CN112892438A - System and method for synthesizing rubber scorch retarder CTP through continuous flow micro-reaction - Google Patents
System and method for synthesizing rubber scorch retarder CTP through continuous flow micro-reaction Download PDFInfo
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Abstract
本发明属于精细化工技术领域，尤其涉及一种连续流微反应合成橡胶防焦剂CTP的系统和方法。本发明提供的系统包括：环己基次磺酰氯和催化剂混合液输送管道；酞酰亚胺钠盐和催化剂混合液输送管道；分别与环己基次磺酰氯和催化剂混合液输送管道的出料口以及酞酰亚胺钠盐和催化剂混合液输送管道的出料口相连接的微反应装置；所述微反应装置为管式反应器。本发明提供的系统通过利用液、液两相流在微反应装置充分接触反应合成橡胶防焦剂CTP，实现了CTP合成的不间断反应，大大提高了合成CTP的生产效率和反应收率，同时提升了产品的纯度和质量稳定性，具有较好的应用前景，并能产生可观的经济效益和社会效益。
The invention belongs to the technical field of fine chemicals, and in particular relates to a system and method for a continuous flow micro-reaction synthetic rubber scorch retarder CTP. The system provided by the invention comprises: a pipeline for conveying cyclohexylsulfenyl chloride and a mixed solution of catalyst; The micro-reaction device is connected with the discharge port of the phthalimide sodium salt and the catalyst mixed solution conveying pipeline; the micro-reaction device is a tubular reactor. The system provided by the invention realizes the uninterrupted reaction of CTP synthesis by fully contacting and reacting synthetic rubber anti-scorch agent CTP in a micro-reaction device by utilizing liquid and liquid two-phase flow, greatly improving the production efficiency and reaction yield of synthesizing CTP, and at the same time It improves the purity and quality stability of the product, has a good application prospect, and can produce considerable economic and social benefits.
Description
The application is filed as application No. 201910203186.3 on 03-18.2019, and is entitled "a system and a method for synthesizing rubber scorch retarder CTP by continuous flow micro-reaction".
Technical Field
The invention belongs to the technical field of fine chemical engineering, and particularly relates to a system and a method for synthesizing a rubber scorch retarder CTP through continuous flow micro-reaction.
Background
Rubber scorch retarder ctp (pvi) chemical name N-cyclohexylthiophthalimide, CAS: 17796-82-6, formula: c14H15O2SN, molecular weight: 261.3, physicochemical properties: white or light yellow crystals, readily soluble in benzene, diethyl ether, acetone and ethyl acetate, in warm n-heptane and carbon tetrachloride. Slightly soluble in gasoline, insoluble in kerosene and water. The additive can effectively prevent rubber from scorching in the processing process, is widely applied to the fields of natural rubber and synthetic rubber, has a good scorching prevention effect when being used together with various universal accelerators, and can greatly improve the processing safety and the storage stability of rubber materials on the premise of not influencing the vulcanization speed and the vulcanized rubber performance.
Currently, most of CTP synthesis is a batch kettle type reaction, which is a heterogeneous liquid-solid reaction. The main reaction is the condensation of sodium salt of phthalimide and cyclohexyl sulfenyl chloride, which is as follows:
in the batch kettle type reaction synthesis process of CTP, reaction raw materials are easy to decompose, and two phases are not easy to be fully and uniformly mixed during the reaction, so that the heterogeneous reaction has the disadvantages of poor mass transfer efficiency, long reaction time, more side reactions, and low yield and purity. Therefore, how to shorten the reaction period, sufficiently, rapidly and efficiently mix the two raw material solutions, inhibit the decomposition of the raw material solutions and the occurrence of side reactions, and improve the reaction yield and the product purity has become a key point of research of many researchers.
Disclosure of Invention
In view of the above, the present invention aims to provide a system and a method for synthesizing a rubber scorch retarder CTP by continuous flow micro-reaction, which break through the technical barrier of the traditional synthetic process method, convert the existing batch reactor reaction into continuous micro-reaction, realize continuous operation of the rubber scorch retarder CTP synthesis, shorten the reaction period, and improve the reaction yield and the product purity.
The invention provides a system for synthesizing rubber scorch retarder CTP by continuous flow micro-reaction, which comprises:
a pipeline for conveying a mixed solution of cyclohexyl sulfenyl chloride and a catalyst;
a delivery pipeline for the mixed liquid of the phthalimide sodium salt and the catalyst;
the micro-reaction device is respectively connected with the discharge ports of the cyclohexyl sulfenyl chloride and catalyst mixed liquid conveying pipeline and the discharge ports of the phthalimide sodium salt and catalyst mixed liquid conveying pipeline;
the micro-reaction device is a tubular reactor.
Preferably, the cyclohexyl sulfenyl chloride and catalyst mixed liquor conveying pipeline is sequentially provided with a first filter, a first flat flow metering pump, a first mass flow meter and a first pressure gauge along the mixed liquor conveying direction;
and the delivery pipeline of the phthalimide sodium salt and the catalyst mixed liquor is sequentially provided with a second filter, a second horizontal flow metering pump, a second mass flow meter and a second pressure gauge along the delivery direction of the mixed liquor.
Preferably, the device further comprises an acidimeter, wherein the acidimeter is arranged at a discharge hole of the micro-reaction device.
Preferably, the tubular reactor is a spiral stirring tubular reactor and comprises a shell 301 and a cylindrical cavity 302, an interlayer 303 is arranged between the shell 301 and the cylindrical cavity 302, and a cooling medium is filled in the interlayer 303 when the tubular reactor is used; the top of the shell 301 is provided with a feed inlet 304 connected with the cylindrical cavity 302, the bottom of the shell 301 is provided with a discharge outlet 305 connected with the cylindrical cavity 302, and the side surface of the shell 301 is respectively provided with a cooling medium inlet 306 and a cooling medium outlet 307 extending into the interlayer 303; a vertical rotating shaft 308 is arranged in the cylindrical cavity 302, a spiral stirring blade 309 is installed on the rotating shaft 308, and the end of the rotating shaft 308 is connected with a motor.
