Isopropanol separation and purification system
By introducing dehydration units and reflux units in the isopropanol separation process, using membrane dehydration and multi-stage condensation technology, the problems of long processes and high energy consumption in the existing processes are solved, and the separation effect of low energy consumption and environmental protection is achieved.
Patent Information
- Application Number
- CN202420910358.7
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-04-29
- Publication Date
- 2024-12-10
- Estimated Expiration
- 2034-04-29
AI Technical Summary
The existing isopropanol separation process has a long process, high energy consumption, and requires the use of extractive agents, which has environmental protection problems.
A isopropanol separation and purification system including a distillation tower, a dehydration unit and a reflux unit is designed, and dehydration and heat recovery are carried out through a membrane dehydration device and a multi-stage condenser, which simplifies the separation process and reduces energy consumption.
The separation process is simplified and energy consumption is reduced. The isopropanol product with qualified water content is obtained directly from the lower part of the distillation tower, reducing material losses and improving product yield.
Smart Images
Figure CN222138993U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the field of isopropanol preparation, in particular to an isopropanol separation and purification system. Background Art
[0002] Propanol, commonly known as isopropanol, has a wide range of uses as an organic raw material and solvent. At present, the preparation of isopropanol by acetone hydrogenation is the most mainstream preparation method in the industry. The acetone hydrogenation method refers to the exothermic reaction of reducing acetone to isopropanol in a hydrogen atmosphere under the catalysis of homogeneous or heterogeneous catalysts such as Raney nickel, nickel-copper alloy, and inert metals (platinum, palladium, rhodium, ruthenium, iridium). Among them, the crude isopropanol obtained by the hydrogenation reaction usually contains more impurities. This part of the crude isopropanol needs to be separated and purified to obtain an isopropanol product that meets the requirements.
[0003] In the existing isopropanol separation process, distillation tower rough separation, extraction, dehydration and other processes are often used to separate the isopropanol product, so as to obtain an isopropanol product with a qualified water content. However, this method has the disadvantages of long process, high energy consumption, and the need to use an extraction agent, which is not conducive to environmental protection. Utility Model Content
[0004] The utility model aims to provide an isopropanol separation and purification system with low energy consumption, low loss and simple separation process.
[0005] A separation and purification system for isopropanol comprises a distillation tower, a dehydration unit, a reflux unit and a light component discharge unit, wherein the top outlet of the distillation tower is respectively connected to the dehydration unit and the reflux unit, the dehydration unit is connected to the light component discharge unit, and the reflux unit is respectively connected to the distillation tower and the light component discharge unit.
[0006] The above technical scheme relates to an isopropanol separation and purification system, which is used for separating and purifying crude isopropanol generated after the hydrogenation reaction of acetone, and comprises a distillation tower, a dehydration unit, a reflux unit and a light component discharge unit. The hydrogenation reaction product after heat exchange, i.e., crude isopropanol, enters the distillation tower for separation. The top gas phase of the distillation tower is divided into two parts through a pipeline, which go to the dehydration unit and the reflux unit respectively. The dehydration unit can dehydrate the light components at the top of the distillation tower, and the dehydrated light components are sent to the light component discharge unit. A part of the light components going to the reflux unit is returned to the distillation tower as reflux to improve the separation effect in the distillation tower, and the other part goes to the light component discharge unit. The light component discharge unit is connected to the light component collection tank area through a pipeline. The present application provides a dehydration unit and a reflux unit, and divides the light components at the top of the distillation tower into two parts, wherein a part of the light components enters the dehydration unit for dehydration, thereby effectively reducing the water content in the distillation tower, so that the isopropanol product with qualified water content can be directly extracted from the lower measurement line of the distillation tower, and there is no need to dehydrate and separate the extracted isopropanol, the separation process is simple, and the energy consumption during separation is low. The other part of the light components at the top of the distillation tower is condensed and refluxed to the distillation tower through the reflux unit, and the light component exhaust gas is recovered by condensation, which further reduces the material loss during the discharge of the light component exhaust gas and improves the product yield.
[0007] As a further solution of the utility model, the dehydration unit includes a membrane dehydration device, a dehydrated material cooler, a dehydrated material buffer tank and a light component external pump which are connected in sequence, the membrane dehydration device is connected to the top of the distillation tower, and the light component external pump is connected to the light component discharge unit.
[0008] In the above technical scheme, a part of the gas phase at the top of the distillation tower enters the membrane dehydration device through a pipeline. The membrane dehydration device dehydrates the light components entering the top of the tower through the selective separation effect of the membrane material. The dehydrated light components enter the dehydrated material cooler for cooling, and then enter the dehydrated material buffer tank for buffering, and then enter the light component discharge unit, and are sent to the light component collection tank area by the light component discharge unit. The light component discharge unit is also provided with a light component external pump for providing power.
