the invention can be carried out in a place where there is a demand for the use of the production system and can start industrial production of a compost in a short time.EXPLANATIONS OF LETTERS OR NUMBERS1. Continuous tank reactor;2. Production system;10 to 13. Reaction tank;21. 36. Acrylonitrile feed piping;22. 35. Catalyst feed piping;23. 37. Natural water supply piping;24. Stirring paddle;25. Acid/alkali solution feed piping;26. Reaction liquid feeding pipe;27. Reaction product collection pipe;28. Acrylonitrile Feed Port; 29. Biocatalyst feed port;31. Alkaline solution storage tank;32. Biocatalyst aqueous dispersion storage tank;33. Portable container;34. Alkaline solution feed piping; e38. Motor
    权利要求:
    Claims (9)
    [0001]
    1. Method for producing acrylamide in a continuous tank reactor, characterized in that it comprises: flowing a reaction liquid from an upstream reaction tank to a downstream reaction tank through a reaction liquid feed tube in a Reynolds number from 1,800 to 22,000, where the continuous tank reactor comprises two or more reaction tanks and the reaction liquid feed tube, which connects the reaction tank to the adjacent reaction tank, and the height of a liquid surface of the downstream reaction tank is smaller than the liquid surface of the upstream reaction tank.
    [0002]
    2. Method according to claim 1, characterized in that at least one tank of the reaction tanks is accommodated in a portable container, and a value obtained by dividing an internal volume (m3) of the portable container by a flow (m3 /h) of the reaction liquid flowing at least in the reaction tank accommodated in the portable container is 5 to 70 hours.
    [0003]
    3. Method according to claim 1, characterized in that it further comprises: feeding a liquid containing acrylonitrile to at least one tank of reaction tanks; feeding natural water to at least one tank of reaction tanks; and the feeding of an aqueous dispersion of biocatalyst to at least one tank of the reaction tanks.
    [0004]
    4. Method according to claim 1, characterized in that it further comprises: feeding a liquid containing acrylonitrile, raw water and an aqueous dispersion of biocatalyst to at least one tank positioned on the most upstream side of the reaction liquid.
    [0005]
    5. Method according to claim 1, characterized in that at least one tank of the reaction tanks is accommodated in a portable container and in that the total volume of the at least one tank accommodated in the portable container is 1/6 to 3/5 of an internal volume of the portable container.
    [0006]
    6. Method according to claim 1, characterized in that at least one tank of reaction tanks is accommodated in a portable container and in that another portable container is disposed in the portable container in which the at least one tank of tanks of reaction is accommodated.
    [0007]
    7. Method according to claim 1, characterized in that at least one tank of the reaction tanks is accommodated in a portable container and in that a volume of the at least one reaction tank accommodated in the portable container is 6, 4 m3 to 22.9 m3.
    [0008]
    8. Method according to claim 1, characterized in that the difference in height of the liquid surface between the reaction tank and the adjacent reaction tank is 0.05 to 10 cm.
    [0009]
    9. Method according to claim 1, characterized in that the difference in height of the liquid surface between the reaction tank and the adjacent reaction tank is 0.1 to 3 cm.
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    法律状态:
    2018-05-22| B25D| Requested change of name of applicant approved|Owner name: MITSUBISHI CHEMICAL ENGINEERING CORPORATION (JP) , |
    2019-12-24| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|
    2020-08-04| B25A| Requested transfer of rights approved|Owner name: MITSUBISHI CHEMICAL CORPORATION (JP) |
    2021-06-08| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2021-08-10| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 03/07/2015, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    JP2014142688|2014-07-10|
    JP2014-142688|2014-07-10|
    PCT/JP2015/069307|WO2016006556A1|2014-07-10|2015-07-03|Method for producing compound and compound production system used in said production method|
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