Preferably, the diameter of the cylindrical cavity 302 is 0.2-1.5 m; the gap distance between the edge of the spiral stirring blade 309 and the inner side wall of the cylindrical cavity 302 is 1-3 mm.
The invention provides a method for synthesizing rubber scorch retarder CTP by continuous flow micro-reaction, which comprises the following steps:
conveying the reaction liquid A and the reaction liquid B into a micro-reaction device for continuous reaction, and obtaining a rubber scorch retarder CTP at a discharge hole of the micro-reaction device;
the reaction liquid A comprises a cyclohexyl sulfenyl chloride solution, and the reaction liquid B comprises a phthalimide sodium salt solution; the reaction liquid A and/or the reaction liquid B also contain a catalyst;
the micro-reaction device is a tubular reactor.
Preferably, the catalyst is selected from one or more of benzyltriethylammonium chloride, tetrabutylammonium bromide, tetrabutylammonium chloride, tetrabutylammonium hydrogen sulfate, trioctylmethylammonium chloride, dodecyltrimethylammonium chloride and tetradecyltrimethylammonium chloride;
the catalyst accounts for 1-10 per mill of the mass of the reaction liquid A or the reaction liquid B.
Preferably, in the continuous reaction process, the feeding pressure of the tubular reactor is 0.01-0.50 MPa, the feeding flow of the tubular reactor is 1000-3000L/h, the temperature of the continuous reaction is-5-25 ℃, the rotating speed of the tubular reactor is 200-1000 r/min, the residence time of the reaction liquid A and the reaction liquid B in the tubular reactor is 1-10 min, and the pH value of the material at the discharge port is 4-10.
Compared with the prior art, the invention provides a system and a method for synthesizing rubber scorch retarder CTP by continuous flow micro-reaction. The system provided by the invention comprises: a pipeline for conveying a mixed solution of cyclohexyl sulfenyl chloride and a catalyst; a delivery pipeline for the mixed liquid of the phthalimide sodium salt and the catalyst; the micro-reaction device is respectively connected with the discharge ports of the cyclohexyl sulfenyl chloride and catalyst mixed liquid conveying pipeline and the discharge ports of the phthalimide sodium salt and catalyst mixed liquid conveying pipeline; the micro-reaction device is a tubular reactor. The method provided by the invention comprises the following steps: conveying the reaction liquid A and the reaction liquid B into a micro-reaction device for continuous reaction, and obtaining a rubber scorch retarder CTP at a discharge hole of the micro-reaction device; the reaction liquid A comprises a cyclohexyl sulfenyl chloride solution, and the reaction liquid B comprises a phthalimide sodium salt solution; the reaction liquid A and/or the reaction liquid B also contain a catalyst; the micro-reaction device is a tubular reactor. The system and the method provided by the invention fully contact and react the synthesized rubber scorch retarder CTP in the micro-reaction device by utilizing the liquid-liquid two-phase flow, thereby realizing the uninterrupted reaction of CTP synthesis, greatly improving the production efficiency and the reaction yield of the synthesized CTP, simultaneously improving the purity and the quality stability of the product, having better application prospect and generating considerable economic benefit and social benefit.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a Y-type feed inlet microchannel reactor provided by an embodiment of the invention;
FIG. 2 is an enlarged partial schematic view of a single stage microchannel provided by an embodiment of the invention;
figure 3 is a schematic diagram of a high shear reactor with multiple stages of stator and rotor configurations provided by an embodiment of the present invention;
FIG. 4 is a schematic structural view of a helical stirred tube reactor according to an embodiment of the present invention;
FIG. 5 is a flow chart of a system for synthesizing rubber scorch retarder CTP by continuous flow micro-reaction provided by the embodiment of the invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The invention provides a system for synthesizing rubber scorch retarder CTP by continuous flow micro-reaction, which comprises:
a pipeline for conveying a mixed solution of cyclohexyl sulfenyl chloride and a catalyst;
a delivery pipeline for the mixed liquid of the phthalimide sodium salt and the catalyst;
the micro-reaction device is respectively connected with the discharge ports of the cyclohexyl sulfenyl chloride and catalyst mixed liquid conveying pipeline and the discharge ports of the phthalimide sodium salt and catalyst mixed liquid conveying pipeline;
the micro-reaction device is a micro-channel reactor, a high shear reactor or a tubular reactor.
The system provided by the invention comprises a cyclohexyl sulfenyl chloride and catalyst mixed liquid conveying pipeline, a phthalimide sodium salt and catalyst mixed liquid conveying pipeline and a micro-reaction device. The pipeline for conveying the mixed liquid of the cyclohexyl sulfenyl chloride and the catalyst is used for conveying the mixed liquid of the cyclohexyl sulfenyl chloride and the catalyst or a cyclohexyl sulfenyl chloride solution. In one embodiment of the present invention, the cyclohexylsulfenyl chloride and catalyst mixed liquor conveying pipe is provided with a first filter, a first mass flow meter, a first pressure gauge, and a first mass flow meter in this order in the mixed liquor conveying direction.
In the invention, the pipe for conveying the mixed liquid of the sodium phthalimide and the catalyst is used for conveying the mixed liquid of the sodium phthalimide and the catalyst or the sodium phthalimide solution. In one embodiment of the invention, the phthalimide sodium salt and catalyst mixed liquor conveying pipeline is sequentially provided with a second filter, a second two-flow metering pump, a second mass flow meter and a second pressure gauge along the mixed liquor conveying direction.
In the invention, the micro-reaction device is a micro-channel reactor, a high shear reactor or a tubular reactor, and a feed inlet of the micro-reaction device is respectively connected with a discharge port of the cyclohexyl sulfenyl chloride and catalyst mixed liquid conveying pipeline and a discharge port of the phthalimide sodium salt and catalyst mixed liquid conveying pipeline, and is used for carrying out a mixing reaction of the cyclohexyl sulfenyl chloride and the phthalimide sodium salt.
