A continuous reactor for glycine

Abstract

The utility model relates to the technical field of chemical reaction equipment, concretely relates to a glycine continuous reactor, including initial reactor and integrated reactor, and the series connection structure of glycine continuous reactor through initial reactor and integrated reactor has realized the whole process continuous flow of material from feeding, initial mixing to depth reaction, has overcome the inherent interruption and batch fluctuation of intermittent operation, and the inside of integrated reactor is divided into low temperature reaction section and high temperature reaction section according to material flow direction, and the constant temperature carrier import and export are independently configured respectively, thereby realizing the accurate zoning control of reaction temperature: low temperature reaction section is favorable to control main reaction rate and selectivity, and high temperature reaction section ensures reaction completely and inhibits byproduct. Through the design of continuous feeding and segmented temperature control cooperation, while guaranteeing reaction efficiency and product yield, completely get rid of the bottleneck such as plugging, coking and operation discontinuity caused by uneven mixing, extensive temperature control of traditional batch kettle.

Description

Technical Field

[0001] This utility model relates to the field of chemical reaction equipment technology, and in particular to a glycine continuous reactor. Background Technology

[0002] Glycine (aminoacetic acid), as one of the simplest amino acids with enormous industrial demand, has extremely wide applications in pharmaceuticals, food additives, feed, pesticides, and electroplating. Currently, the mainstream industrial method for synthesizing glycine is a derivative of the Strecker amino acid synthesis process, which uses hydroxyacetonitrile (ethanol nitrile) and ammonia as the main raw materials.

[0003] Traditional production processes typically employ batch reactors. This process usually involves first mixing hydroxyacetonitrile with excess ammonia in a mixer, then pumping the mixture into a reactor. The mixture is then heated via an external jacket or coil and held at a specific temperature for several hours to complete the reaction.

[0004] However, traditional batch reactors used for glycine synthesis cannot achieve continuous material flow and segmented temperature-controlled reactions in practical applications. Utility Model Content

[0005] The purpose of this invention is to provide a continuous glycine reactor that solves the problem that traditional batch reactors used for glycine synthesis cannot achieve continuous material flow and segmented temperature control in practical applications.

[0006] To achieve the above objectives, this utility model provides a glycine continuous reactor, which includes a primary reactor and an integrated reactor. The primary reactor has a hydroxyacetonitrile inlet and an ammonia inlet on both sides of its front end, and a discharge outlet at its rear end. The integrated reactor has a premix inlet on the side of its bottom and a reactant outlet on the side of its top. The premix inlet and the discharge outlet are connected by a pipe. The primary reactor is equipped with an insulation jacket on its exterior. The sides of the insulation jacket at both ends are respectively provided with a heat carrier inlet and a heat carrier outlet. The interior of the integrated reactor is divided into a low-temperature reaction section and a high-temperature reaction section from bottom to top along the material flow direction. The low-temperature reaction section is provided with a low-temperature constant-temperature carrier inlet and a low-temperature constant-temperature carrier outlet, and the high-temperature reaction section is provided with a high-temperature constant-temperature carrier inlet and a high-temperature constant-temperature carrier outlet.

[0007] The initial reactor is provided with a plurality of first distribution plates and a plurality of second distribution plates evenly arranged inside, with the plurality of first distribution plates and the plurality of second distribution plates arranged alternately.

[0008] The heat carrier inlet is located on the side of the primary reactor near the ammonia inlet, and the heat carrier outlet is located on the side of the primary reactor near the discharge outlet.

[0009] The low-temperature carrier inlet is located at the bottom of the low-temperature reaction section, and the low-temperature carrier outlet is located on the side of the top of the low-temperature reaction section, and on the side of the low-temperature reaction section away from the low-temperature carrier inlet.

[0010] The high constant temperature carrier inlet is located on one side of the bottom of the high temperature reaction section and on the side of the high temperature reaction section away from the low constant temperature carrier outlet. The high constant temperature carrier outlet is located at the top of the high temperature reaction section and on the side of the high temperature reaction section away from the high constant temperature carrier inlet.

[0011] Material flow rate control valves are installed at both the hydroxyacetonitrile inlet and the ammonia inlet.

[0012] Temperature sensors are installed in the insulation jacket, the low-temperature reaction section, and the high-temperature reaction section.