[0009] As a further solution of the utility model, the reflux unit includes at least two condensers and reflux tanks connected in sequence, the first condenser is connected to the top of the distillation tower, and the outlet at the bottom of the reflux tank is connected to the distillation tower and the light component discharge unit through pipelines.
[0010] In the above technical solution, the reflux unit includes at least two condensers and reflux tanks that are arranged and connected in sequence. The condenser can recover part of the heat while condensing. A plurality of condensers that are connected in sequence are arranged to recover the heat in stages, which can effectively recover the heat in the light component and improve the efficiency of heat recovery. Some of the light components at the top of the distillation tower enter the condenser in sequence for condensation, and after cooling through all condensers, enter the reflux tank for gas-liquid separation. The outlet of the reflux tank is connected to the distillation tower and the light component discharge unit through pipelines, respectively. A part of the liquid phase separated in the reflux tank is returned to the distillation tower as reflux through the pipeline, and the other part enters the light component discharge unit to wait for subsequent discharge treatment. The reflux unit is also provided with a reflux pump for providing power.
[0011] As a further solution of the present invention, the reflux unit also includes a non-condensable gas production tank, the outlet at the top of the reflux tank is connected to the inlet of the non-condensable gas production tank through a pipeline, the outlet at the top of the non-condensable gas production tank is connected to the flare through a pipeline, and a pipeline refluxing to the reflux tank is provided at the bottom of the non-condensable gas production tank.
[0012] In the above technical scheme, a reflux tank condenser is provided between the reflux tank and the non-condensable gas production tank. The exhaust gas in the reflux tank is further condensed by the reflux tank condenser and then enters the non-condensable gas production tank. The non-condensable gas production tank can perform gas-liquid separation on this part of the gas, wherein the liquid part flows back to the reflux tank through the bottom pipeline, so as to recover the effective components such as isopropanol therein, and the non-condensable gas part is discharged to the flare through the top pipeline for treatment.
[0013] As a further solution of the present invention, the pipeline connecting the light component ejection pump and the light component discharge unit is provided with a branch connected to the reflux tank.
[0014] In the above technical solution, a branch is provided on the pipeline connecting the light component external pump and the light component discharge unit, and the branch is connected to the reflux tank. A part of the light component after dehydration is returned to the reflux tank as reflux through the branch.
[0015] As a further solution of the present invention, the outlet of the light component discharge unit is connected to the light component collection tank area.
[0016] In the above technical solution, the outlet of the light component discharge unit is connected to the light component collection tank area through a pipeline, and part of the light components are extracted and sent to the light component collection tank area for collection.
[0017] As a further solution of the utility model, a heavy component discharge unit is provided at the bottom of the distillation tower, the heavy component discharge unit is connected to the outlet of the bottom of the distillation tower, and the outlet of the heavy component discharge unit is connected to the heavy component collection tank area.
[0018] In the above technical solution, the bottom outlet of the distillation tower is connected to a heavy component discharge unit, and the heavy component discharge unit is used to transport the heavy components at the bottom of the distillation tower to the heavy component collection tank area for recovery.
[0019] As a further solution of the utility model, a reboiler is provided at the bottom of the distillation tower, and the inlet and outlet of the reboiler are connected to the bottom of the distillation tower.
[0020] In the above technical solution, the distillation tower is connected to a reboiler, the inlet and outlet of the reboiler are connected to the bottom of the distillation tower through a pipeline, and the reboiler provides heat to the material in the distillation tower to ensure the separation efficiency of the distillation tower.
[0021] As a further solution of the utility model, the distillation tower is connected to a feed line, and the feed line includes a feed heater.
[0022] In the above technical solution, the distillation tower is provided with a feed line, which is used to feed the reaction product produced by the acetone hydrogenation reaction, namely crude isopropanol, into the distillation tower for separation and purification. The feed line is provided with a feed heater, which is used to preheat the crude isopropanol entering the distillation tower and increase the inlet temperature of the distillation tower.
[0023] As a further solution of the utility model, the distillation tower is provided with a product extraction line, and the product extraction line is connected to the lower part of the distillation tower.
[0024] In the above technical solution, the distillation tower is connected to a product extraction line, which is connected to the lower part of the distillation tower for extracting the separated isopropyl alcohol product with qualified water content and sending it to the isopropyl alcohol product tank area for collection.