In the invention, the microchannel reactor can be a Y-shaped feed inlet microchannel reactor. The following describes a Y-type feed inlet microchannel reactor provided by the present invention with reference to fig. 1 and 2, fig. 1 is a schematic structural view of the Y-type feed inlet microchannel reactor provided by the embodiment of the present invention, fig. 2 is a partially enlarged schematic view of a single-stage microchannel provided by the embodiment of the present invention, and in fig. 1 and 2, 101 denotes a feed inlet, 102 denotes a microchannel, 103 denotes a discharge outlet, 104 denotes an inlet of the microchannel, and 105 denotes an outlet of the microchannel. In the invention, the Y-shaped feed inlet microchannel reactor comprises a feed inlet 101, a microchannel 102 and a discharge outlet 103, wherein the feed inlet 101 is connected with an inlet 104 of the microchannel 102, and the discharge outlet 103 is connected with an outlet 105 of the microchannel 102. In one embodiment of the present invention, the micro channel 102 is a fence shape, and the diameter is preferably 10-100 mm, and specifically may be 10mm, 15mm, 20mm, 25mm, 30mm, 35mm, 40mm, 45mm, 50mm, 55mm, 60mm, 65mm, 70mm, 75mm, 80mm, 85mm, 90mm, 95mm, or 100 mm. In one embodiment of the present invention, the microchannel 102 is multi-stage, and the inlets and outlets of the multi-stage microchannels 102 are connected in sequence.
In the present invention, the high shear reactor may be specifically a high shear reactor with a multi-stage stator rotor. Referring to fig. 3, a high shear reactor with a multi-stage stator and rotor according to the present invention is described, fig. 3 is a schematic structural diagram of a high shear reactor with a multi-stage stator and rotor according to an embodiment of the present invention, in fig. 3, 201 denotes a housing, 202 denotes a stator, 203 denotes a rotor, 204 denotes a drive shaft, 205 denotes a feed inlet, 206 denotes a discharge outlet, 207 denotes a stator base, 208 denotes a mechanical seal, 209 denotes a stator ring gear, and 210 denotes a rotor ring gear. In the invention, the high shear reactor comprises a shell 201, a stator 202, a rotor 203 and a transmission shaft 204, wherein a feed inlet 205 is arranged on one side of the shell 201, a discharge outlet 206 is arranged on the top of the shell, the stator 202 is arranged on a stator base 207 arranged on the inner surface of the side wall of the shell 201 connected with the feed inlet 201 of the reactor, the rotor 203 is arranged on the transmission shaft 204, the stator 202 and the rotor 203 are mutually matched, a mechanical seal 208 is also arranged on the transmission shaft 204, and one end of the transmission shaft 204 is connected with a. In one embodiment of the present invention, the stator 202 is provided with a stator ring gear 209, the rotor 203 is provided with a rotor ring gear 210, and the stator ring gear 209 and the rotor ring gear 210 are engaged with each other.
In the present invention, the tubular reactor may be specifically a helical stirred tubular reactor. In fig. 4, 301 denotes a housing, 302 denotes a cylindrical cavity, 303 denotes an interlayer, 304 denotes a feed port, 305 denotes a discharge port, 306 denotes a cooling medium inlet, 307 denotes a cooling medium outlet, 308 denotes a vertical rotation shaft, and 309 denotes a helical stirring blade. In the invention, the spiral stirring pipe type reactor comprises a shell 301 and a cylindrical cavity 302, an interlayer 303 is arranged between the shell 301 and the cylindrical cavity 302, and a cooling medium is filled in the interlayer 303 in the use process of the reactor; the top of the shell 301 is provided with a feed inlet 304 connected with the cylindrical cavity 302, the bottom of the shell 301 is provided with a discharge outlet 305 connected with the cylindrical cavity 302, and the side surface of the shell 301 is respectively provided with a cooling medium inlet 306 and a cooling medium outlet 307 extending into the interlayer 303; a vertical rotating shaft 308 is arranged in the cylindrical cavity 302, a spiral stirring blade 309 is installed on the rotating shaft 308, and the end of the rotating shaft 308 is connected with a motor. In an embodiment provided by the present invention, the diameter of the cylindrical cavity 302 is preferably 0.2-1.5 m, and specifically may be 0.2m, 0.3m, 0.4m, 0.5m, 0.6m, 0.7m, 0.8m, 0.9m, 1m, 1.1m, 1.2m, 1.3m, 1.4m, or 1.5 m. In an embodiment provided by the present invention, the gap distance between the edge of the helical stirring blade 309 and the inner sidewall of the cylindrical cavity 302 is preferably 1-3 mm, and specifically may be 1mm, 1.2mm, 1.5mm, 1.7mm, 2mm, 2.3mm, 2.5mm, 2.7mm, or 3 mm.
In the present invention, the system preferably further comprises an acidimeter, which is disposed at the discharge port of the micro-reaction device and is used for monitoring the pH value of the material (i.e., the reaction product) at the discharge port.
In the invention, the system preferably further comprises a post-treatment device, and a feed inlet of the post-treatment device is connected with a discharge outlet of the micro-reaction device and is used for post-treating materials at the discharge outlet of the micro-reaction device, so that the purity and the quality of products are improved. In one embodiment provided by the invention, the post-treatment device comprises a continuous phase separator, a purification unit, a solid-liquid separation unit, a drying unit and a screening unit which are sequentially arranged along the material conveying direction.
The invention also provides a method for synthesizing the rubber scorch retarder CTP by continuous flow micro-reaction, which comprises the following steps:
conveying the reaction liquid A and the reaction liquid B into a micro-reaction device for continuous reaction to obtain a rubber scorch retarder CTP at a discharge hole of the micro-reaction device;
the reaction liquid A comprises a cyclohexyl sulfenyl chloride solution, and the reaction liquid B comprises a phthalimide sodium salt solution; the reaction liquid A and/or the reaction liquid B also contain a catalyst;
the micro-reaction device is a micro-channel reactor, a high shear reactor or a tubular reactor.
