Separation and recovery method of olefin hydroformylation reaction liquid

Abstract

The invention relates to the technical field of chemical production, in particular to a separation and recovery method of olefin hydroformylation reaction liquid, which comprises the following steps: step 1, introducing the olefin hydroformylation reaction liquid into an evaporator, and heating to 60-150 DEG C; and 2, conveying the gas and liquid material flows flowing out of the evaporator and synthesis gas composed of hydrogen and carbon monoxide to a gas-liquid separator, and carrying out separation treatment to obtain a gas phase material flow and a liquid phase material flow containing a catalyst. According to the separation and recovery method provided by the invention, the synthesis gas is introduced in the separation process of the reaction liquid, the synthesis gas and the liquid-phase material flow containing the catalyst are simultaneously introduced into the cyclone separator, and the internal structure of the cyclone separator is transformed, so that the synthesis gas is in full contact with the rhodium catalyst, and the rhodium catalyst is protected; the deactivation rate of the rhodium catalyst is reduced, the recycling of most of the rhodium catalyst is realized, and the loss of the rhodium catalyst is greatly reduced.

Description

Technical Field

[0001] This invention relates to the field of chemical production technology, and in particular to a method for separating and recovering olefin hydroformylation reaction liquid. Background Technology

[0002] The hydroformylation of olefins is a reaction that converts olefins, hydrogen, and carbon monoxide into aldehydes. This reaction is of great significance in the chemical industry because aldehydes can be further converted into high-value-added chemicals such as alcohols, acids, and esters, which are widely used in detergents, plasticizers, surfactants, pharmaceuticals, and fragrances. The process of olefin hydroformylation can be summarized as follows: under the action of a transition metal complex catalyst, a hydrogen atom and a formyl group are added to both ends of the double bond of the olefin, respectively, to generate an aldehyde with an additional carbon atom. This reaction is usually carried out in the presence of transition metals such as rhodium and iridium.

[0003] Prior art, such as patent CN107138182B, discloses an apparatus and method for the above-mentioned reaction, describing an apparatus and method for separating a homogeneous catalyst from a feed stream containing a homogeneous catalyst and a separated component, wherein the separated component can be separated therefrom by evaporation. The feed stream is supplied to an evaporation zone, causing the separated component to evaporate. The evaporation zone is configured such that the feed stream has a first residence time in the evaporation zone. The evaporated separated component is then fed directly to a vapor-liquid separator including a cooling device, where the liquid containing the homogeneous catalyst is collected. The vapor-liquid separator allows a residence time of approximately 10 seconds to approximately 60 minutes. The volume of the liquid containing the homogeneous catalyst is maintained at a level where the cooling device is substantially immersed in the liquid containing the homogeneous catalyst. In the above reaction, the reaction liquid is a liquid containing butyraldehyde and a rhodium catalyst, with the rhodium catalyst dissolved in the heavy component organic solvent. By heating the reaction liquid in the evaporator, the butyraldehyde is vaporized into a gas. The butyraldehyde gas and the rhodium catalyst enter the gas-liquid separator together. The butyraldehyde gas is discharged from the top, and the cooled rhodium catalyst is discharged from the bottom and returned to the reaction vessel. However, the high temperature will accelerate the deactivation rate of the rhodium catalyst. Cooling pipes are installed in the gas-liquid separator to cool the rhodium catalyst, but this will still cause the loss of the rhodium catalyst.

[0004] Meanwhile, based on existing theories of metal complex catalysis, the active species of the rhodium catalyst used in the hydroformylation reaction of olefins is a rhodium-hydrogen complex containing ligands and carbon monoxide. This species is gradually destroyed and deactivated during the high-temperature evaporation process. In fact, additional rhodium catalysts are required to maintain the normal operation of the equipment in industrial production.

[0005] Therefore, whether a separation and recovery device for olefin hydroformylation catalyst can be provided based on the shortcomings of existing technology, so as to realize the protection and recovery of rhodium catalyst and reduce the risk of loss and deactivation of rhodium catalyst during the reaction process, has become a technical problem that urgently needs to be solved by those skilled in the art. Summary of the Invention

[0006] This invention provides a method for separating and recovering olefin hydroformylation reaction solution, which solves the problems of rhodium catalyst loss and catalyst deactivation in the prior art.

[0007] A method for separating and recovering an olefin hydroformylation reaction solution includes the following steps:

[0008] Step 1: Introduce the olefin hydroformylation reaction solution into the evaporator and heat it to 60-150°C. Those skilled in the art can select the appropriate temperature based on production output, production scale, production equipment, etc. This selection does not require any creative effort. For example, 60°C, 70°C, 80°C, 90°C, 100°C, 110°C, 120°C, 130°C, 140°C, or 150°C can be selected.

[0009] Step 2: The gas and liquid streams flowing out of the evaporator, together with the synthesis gas composed of hydrogen and carbon monoxide, are transported to a gas-liquid separator for separation to obtain a gas phase stream and a liquid phase stream containing the catalyst.

[0010] Furthermore, the gas-liquid separator in step 2 is a cyclone separator.

[0011] Furthermore, it also includes step 3: taking the gaseous stream separated in step 2 and conveying it to a demister. The demister is equipped with a cooling device. The gas is separated by demistering and cooling to obtain a gaseous stream and a liquid stream containing a catalyst. The gaseous stream and a liquid stream containing trace amounts of catalyst are then separated.