[0025] The utility model has the following beneficial effects:
[0026] An isopropanol product with a qualified water content is obtained, and the separation process is simple and the energy consumption is low. The present application is provided with a dehydration unit and a reflux unit. By dividing the light components at the top of the distillation tower into two parts, one part of which enters the dehydration unit and is dehydrated by a membrane dehydration device, the water content in the distillation tower can be effectively reduced, so that an isopropanol product with a qualified water content can be directly extracted from the lower measurement line of the distillation tower, and there is no need to dehydrate and separate the extracted isopropanol, the separation process is simple, and the separation energy consumption is low.
[0027] The light component extraction loss is low. Another part of the light components at the top of the distillation tower are condensed and refluxed to the distillation tower through the reflux unit. The exhaust gas extracted from the reflux unit is further condensed through the condenser and sent to the non-condensable gas extraction tank for separation. The isopropanol and other components in the non-condensable gas can be recovered, further reducing the material loss in the process of light component non-condensable gas emission and improving the product yield. BRIEF DESCRIPTION OF THE DRAWINGS
[0028] Figure 1 The figure is a schematic diagram of the structure of a system for separating and purifying isopropanol according to an embodiment.
[0029] Description of reference numerals in the figures:
[0030] T1-distillation tower; E1-feed heater; E2-reboiler; F1-dehydrated material cooler; F2-first condenser; F3-second condenser; F4-light component discharge unit; F5-heavy component discharge unit; F6-reflux tank condenser; P1-light component external pump; P2-reflux pump; V1-dehydrated material buffer tank; V2-reflux tank; V3-non-condensable gas production tank; M1-membrane dehydration device. DETAILED DESCRIPTION
[0031] The following will further describe the separation and purification system of isopropanol of the utility model in detail in combination with specific embodiments and drawings. Among them, the drawings are only used for exemplary description, and only schematic diagrams are shown, not physical drawings, and cannot be understood as limitations on this patent; in order to better illustrate the embodiments of the utility model, some parts of the drawings may be omitted, enlarged or reduced, and do not represent the size of the actual product; for those skilled in the art, it is understandable that some well-known structures and their descriptions in the drawings may be omitted.
[0032] Please refer to Figure 1 In a non-limiting embodiment of the utility model, a separation and purification system of isopropanol includes a distillation tower T1, a dehydration unit, a reflux unit and a light component discharge unit F4, wherein the top outlet of the distillation tower T1 is respectively connected to the dehydration unit and the reflux unit, the dehydration unit is connected to the light component discharge unit F4, and the reflux unit is respectively connected to the distillation tower T1 and the light component discharge unit F4. In the present embodiment, a separation and purification system of isopropanol is provided, which is used for separating and purifying crude isopropanol generated after the hydrogenation reaction of acetone, and comprises a distillation tower T1, a dehydration unit, a reflux unit and a light component discharge unit F4. The hydrogenation reaction product after heat exchange, i.e., crude isopropanol, enters the distillation tower T1 for separation. The top gas phase of the distillation tower T1 is divided into two parts through a pipeline, which go to the dehydration unit and the reflux unit respectively. The dehydration unit can dehydrate the light components at the top of the distillation tower T1, and the dehydrated light components are sent to the light component discharge unit F4. A part of the light components going to the reflux unit are returned to the distillation tower T1 as reflux to improve the separation effect in the distillation tower T1, and the other part goes to the light component discharge unit F4. The light component discharge unit F4 is connected to the light component collection tank area through a pipeline to collect the light components.
[0033] In this embodiment, the light components at the top of the distillation tower T1 are divided into two parts by setting up a dehydration unit and a reflux unit, wherein a part of the light components enters the dehydration unit for dehydration, which can effectively reduce the water content in the distillation tower T1, so that the isopropanol product with qualified water content can be directly extracted from the lower measurement line of the distillation tower T1, and there is no need to dehydrate and separate the extracted isopropanol, the separation process is simple, and the energy consumption during separation is low. The other part of the light components at the top of the distillation tower are condensed and refluxed to the distillation tower T1 through the reflux unit, and the light component exhaust gas is recovered by condensation, which further reduces the material loss in the discharge process of the light component exhaust gas and improves the product yield.
[0034] Please refer to Figure 1 In a non-limiting embodiment of the utility model, the dehydration unit includes a membrane dehydration device M1, a dehydration material cooler F1, a dehydration material buffer tank V1 and a light component external pump P1 connected in sequence, the membrane dehydration device M1 is connected to the top of the distillation tower T1, and the light component external pump P1 is connected to the light component discharge unit F4. In this embodiment, a part of the gas phase at the top of the distillation tower T1 enters the membrane dehydration device M1 through a pipeline, and the membrane dehydration device M1 dehydrates the light components entering the top of the tower through the selective separation effect of the membrane material. The dehydrated light components enter the dehydration material cooler F1 for cooling, enter the dehydration material buffer tank V1 for buffering, and then enter the light component discharge unit F4, and are sent to the light component collection tank area for collection by the light component discharge unit F4.