In the method provided by the present invention, first, a reaction solution a and a reaction solution B are provided. The reaction solution A comprises a cyclohexyl sulfenyl chloride solution, and the concentration of the cyclohexyl sulfenyl chloride in the reaction solution A is preferably 12-25 wt%, and specifically can be 12 wt%, 13 wt%, 14 wt%, 15 wt%, 16 wt%, 17 wt%, 18 wt%, 19 wt%, 20 wt%, 21 wt%, 22 wt%, 23 wt%, 24 wt% or 25 wt%; the reaction liquid B comprises a phthalimide sodium salt solution, and the concentration of the phthalimide sodium salt in the reaction liquid B is preferably 15-30 wt%, and specifically can be 15 wt%, 16 wt%, 17 wt%, 18 wt%, 19 wt%, 20 wt%, 21 wt%, 22 wt%, 23 wt%, 24 wt%, 25 wt%, 26 wt%, 27 wt%, 28 wt%, 29 wt% or 30 wt%. In the present invention, the reaction solution a and/or the reaction solution B further contains a catalyst, wherein the catalyst is preferably selected from ammonium salt type surfactants, including but not limited to one or more of benzyltriethylammonium chloride, tetrabutylammonium bromide, tetrabutylammonium chloride, tetrabutylammonium hydrogen sulfate, trioctylmethylammonium chloride, dodecyltrimethylammonium chloride and tetradecyltrimethylammonium chloride; the catalyst preferably accounts for 1-10% of the mass of the cyclohexylsulfenyl chloride solution in the reaction liquid a or the phthalimide sodium salt solution in the reaction liquid B, and specifically may be 1%, 1.5%, 2%, 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, 5.5%, 6%, 6.5%, 7%, 7.5%, 8%, 8.5%, 9%, 9.5% or 10%. In the present invention, the storage temperature of the reaction solution A before being transferred to the micro-reaction apparatus is preferably controlled to-5 to 15 ℃, and specifically may be-5 ℃, -4 ℃, -3 ℃, -2 ℃, -1 ℃, 0 ℃, 1 ℃, 2 ℃, 3 ℃, 4 ℃, 5 ℃, 6 ℃, 7 ℃, 8 ℃, 9 ℃, 10 ℃, 11 ℃, 12 ℃, 13 ℃, 14 ℃ or 15 ℃; the preservation temperature of the reaction solution B before being conveyed to the micro-reaction device is preferably controlled to be-3-10 ℃, and specifically can be-3 ℃, 2 ℃, 1 ℃, 0 ℃, 1 ℃, 2 ℃, 3 ℃, 4 ℃, 5 ℃, 6 ℃, 7 ℃, 8 ℃, 9 ℃ or 10 ℃.
In the method provided by the invention, after the reaction liquid A and the reaction liquid B are obtained, the reaction liquid A and the reaction liquid B are conveyed to a micro-reaction device for continuous reaction. Wherein the molar ratio of the cyclohexylsulfenyl chloride in the reaction liquid a to the phthalimide sodium salt in the reaction liquid B is preferably 1: (0.8-1.2), specifically 1:0.8, 1:0.9, 1:1, 1:1.1 or 1: 1.2; the volume ratio of the reaction liquid a to the reaction liquid B is preferably 1: (0.5-1.5), specifically 1:0.5, 1:0.6, 1:0.7, 1:0.8, 1:0.9, 1:1, 1:1.1, 1:1.2, 1:1.3, 1:1.4 or 1: 1.5; the micro-reaction device is a micro-channel reactor, a high shear reactor or a tubular reactor, and the specific structure thereof is described above and will not be described herein.
In one embodiment provided by the present invention, the micro-reaction device selects a microchannel reactor; in the continuous reaction process, the feeding pressure of the microchannel reactor is preferably 0.01-0.50 MPa, and specifically can be 0.01MPa, 0.05MPa, 0.10MPa, 0.15MPa, 0.20MPa, 0.25MPa, 0.30MPa, 0.35MPa, 0.40MPa, 0.45MPa or 0.50 MPa; in the continuous reaction process, the feeding flow of the microchannel reactor is preferably 1000-3000L/h, and specifically can be 1000L/h, 1200L/h, 1500L/h, 1700L/h, 2000L/h, 2300L/h, 2500L/h, 2700L/h and 3000L/h; in the continuous reaction process, the temperature of the continuous reaction is preferably-5-30 ℃, more preferably 15-30 ℃, and specifically can be 15 ℃, 16 ℃, 17 ℃, 18 ℃, 19 ℃, 20 ℃, 21 ℃, 22 ℃, 23 ℃, 24 ℃, 25 ℃, 26 ℃, 27 ℃, 28 ℃, 29 ℃ or 30 ℃; in the continuous reaction process, the residence time of the reaction liquid A and the reaction liquid B in the microchannel reactor is preferably 1-15 min, and specifically can be 1min, 2min, 3min, 4min, 5min, 6min, 7min, 8min, 9min, 10min, 11min, 12min, 13min, 14min or 15 min; in the continuous reaction process, the pH value of the material at the discharge port is preferably 4-10, and specifically can be 4, 5, 6, 7, 8, 9 or 10.
In one embodiment provided herein, the micro-reaction device is selected from a high shear reactor; in the continuous reaction process, the feeding pressure of the high-shear reactor is preferably 0.01-1.0 MPa, and specifically can be 0.01MPa, 0.05MPa, 0.10MPa, 0.15MPa, 0.20MPa, 0.25MPa, 0.30MPa, 0.35MPa, 0.40MPa, 0.45MPa, 0.50MPa, 0.55MPa, 0.60MPa, 0.65MPa, 0.70MPa, 0.75MPa, 0.80MPa, 0.85MPa, 0.90MPa, 0.95MPa or 1.0 MPa; in the continuous reaction process, the feeding flow of the high shear reactor is preferably 1000-3000L/h, and specifically can be 1000L/h, 1200L/h, 1500L/h, 1700L/h, 2000L/h, 2300L/h, 2500L/h, 2700L/h and 3000L/h; in the continuous reaction process, the temperature of the continuous reaction is preferably-3 to 15 ℃, more preferably 10 to 15 ℃, and specifically can be 10 ℃, 10.5 ℃, 11 ℃, 11.5 ℃, 12 ℃, 12.5 ℃, 13 ℃, 13.5 ℃, 14 ℃, 14.5 ℃ or 15 ℃; in the continuous reaction process, the rotating speed of the high-shear reactor is preferably 2500-5500 r/min, and specifically can be 2500r/min, 3000r/min, 3500r/min, 4000r/min, 4500r/min, 5000r/min or 5500 r/min; in the continuous reaction process, the residence time of the reaction liquid A and the reaction liquid B in the high shear reactor is preferably 1-10 min, and specifically can be 1min, 2min, 3min, 4min, 5min, 6min, 7min, 8min, 9min or 10 min; in the continuous reaction process, the pH value of the material at the discharge port is preferably 4-10, and specifically can be 4, 5, 6, 7, 8, 9 or 10.