[0013] This invention discloses a continuous glycine reactor, comprising a primary reactor and an integrated reactor. The continuous glycine reactor, through the series connection of the primary reactor and the integrated reactor, achieves continuous material flow from feeding and initial mixing to deep reaction, overcoming the interruptions and batch fluctuations inherent in batch operations. The integrated reactor is internally divided into a low-temperature reaction section and a high-temperature reaction section according to the material flow direction, each with its own independently configured thermostatic carrier inlet and outlet, thereby achieving precise zoned control of the reaction temperature. The low-temperature reaction section facilitates control of the main reaction rate and selectivity, while the high-temperature reaction section ensures complete reaction and suppresses byproducts. Through the combined design of continuous feeding and segmented temperature control, while ensuring reaction efficiency and product yield, it completely overcomes the bottlenecks of traditional batch reactors caused by uneven mixing and inefficient temperature control, such as clogging, coking, and discontinuous operation. Attached Figure Description

[0014] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0015] Figure 1 This is a schematic diagram of the structure of the glycine continuous reactor provided by this utility model.

[0016] 101 - Initial reactor, 102 - Integrated reactor, 103 - Hydroxyacetonitrile inlet, 104 - Ammonia inlet, 105 - Discharge port, 106 - Initial mixture inlet, 107 - Reactant outlet, 108 - Insulation jacket, 109 - Heat carrier inlet, 110 - Heat carrier outlet, 111 - Low temperature reaction section, 112 - High temperature reaction section, 113 - Low temperature constant temperature carrier inlet, 114 - Low temperature constant temperature carrier outlet, 115 - High temperature constant temperature carrier inlet, 116 - High temperature constant temperature carrier outlet, 117 - First distribution plate, 118 - Second distribution plate, 119 - Material flow rate control valve, 120 - Temperature sensor. Detailed Implementation

[0017] The embodiments of this utility model are described in detail below. Examples of these embodiments are shown in the accompanying drawings, wherein the same or similar reference numerals denote the same or similar elements or elements having the same or similar functions throughout. The embodiments described below with reference to the accompanying drawings are exemplary and intended to explain this utility model, and should not be construed as limiting this utility model.

[0018] Please see Figure 1 This utility model provides a glycine continuous reactor, which includes a primary reactor 101 and an integrated reactor 102. The primary reactor 101 has a hydroxyacetonitrile inlet 103 and an ammonia inlet 104 on both sides of its front end, and a discharge port 105 at its rear end. The integrated reactor 102 has a primary mixture inlet 106 on the side of its bottom and a reactant outlet 107 on the side of its top. The primary mixture inlet 106 and the discharge port 105 are connected by a pipe. The primary reactor 101 is provided with an insulation jacket 108. The sides of the insulation jacket 108 are respectively provided with a heat carrier inlet 109 and a heat carrier outlet 110. The interior of the integrated reactor 102 is divided into a low-temperature reaction section 111 and a high-temperature reaction section 112 from bottom to top along the material flow direction. The low-temperature reaction section 111 is provided with a low-temperature constant-temperature carrier inlet 113 and a low-temperature constant-temperature carrier outlet 114. The high-temperature reaction section 112 is provided with a high-temperature constant-temperature carrier inlet 115 and a high-temperature constant-temperature carrier outlet 116.

[0019] In this embodiment, the glycine continuous reactor, through the series connection of the primary reactor 101 and the integrated reactor 102, achieves continuous material flow from feeding and initial mixing to deep reaction, overcoming the interruptions and batch fluctuations inherent in batch operations. The integrated reactor 102 is internally divided into a low-temperature reaction section 111 and a high-temperature reaction section 112 according to the material flow direction, each with its own independent thermostatic carrier inlet and outlet, thereby achieving precise zoned control of the reaction temperature: the low-temperature reaction section 111 facilitates control of the main reaction rate and selectivity, while the high-temperature reaction section 112 ensures complete reaction and suppresses byproducts. Through the combined design of continuous feeding and segmented temperature control, while ensuring reaction efficiency and product yield, it completely eliminates the bottlenecks of traditional batch reactors caused by uneven mixing and coarse temperature control, such as clogging, coking, and discontinuous operation.

[0020] Furthermore, the interior of the primary reactor 101 is uniformly provided with a plurality of first distribution plates 117 and a plurality of second distribution plates 118, with the plurality of first distribution plates 117 and the plurality of second distribution plates 118 being arranged alternately.

[0021] In this embodiment, by alternately arranging multiple sets of the first distribution plate 117 and the second distribution plate 118 inside the initial reactor 101, a multi-layered, high-intensity mixing and shearing environment is constructed. This enhances the turbulence and collision between the two materials, hydroxyacetonitrile and ammonia, thereby ensuring a high reaction rate in the initial stage and improving the overall system reaction efficiency and product yield.

[0022] Furthermore, the heat carrier inlet 109 is located on the side of the primary reactor 101 near the ammonia inlet 104, and the heat carrier outlet 110 is located on the end of the primary reactor 101 near the discharge outlet 105.