[0035] Specifically, the membrane dehydration device M1 is provided with a recovery line, which is connected to the recovery area and is used to discharge the permeate in the membrane dehydration device M1 and recover it.
[0036] Please refer to Figure 1 In a non-limiting embodiment of the present invention, the reflux unit includes at least two condensers and a reflux tank V2 connected in sequence, the first condenser is connected to the top of the distillation tower T1, and the outlet at the bottom of the reflux tank V2 is connected to the distillation tower T1 and the light component discharge unit F4 through pipelines. In this embodiment, the reflux unit includes at least two condensers and a reflux tank V2 which are arranged and connected in sequence. The condenser can recover part of the heat while condensing. A plurality of condensers which are connected in sequence are arranged to recover the heat in stages, which can effectively recover the heat in the light components and improve the efficiency of heat recovery. Part of the light components at the top of the distillation tower T1 enter the condenser in sequence for condensation, and enter the reflux tank V2 for gas-liquid separation after being cooled by all condensers. The outlet of the reflux tank V2 is respectively connected to the distillation tower T1 and the light component discharge unit F4 through pipelines. A part of the liquid phase separated in the reflux tank V2 is returned to the distillation tower T1 as reflux through the pipeline, and the other part enters the light component discharge unit F4 to wait for subsequent discharge treatment. Specifically, a reflux pump P2 is also provided in the reflux unit for providing power.
[0037] Preferably, two condensers are provided, namely the first condenser F2 and the second condenser F3. The light components at the top of the distillation tower T1 first enter the first condenser F2 to be cooled to 110°C, then enter the second condenser F3 to be cooled to 60°C, and then enter the reflux tank V2 for gas-liquid separation. By recovering heat in stages through two condensers arranged in sequence, the heat recovery rate can be effectively improved and the energy consumption can be reduced.
[0038] Please refer to Figure 1 In a non-limiting embodiment of the utility model, the reflux unit also includes a non-condensable gas production tank V3, the outlet at the top of the reflux tank V2 is connected to the inlet of the non-condensable gas production tank V3 through a pipeline, the outlet of the non-condensable gas production tank V3 is connected to the flare through a pipeline, and a pipeline for reflux to the reflux tank is provided at the bottom of the non-condensable gas production tank. In this embodiment, specifically, a reflux tank condenser F6 is provided between the reflux tank V2 and the non-condensable gas production tank V3, and the exhaust gas in the reflux tank V2 is further condensed by the reflux tank condenser F6 and enters the non-condensable gas production tank V3, and the non-condensable gas production tank V3 can perform gas-liquid separation on this part of the gas, wherein the liquid part flows back to the reflux tank V2 through the pipeline at the bottom of the non-condensable gas production tank V3, thereby recovering effective components such as isopropanol therein, and the non-condensable gas part is discharged to the flare through the pipeline at the top of the reflux tank V2 for treatment.
[0039] Please refer to Figure 1 In a non-limiting embodiment of the utility model, the pipeline connecting the light component external pump P1 and the light component discharge unit F4 is provided with a branch connected to the reflux tank V2. In this embodiment, the pipeline connecting the light component external pump P1 and the light component discharge unit F4 is provided with a branch, which is connected to the reflux tank V2, and a part of the light component after dehydration is returned to the reflux tank V2 as reflux through the branch.
[0040] Please refer to Figure 1 In a non-limiting embodiment of the present invention, the outlet of the light component discharge unit F4 is connected to the light component collection tank area. In this embodiment, the outlet of the light component discharge unit F4 is connected to the light component collection tank area through a pipeline, and part of the light component is produced and sent to the light component collection tank area for collection.
[0041] Please refer to Figure 1In a non-limiting embodiment of the utility model, a heavy component discharge unit F5 is provided at the bottom of the distillation tower T1, and the heavy component discharge unit F5 is connected to the outlet of the bottom of the distillation tower T1, and the outlet of the heavy component discharge unit F5 is connected to the heavy component collection tank area. In this embodiment, the bottom outlet of the distillation tower T1 is connected to the heavy component discharge unit F5, and the heavy component discharge unit F5 is used to transport the heavy components at the bottom of the distillation tower T1 to the heavy component collection tank area for recovery.