In one embodiment provided by the present invention, the micro-reaction device is selected from a tubular reactor; in the continuous reaction process, the feeding pressure of the tubular reactor is preferably 0.01-0.50 MPa, and specifically can be 0.01MPa, 0.05MPa, 0.10MPa, 0.15MPa, 0.20MPa, 0.25MPa, 0.30MPa, 0.35MPa, 0.40MPa, 0.45MPa or 0.50 MPa; in the continuous reaction process, the feeding flow of the tubular reactor is preferably 1000-3000L/h, and specifically can be 1000L/h, 1200L/h, 1500L/h, 1700L/h, 2000L/h, 2300L/h, 2500L/h, 2700L/h and 3000L/h; in the continuous reaction process, the temperature of the continuous reaction is preferably-5-25 ℃, more preferably 10-25 ℃, and specifically can be 10 ℃, 11 ℃, 12 ℃, 13 ℃, 14 ℃, 15 ℃, 16 ℃, 17 ℃, 18 ℃, 19 ℃, 20 ℃, 21 ℃, 22 ℃, 23 ℃, 24 ℃ or 25 ℃; in the continuous reaction process, the rotation speed of the tubular reactor is preferably 200-1000 r/min, and specifically can be 200r/min, 250r/min, 300r/min, 350r/min, 400r/min, 450r/min, 500r/min, 550r/min, 600r/min, 650r/min, 700r/min, 750r/min, 800r/min, 850r/min, 900r/min, 950r/min or 1000 r/min; in the continuous reaction process, the residence time of the reaction liquid A and the reaction liquid B in the tubular reactor is preferably 1-10 min, and specifically can be 1min, 2min, 3min, 4min, 5min, 6min, 7min, 8min, 9min or 10 min; in the continuous reaction process, the pH value of the material at the discharge port is preferably 4-10, and specifically can be 4, 5, 6, 7, 8, 9 or 10.
In the method provided by the invention, after the reaction liquid A and the reaction liquid B are subjected to continuous reaction, the rubber scorch retarder CTP is obtained at the discharge hole of the micro-reaction device. In the present invention, in order to improve the purity and quality of the rubber scorch retarder CTP product, the obtained rubber scorch retarder CTP is preferably subjected to a post-treatment, and the specific process of the post-treatment preferably comprises: and sequentially carrying out phase splitting, purification, solid-liquid separation, drying and screening on the rubber scorch retarder CTP obtained at the discharge hole to obtain a high-quality rubber scorch retarder CTP product.
The system and the method provided by the invention fully contact and react the synthesized rubber scorch retarder CTP in the micro-reaction device by utilizing the liquid-liquid two-phase flow, thereby realizing the uninterrupted reaction of CTP synthesis, greatly improving the production efficiency and the reaction yield of the synthesized CTP, and simultaneously improving the purity and the quality stability of the product.
More specifically, the present invention provides systems and methods that include at least the following advantages:
1. the invention utilizes the micro-reaction device to prepare the synthetic CTP, has simple process, convenient operation, small occupied area and easy large-scale production and application; in the preferred technical scheme provided by the invention, through the arranged flowmeter and the pressure gauge, the proportion of each raw material can be accurately controlled, so that the raw materials are quickly and uniformly mixed, the mass transfer and reaction efficiency is greatly improved, the reaction period is shortened to 1-15 min from 0.5-2 h, and the raw material decomposition and side reaction can be more favorably inhibited; in another preferred technical scheme provided by the invention, the pH value of the terminal material after the reaction can be monitored in real time by arranging the acidimeter, so that the inflow of two raw material liquids is fed back and adjusted, the reaction can be carried out stably, efficiently and orderly, and the drift of the material input ratio in the production process is prevented.
2. The method for synthesizing CTP by using the micro-reaction device provided by the invention is carried out in a continuous flow mode, realizes the uninterrupted reaction of CTP synthesis, greatly improves the production efficiency and the conversion rate of the reaction, has stable product quality, ensures that the prepared CTP has more excellent performance, simultaneously uses less water in the preparation process, reduces the generation of synthetic wastewater and the pollution of COD in the wastewater to the environment, is safer, more environment-friendly and pollution-free, accords with the development direction of developing green chemical industry, has better application prospect, and can generate considerable economic benefit and social benefit.
3. The invention utilizes a micro-reaction device to synthesize CTP, has low energy consumption and high stability, and can fully contact liquid and liquid phases to ensure more complete reaction for heterogeneous liquid-solid reaction compared with the traditional intermittent reaction kettle; in the preferred technical scheme provided by the invention, according to the characteristics of CTP reaction, by selecting micro-reaction devices such as a micro-channel reactor with a Y-shaped feed inlet with the diameter of 10-100 mm, a high-shear reactor with a stator and a rotor, a tubular reactor with a spiral stirrer and the like which are suitable for the reaction, the mass transfer and the reaction rate are improved, and meanwhile, the anti-blocking effect can be achieved, so that the rapid and smooth reaction is facilitated.
4. The experimental results show that: the purity and the yield of the CTP product prepared by the method are higher, and the purity is improved by 1-1.5% compared with the product prepared by the traditional process; compared with the traditional process, the yield is improved by 5-7% and reaches more than 95%.
For the sake of clarity, the following examples are given in detail.
Example 1
System for synthesizing rubber scorch retarder CTP through continuous flow micro-reaction
The present embodiment provides a continuous flow micro-reaction synthetic rubber scorch retarder CTP system as shown in FIG. 5, comprising: a cyclohexyl sulfenyl chloride and catalyst mixed liquid conveying pipeline 1, a phthalimide sodium salt and catalyst mixed liquid conveying pipeline 2, a micro-reaction device 11, an acidimeter 12 and a post-treatment device 13.