[0023] Furthermore, the low-temperature carrier inlet 113 is located at the bottom of the low-temperature reaction section 111, and the low-temperature carrier outlet 114 is located on the side of the top of the low-temperature reaction section 111, and on the side of the low-temperature reaction section 111 away from the low-temperature carrier inlet 113.

[0024] Furthermore, the high constant temperature carrier inlet 115 is located on one side of the bottom of the high temperature reaction section 112 and on the side of the high temperature reaction section 112 away from the low constant temperature carrier outlet 114, and the high constant temperature carrier outlet 116 is located at the top of the high temperature reaction section 112 and on the side of the high temperature reaction section 112 away from the high constant temperature carrier inlet 115.

[0025] In this embodiment, in the initial reactor 101, the heat carrier and the material flow in the same direction, establishing a uniform temperature field and providing an optimal and stable starting point for the initial reaction. In the low-temperature reaction section 111 and the high-temperature reaction section 112, the isothermal carrier also contacts the rising material in the same direction from bottom to top. This not only ensures the extreme uniformity of axial and radial temperatures in each reaction section, but also avoids local overheating or reaction blind zones.

[0026] Furthermore, material flow rate control valves 119 are provided at both the hydroxyacetonitrile inlet 103 and the ammonia inlet 104.

[0027] In this embodiment, by setting independent material flow rate control valves 119 at the hydroxyacetonitrile inlet 103 and the ammonia inlet 104 respectively, precise and flexible control of the feeding rate of the two key reaction raw materials is achieved.

[0028] Furthermore, temperature sensors 120 are provided at the insulation jacket 108, the low-temperature reaction section 111, and the high-temperature reaction section 112.

[0029] In this embodiment, by comprehensively installing temperature sensors 120 at key locations in the insulation jacket 108, the low-temperature reaction section 111, and the high-temperature reaction section 112, a real-time temperature monitoring system for the entire reaction process is constructed.

[0030] The above-disclosed embodiments are merely preferred embodiments of the present utility model and should not be construed as limiting the scope of the present utility model. Those skilled in the art can understand that implementing all or part of the above-described embodiments and making equivalent changes in accordance with the claims of the present utility model are still within the scope of the utility model.

Claims

1. A continuous glycine reactor, characterized in that, The reactor includes a primary reactor and an integrated reactor. The primary reactor has a hydroxyacetonitrile inlet and an ammonia inlet on both sides of its front end, and a discharge outlet at its rear end. The integrated reactor has a primary mixture inlet on the side of its bottom and a reactant outlet on the side of its top. The primary mixture inlet and the discharge outlet are connected by a pipeline. The primary reactor is equipped with an insulation jacket on its exterior. The sides of the insulation jacket at both ends are respectively provided with a heat carrier inlet and a heat carrier outlet. The interior of the integrated reactor is divided into a low-temperature reaction section and a high-temperature reaction section from bottom to top along the material flow direction. The low-temperature reaction section is provided with a low-temperature constant-temperature carrier inlet and a low-temperature constant-temperature carrier outlet, and the high-temperature reaction section is provided with a high-temperature constant-temperature carrier inlet and a high-temperature constant-temperature carrier outlet.

2. The glycine continuous reactor as described in claim 1, characterized in that, The interior of the primary reactor is uniformly provided with multiple first distribution plates and multiple second distribution plates, which are arranged alternately.

3. The glycine continuous reactor as described in claim 2, characterized in that, The heat carrier inlet is located on the side of the primary reactor near the ammonia inlet, and the heat carrier outlet is located on the side of the primary reactor near the discharge outlet.

4. The glycine continuous reactor as described in claim 3, characterized in that, The low-temperature carrier inlet is located at the bottom of the low-temperature reaction section, and the low-temperature carrier outlet is located on the side of the top of the low-temperature reaction section, and on the side of the low-temperature reaction section away from the low-temperature carrier inlet.

5. The glycine continuous reactor as described in claim 4, characterized in that, The high constant temperature carrier inlet is located on one side of the bottom of the high temperature reaction section and on the side of the high temperature reaction section away from the low constant temperature carrier outlet. The high constant temperature carrier outlet is located at the top of the high temperature reaction section and on the side of the high temperature reaction section away from the high constant temperature carrier inlet.

6. The glycine continuous reactor as described in claim 5, characterized in that, Both the hydroxyacetonitrile inlet and the ammonia inlet are equipped with material flow rate control valves.

7. The glycine continuous reactor as described in claim 6, characterized in that, Temperature sensors are installed at the insulation jacket, the low-temperature reaction section, and the high-temperature reaction section.

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