[0042] Please refer to Figure 1 In a non-limiting embodiment of the utility model, a reboiler E2 is provided at the bottom of the distillation tower T1, and the inlet and outlet of the reboiler E2 are connected to the bottom of the distillation tower T1. In this embodiment, the distillation tower T1 is connected to the reboiler E2, and the inlet and outlet of the reboiler E2 are connected to the bottom of the distillation tower T1 through a pipeline, and the reboiler E2 provides heat to the material in the distillation tower T1 to ensure the separation efficiency of the distillation tower T1.
[0043] Please refer to Figure 1 In a non-limiting embodiment of the utility model, the distillation tower T1 is connected to a feed line, and the feed line includes a feed heater E1. In this embodiment, the distillation tower T1 is provided with a feed line, and the feed line is used to feed the reaction product produced by the acetone hydrogenation reaction, that is, crude isopropanol, into the distillation tower T1 for separation and purification. The feed line is provided with a feed heater E1, and the feed heater E1 is used to preheat the crude isopropanol entering the distillation tower T1 to increase the inlet temperature of the distillation tower T1.
[0044] Please refer to Figure 1 In a non-limiting embodiment of the utility model, the distillation tower T1 is provided with a product extraction line, and the product extraction line is connected to the lower part of the distillation tower T1. In this embodiment, the distillation tower T1 is connected to a product extraction line, and the product extraction line is connected to the lower part of the distillation tower T1, which is used to extract the separated isopropyl alcohol product with qualified water content and send it to the isopropyl alcohol product tank area for collection.
[0045] In the description of the present invention, it should be understood that terms such as "upper", "lower", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc., indicating orientations or positional relationships, are based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present invention.
[0046] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Thus, the features defined as "first" and "second" may explicitly or implicitly include one or more of the features.
[0047] In the present invention, unless otherwise clearly specified and limited, the terms "install", "connect", "connect", "fix" and the like should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.
[0048] Although the utility model is described in conjunction with the above specific embodiments, it is obvious that those skilled in the art can make many substitutions, modifications and changes based on the above content. Therefore, all such substitutions, improvements and changes are included in the spirit and scope of the appended claims.
Claims
1. A separation and purification system for isopropanol, characterized in that: It includes a distillation tower, a dehydration unit, a reflux unit and a light component discharge unit, wherein the top outlet of the distillation tower is respectively connected to the dehydration unit and the reflux unit, the dehydration unit is connected to the light component discharge unit, and the reflux unit is respectively connected to the distillation tower and the light component discharge unit.
2. The isopropanol separation and purification system according to claim 1, characterized in that: The dehydration unit comprises a membrane dehydration device, a dehydrated material cooler, a dehydrated material buffer tank and a light component external pump which are connected in sequence. The membrane dehydration device is connected to the top of the distillation tower, and the light component external pump is connected to the light component discharge unit.
3. The isopropanol separation and purification system according to claim 2, characterized in that: The reflux unit includes at least two condensers and a reflux tank connected in sequence, the first condenser is connected to the top of the distillation tower, and the outlet at the bottom of the reflux tank is connected to the distillation tower and the light component discharge unit through pipelines.
4. The isopropanol separation and purification system according to claim 3, characterized in that: The reflux unit also includes a non-condensable gas production tank, the outlet at the top of the reflux tank is connected to the inlet of the non-condensable gas production tank through a pipeline, the top outlet of the non-condensable gas production tank is connected to the flare through a pipeline, and a pipeline refluxing to the reflux tank is provided at the bottom of the non-condensable gas production tank.
5. The isopropanol separation and purification system according to claim 4, characterized in that: The pipeline connecting the light component ejection pump and the light component discharge unit is provided with a branch connected to the reflux tank.
6. The isopropanol separation and purification system according to claim 1, characterized in that: The outlet of the light component discharge unit is connected to the light component collection tank area.
7. The isopropanol separation and purification system according to claim 1, characterized in that: A heavy component discharge unit is provided at the bottom of the distillation tower, the heavy component discharge unit is connected to an outlet at the bottom of the distillation tower, and the outlet of the heavy component discharge unit is connected to a heavy component collecting tank area.
8. The isopropanol separation and purification system according to claim 1, characterized in that: A reboiler is provided at the bottom of the distillation tower, and the inlet and outlet of the reboiler are connected to the bottom of the distillation tower.
9. The isopropanol separation and purification system according to claim 1, characterized in that: The distillation tower is connected with a feed line, and the feed line includes a feed heater.
10. The isopropanol separation and purification system according to claim 1, characterized in that: The distillation tower is provided with a product extraction line, and the product extraction line is connected to the lower part of the distillation tower.