In this example, the cyclohexylsulfenyl chloride and catalyst mixed liquor conveying pipe 1 is provided with a first filter 3, a first mass flow meter pump 5, a first mass flow meter 7, and a first pressure gauge 9 in this order in the mixed liquor conveying direction.
In the present embodiment, the phthalimide sodium salt and catalyst mixed liquor conveying pipe 2 is provided with a second filter 4, a second two-flow metering pump 6, a second mass flow meter 8, and a second pressure gauge 10 in this order in the mixed liquor conveying direction.
In this embodiment, the feed inlet of the micro-reaction device 11 is connected to the discharge port of the cyclohexylsulfenyl chloride and catalyst mixed liquid conveying pipeline 1 and the discharge port of the phthalimide sodium salt and catalyst mixed liquid conveying pipeline 2, respectively.
In this embodiment, the acidimeter 12 is disposed at the discharge port of the micro-reaction device 11.
In this embodiment, the feed inlet of the post-treatment device 13 is connected to the discharge outlet of the micro-reaction device 11, and the post-treatment device 13 includes a continuous phase separator, a purification unit, a solid-liquid separation unit, a drying unit and a sieving unit, which are sequentially arranged along the material conveying direction.
In this embodiment, the micro-reactor 11 may be a Y-type feeding-port micro-channel reactor, a high shear reactor with multi-stage stator and rotor, or a spiral stirring pipe reactor.
In this embodiment, the structure of the Y-type feed inlet microchannel reactor is shown in fig. 1 and fig. 2, and includes a feed inlet 101, a microchannel 102, and a discharge outlet 103, where the feed inlet 101 is connected to an inlet 104 of the microchannel 102, and the discharge outlet 103 is connected to an outlet 105 of the microchannel 102; the micro-channel 102 is fence-shaped and has a diameter of 50 mm; the micro-channel 102 is multi-stage, and the inlet and outlet of the multi-stage micro-channel 102 are connected in sequence.
In this embodiment, the structure with a multi-stage stator-rotor high shear reactor is shown in fig. 3, and includes a housing 201, a stator 202, a rotor 203, and a transmission shaft 204, wherein a feed port 205 is formed at one side of the housing 201, a discharge port 206 is formed at the top of the housing 201, the stator 202 is mounted on a stator base 207 arranged on the inner surface of the sidewall of the housing 201 connected to the feed port 201 of the reactor, the rotor 203 is mounted on the transmission shaft 204, the stator 202 and the rotor 203 are mutually matched, a mechanical seal 208 is further mounted on the transmission shaft 204, and one end of the transmission; the stator 202 is provided with a stator ring gear 209, the rotor 203 is provided with a rotor ring gear 210, and the stator ring gear 209 and the rotor ring gear 210 are engaged with each other.
In this embodiment, the structure of the spiral stirred tube reactor is shown in fig. 4, and includes a shell 301 and a cylindrical cavity 302, an interlayer 303 is disposed between the shell 301 and the cylindrical cavity 302, and a cooling medium is filled in the interlayer 303 during the use of the reactor; the top of the shell 301 is provided with a feed inlet 304 connected with the cylindrical cavity 302, the bottom of the shell 301 is provided with a discharge outlet 305 connected with the cylindrical cavity 302, and the side surface of the shell 301 is respectively provided with a cooling medium inlet 306 and a cooling medium outlet 307 extending into the interlayer 303; a vertical rotating shaft 308 is arranged in the cylindrical cavity 302, a spiral stirring blade 309 is installed on the rotating shaft 308, and the end part of the rotating shaft 308 is connected with a motor; the diameter of the cylindrical cavity 302 is 1 m; the edge of the helical stirring blade 309 is spaced from the inner side wall of the cylindrical cavity 302 by a distance of 2 mm.
Example 2
Method for synthesizing rubber scorch retarder CTP through continuous flow micro-reaction
The synthesis of the rubber scorch retarder CTP was performed in the system provided in example 1, wherein the micro-reaction device in the system was a Y-type feed inlet micro-channel reactor, and the specific synthesis process was as follows:
uniformly mixing a catalyst (benzyltriethylammonium chloride) into a prepared cyclohexyl sulfenyl chloride solution with the concentration of 12-25 wt% and the temperature of-5-15 ℃, wherein the dosage of the catalyst is 5 per mill of the mass of the cyclohexyl sulfenyl chloride solution; storing the prepared phthalimide sodium salt solution with the concentration of 15-30 wt% in an environment of-3-10 ℃.
Then simultaneously starting a first and a second horizontal flow metering pumps, and conveying a mixed solution (marked as a reaction solution A) of cyclohexyl sulfenyl chloride and a catalyst and a phthalimide sodium salt solution (marked as a reaction solution B) into a micro-reaction device, wherein the conveying process comprises the steps that the reaction solution A sequentially flows through a first filter, the first horizontal flow metering pump, a first mass flow meter and a first pressure gauge and then enters a Y-shaped feed inlet micro-channel reactor through a feed inlet, and the reaction solution B sequentially flows through a second filter, the second horizontal flow metering pump, a second mass flow meter and a second pressure gauge and then enters the Y-shaped feed inlet micro-channel reactor through the feed inlet; meanwhile, the molar ratio of the cyclohexylsulfenyl chloride in the reaction liquid a to the phthalimide sodium salt in the reaction liquid B was 1: (0.8 to 1.2), VReaction solution A：VReaction solution BControlling the pressure of the feed of the microchannel reactor to be 0.20MPa, controlling the feed flow rate of the microchannel reactor to be 2000L/h, maintaining the reaction temperature of the inner cavity of the reactor to be 25 ℃, and maintaining the residence time of the reaction liquid in the reactor to be 5min at 1 (0.5-1.5);
during the operation of the Y-shaped feed inlet microchannel reactor, a CTP crude product is continuously obtained at a discharge port of the reactor, and the pH value of a reacted terminal material is monitored in real time by using an acidimeter arranged at the discharge port of the reactor, so that the stable, effective and efficient reaction is ensured, and when the pH value detected by the acidimeter is not within the range of 6-8, the dosage ratio of two strands of mixed liquid can be subjected to micro adjustment according to the specific value of the pH value, so that the optimal reaction proportion is reached.
After obtaining the CTP crude product, sequentially carrying out phase splitting, purification, solid-liquid separation, drying and screening on the obtained CTP crude product in a post-treatment device to obtain 1005kg of CTP finished product with the flow rate of 3 hours, wherein the detection result shows that the purity is 98.82%, the yield is 95.3%, the initial melting point is 90.2 ℃, and other indexes meet the requirements of national standard GB/T24801-2009.
Example 3
Method for synthesizing rubber scorch retarder CTP through continuous flow micro-reaction
The synthesis of the rubber scorch retarder CTP was performed in the system provided in example 1, wherein the micro-reactor device in the system was selected to have a multi-stage stator-rotor high shear reactor, and the specific synthesis process was as follows:
uniformly mixing a catalyst (benzyltriethylammonium chloride) into a phthalimide sodium salt solution with the concentration of 15-30 wt% and the temperature of-3-10 ℃, wherein the dosage of the catalyst is 5 per thousand of the mass of the phthalimide sodium salt solution; storing the prepared cyclohexyl sulfenyl chloride solution with the concentration of 12-25 wt% in an environment of-5-15 ℃.
Then starting a first and a second horizontal flow metering pumps simultaneously, conveying the cyclohexylsulfenyl chloride solution (marked as reaction liquid A) and the mixed solution of phthalimide sodium salt and a catalyst (marked as reaction liquid B) into a micro-reaction device, wherein the conveying process comprises the steps that the reaction liquid A sequentially flows through a first filter, the first horizontal flow metering pump, a first mass flow meter and a first pressure gauge and then enters a high-shear reactor with a multi-stage stator and a rotor through a feeding hole, and the reaction liquid B sequentially flows through a second filter, the second horizontal flow metering pump, a second mass flow meter and a second pressure gauge and then enters the high-shear reactor with the multi-stage stator and the rotor through the feeding hole; meanwhile, the molar ratio of the cyclohexylsulfenyl chloride in the reaction liquid a to the phthalimide sodium salt in the reaction liquid B was 1: (0.8 to 1.2), VReaction solution A：VReaction solution BThe pressure of the feeding material of the high-shear reactor is controlled to be 0.5-1.5 MPa, and the feeding flow of the high-shear reactor is controlled to be 0.50MPaControlling the speed at 2000L/h, setting the rotating speed of the high-shear reactor at 3500r/min, maintaining the reaction temperature of the inner cavity of the reactor at 12 ℃, and maintaining the residence time of the reaction liquid in the reactor at 2 min;
the method comprises the steps of continuously obtaining a CTP crude product at a discharge port of a reactor in the operation process of a high-shear reactor with a multi-stage stator and a multi-stage rotor, and monitoring the pH value of a reacted terminal material in real time by using an acidimeter arranged at the discharge port of the reactor, so that the stable, effective and efficient reaction is ensured, and when the pH value detected by the acidimeter is not within the range of 6-8, the dosage ratio of two strands of mixed liquid can be subjected to micro adjustment according to the specific value of the pH value, so as to achieve the optimal reaction ratio.
After obtaining the CTP crude product, sequentially carrying out phase splitting, purification, solid-liquid separation, drying and screening on the obtained CTP crude product in a post-treatment device to obtain 1025kg of CTP finished product with the flow rate of 3 hours, wherein the detection result shows that the purity is 99.02%, the yield is 96.1%, the initial melting point is 90.3 ℃, and other indexes all meet the requirements of national standard GB/T24801-2009.
Example 4
Method for synthesizing rubber scorch retarder CTP through continuous flow micro-reaction
The synthesis of the rubber scorch retarder CTP was performed in the system provided in example 1, wherein the micro-reaction device in the system was a spiral stirred tube reactor, and the specific synthesis process was as follows:
uniformly mixing a catalyst (benzyltriethylammonium chloride) into a prepared cyclohexyl sulfenyl chloride solution with the concentration of 12-25 wt% and the temperature of-5-15 ℃, wherein the dosage of the catalyst is 5 per mill of the mass of the cyclohexyl sulfenyl chloride solution; storing the prepared phthalimide sodium salt solution with the concentration of 15-30 wt% in an environment of-3-10 ℃.
Then simultaneously starting a first and a second horizontal flow metering pumps, conveying a mixed solution (marked as reaction liquid A) of cyclohexyl sulfenyl chloride and a catalyst and a sodium phthalimide solution (marked as reaction liquid B) into a micro-reaction device, wherein the conveying process comprises the steps that the reaction liquid A sequentially flows through a first filter, the first horizontal flow metering pump, a first mass flow meter and a first pressure gauge and then enters a spiral stirring tubular reactor through a feeding hole, and the reaction liquid B simultaneously enters the spiral stirring tubular reactor according to the reaction liquid AThe secondary flow enters the spiral stirring pipe type reactor through the feed inlet after passing through a second filter, a second flat flow metering pump, a second mass flow meter and a second pressure meter; meanwhile, the molar ratio of the cyclohexylsulfenyl chloride in the reaction liquid a to the phthalimide sodium salt in the reaction liquid B was 1: (0.8 to 1.2), VReaction solution A：VReaction solution BControlling the feeding pressure of a spiral stirring tubular reactor to be 0.20MPa, controlling the feeding flow rate of the spiral stirring tubular reactor to be 2000L/h, controlling the rotating speed of the spiral stirring tubular reactor to be 500r/min, maintaining the reaction temperature of an inner cavity of the reactor to be 20 ℃, and maintaining the residence time of a reaction solution in the reactor to be 5 min;
in the operation process of the spiral stirring tubular reactor, CTP crude products are continuously obtained at a discharge port of the reactor, and the pH value of a terminal material after reaction is monitored in real time by using an acidimeter arranged at the discharge port of the reactor, so that the reaction is ensured to be stable, effective and efficient, and when the pH value detected by the acidimeter is not within the range of 6-8, the dosage ratio of two strands of mixed liquid can be subjected to micro adjustment according to the specific value of the pH value, so that the optimal reaction ratio is reached.
After obtaining the CTP crude product, sequentially carrying out phase splitting, purification, solid-liquid separation, drying and screening on the obtained CTP crude product in a post-treatment device to obtain 1060kg of CTP finished product with the flow rate of 3 hours, wherein the detection result shows that the purity is 99.48%, the yield is 95.9%, the initial melting point is 90.5 ℃, and other indexes meet the requirements of the national standard GB/T24801-2009.
Evaluation of Effect
TABLE 1 comparison of inventive examples with results of batch tank reaction condition measurements (compare with 200kg dicyclohexyldisulfide charged):
the CTP product detection in Table 1 is carried out by high performance liquid chromatography, and the specific conditions are as follows:
1. a detector: a multi-wavelength ultraviolet spectral detector or a spectral detector with equal performance.
2. A chromatographic column: the stationary phase is a chromatographic column with C18, length of 250mm, inner diameter of 4.6mm, particle size of 5 μm or equivalent column efficiency.
3. Operating conditions of the high performance liquid chromatography:
| item | Operating conditions |
| Mobile phase/(V/V) | Acetonitrile: 80 parts of water: 20 |
| Flow rate/(mL/min) | 1.0 |
| Column temperature/. degree.C | 40 |
| Wavelength/nm | 254 |
As can be seen from Table 1, compared with the conventional batch reaction kettle, the CTP prepared by the method has higher yield and purity.
Table 2. the product of the example of the present invention is compared with the conventional antiscorching agent CTP powder product of the limited liability company of yin-decoction perpetual chemistry in the test of the application performance (under the same formulation condition, taking NR surface glue as an example):
as can be seen from Table 2, the CTP prepared by the method has equal or better performance compared with the CTP prepared by a traditional batch reaction kettle.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (8)
1. A system for synthesizing rubber scorch retarder CTP by continuous flow micro-reaction comprises:
a pipeline for conveying a mixed solution of cyclohexyl sulfenyl chloride and a catalyst;
a delivery pipeline for the mixed liquid of the phthalimide sodium salt and the catalyst;
the micro-reaction device is respectively connected with the discharge ports of the cyclohexyl sulfenyl chloride and catalyst mixed liquid conveying pipeline and the discharge ports of the phthalimide sodium salt and catalyst mixed liquid conveying pipeline;
the micro-reaction device is a tubular reactor.
2. The system of claim 1, wherein the cyclohexylsulfenyl chloride and catalyst mixed liquor conveying pipe is provided with a first filter, a first mass flow meter, a first pressure gauge in that order in the mixed liquor conveying direction;
and the delivery pipeline of the phthalimide sodium salt and the catalyst mixed liquor is sequentially provided with a second filter, a second horizontal flow metering pump, a second mass flow meter and a second pressure gauge along the delivery direction of the mixed liquor.
3. The system of claim 1, further comprising an acidimeter disposed at a discharge port of the micro-reaction device.
4. The system according to claim 1, wherein the tubular reactor is a spiral stirring tubular reactor, and comprises a shell 301 and a cylindrical cavity 302, an interlayer 303 is arranged between the shell 301 and the cylindrical cavity 302, and a cooling medium is filled in the interlayer 303 during the use of the reactor; the top of the shell 301 is provided with a feed inlet 304 connected with the cylindrical cavity 302, the bottom of the shell 301 is provided with a discharge outlet 305 connected with the cylindrical cavity 302, and the side surface of the shell 301 is respectively provided with a cooling medium inlet 306 and a cooling medium outlet 307 extending into the interlayer 303; a vertical rotating shaft 308 is arranged in the cylindrical cavity 302, a spiral stirring blade 309 is installed on the rotating shaft 308, and the end of the rotating shaft 308 is connected with a motor.
5. The system of claim 4, wherein the cylindrical cavity 302 has a diameter of 0.2-1.5 m; the gap distance between the edge of the spiral stirring blade 309 and the inner side wall of the cylindrical cavity 302 is 1-3 mm.
6. A method for synthesizing rubber scorch retarder CTP by continuous flow micro-reaction comprises the following steps:
conveying the reaction liquid A and the reaction liquid B into a micro-reaction device for continuous reaction, and obtaining a rubber scorch retarder CTP at a discharge hole of the micro-reaction device;
the reaction liquid A comprises a cyclohexyl sulfenyl chloride solution, and the reaction liquid B comprises a phthalimide sodium salt solution; the reaction liquid A and/or the reaction liquid B also contain a catalyst;
the micro-reaction device is a tubular reactor.
7. The method of claim 6, wherein the catalyst is selected from one or more of benzyltriethylammonium chloride, tetrabutylammonium bromide, tetrabutylammonium chloride, tetrabutylammonium hydrogen sulfate, trioctylmethylammonium chloride, dodecyltrimethylammonium chloride, and tetradecyltrimethylammonium chloride;
the catalyst accounts for 1-10 per mill of the mass of the reaction liquid A or the reaction liquid B.
8. The method according to claim 6, wherein in the continuous reaction process, the feeding pressure of the tubular reactor is 0.01-0.50 MPa, the feeding flow of the tubular reactor is 1000-3000L/h, the continuous reaction temperature is-5-25 ℃, the rotating speed of the tubular reactor is 200-1000 r/min, the residence time of the reaction liquid A and the reaction liquid B in the tubular reactor is 1-10 min, and the pH value of the material at the discharge port is 4-10.
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| CN110681327B (en) * | 2019-08-09 | 2021-07-23 | 中国科学院大连化学物理研究所 | Micro-reaction system and method for continuous synthesis of rubber scorch retarder CTP |
| CN112452271B (en) * | 2020-12-18 | 2025-03-28 | 中国科学院生态环境研究中心 | Rapid Mixing Reactor |
| CN115679099A (en) * | 2022-10-31 | 2023-02-03 | 河南金渠银通金属材料有限公司 | Device for reducing silver elementary substance from silver nitrate |
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| CN109876746A (en) | 2019-06-14 |
| CN109876746B (en) | 2022-04-12 |
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