[0012] Furthermore, it also includes step 4: taking the gaseous stream separated in step 3 and processing it through a cooler and a gas-liquid separator to separate syngas and aldehydes.

[0013] Furthermore, in steps 2 and 3, the separated liquid stream containing the catalyst and the liquid stream containing trace amounts of catalyst are both recycled and transported back to the reactor for continued use.

[0014] Furthermore, in step 4, the separated syngas is compressed and then transported to the reactor.

[0015] Furthermore, in step 2, the gas and liquid streams and the synthesis gas enter the cone through the inlet pipe of the cyclone separator and rotate. The gaseous stream is separated into a liquid stream containing the catalyst under the cooling effect of the cooling pipe on the outer wall of the cyclone separator and discharged from the bottom of the cyclone separator. The gaseous stream is discharged from the top of the cyclone separator.

[0016] Furthermore, the inner wall of the cyclone separator cone is spirally provided with a liquid guide channel, and the liquid phase material is discharged from the bottom along the liquid guide channel under the action of the rotation of the cyclone separator.

[0017] Furthermore, an overflow weir is provided on the inner wall of the inlet channel of the cyclone separator, and a liquid outlet is provided on the overflow weir. The liquid phase material discharged from the evaporator flows into the overflow weir through the inlet channel and flows downward along the inner wall of the cone through the liquid outlet.

[0018] Furthermore, within the cyclone separator, the trajectory of the liquid phase containing the catalyst during the separation process is the same as the trajectory of the gas within the cyclone separator.

[0019] Furthermore, the molar ratio of hydrogen to carbon monoxide in the synthesis gas is 1.0 to 2.0.

[0020] More preferably, the molar ratio of hydrogen to carbon monoxide in the syngas is 1.01 to 1.1. Under these conditions, the syngas utilization rate can be further improved, while also being more conducive to the protection of the rhodium catalyst.

[0021] Furthermore, the flow rate of the synthesis gas is 0.001 to 0.1 molar amount of the liquid stream in the olefin hydroformylation reaction.

[0022] More preferably, the flow rate of the syngas is 0.005 to 0.05 of the molar amount of the liquid stream in the olefin hydroformylation reaction. Under these conditions, the separation efficiency can be further improved while reducing catalyst loss.

[0023] One or more technical solutions provided in the embodiments of this application have at least the following technical effects or advantages:

[0024] 1. The present invention provides a method for separating and recovering olefin hydroformylation reaction liquid. In the separation process of the reaction liquid, syngas is introduced and the syngas and the liquid phase containing the catalyst are simultaneously passed into a cyclone separator. By modifying the internal structure of the cyclone separator, the syngas and the rhodium catalyst are fully contacted, which protects the rhodium catalyst, reduces the deactivation rate of the rhodium catalyst, and realizes the recovery and recycling of the rhodium catalyst. The amount of rhodium catalyst carried away by the crude aldehyde is only 18 ppb, which greatly reduces the loss of rhodium catalyst.

[0025] 2. The present invention provides a method for separating and recovering olefin hydroformylation reaction liquid, which allows the reaction liquid and syngas to pass sequentially through a cyclone separator, a demister, a cooler, and a gas-liquid separator, avoiding the risk of rhodium catalyst deactivation due to high temperature, achieving high-quality recovery of rhodium catalyst, and recovering the introduced syngas to the reactor for continued use, resulting in a higher aldehyde yield in the final separation. Attached Figure Description

[0026] Figure 1 This is a flowchart illustrating a method for separating and recovering an olefin hydroformylation reaction solution according to an embodiment of this application.

[0027] Figure 2 This is a schematic diagram of the cyclone separator structure according to an embodiment of this application.

[0028] Attached diagram descriptions: 1. Evaporator; 2. Cyclone separator; 3. Demister; 4. Cooler; 5. Gas-liquid separator; 6. Liquid guide channel; 7. Overflow weir; 8. Cooling pipe. Detailed Implementation

[0029] The technical solution of the present invention will be clearly and completely described below with reference to specific embodiments. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0030] Example 1:

[0031] A method for separating and recovering an olefin hydroformylation reaction solution, such as... Figure 1 and Figure 2 As shown, it includes the following steps:

[0032] Step 1: Introduce the olefin hydroformylation reaction solution into evaporator 1 and heat it to 60°C;

[0033] Step 2: The gas and liquid streams flowing out of the evaporator 1, together with the synthesis gas composed of hydrogen and carbon monoxide, are fed to a gas-liquid separator. The molar ratio of hydrogen to carbon monoxide in the synthesis gas is 1:1, and the flow rate of the synthesis gas is 0.001 of the molar amount of the liquid stream in the olefin hydroformylation reaction. The separation process yields a gaseous stream and a liquid stream containing the catalyst. The liquid stream containing the catalyst is recycled back to the reactor for continued use.

[0034] Step 3: The gaseous stream separated in Step 2 is transported to the demister 3. The demister 3 is equipped with a cooling device. After demisting and cooling, the gas is separated into a gaseous stream and a liquid stream containing trace amounts of catalyst. The gaseous stream includes butyraldehyde and synthesis gas. The liquid stream containing trace amounts of catalyst is recovered into the reactor for continued use.

[0035] Step 4: The gaseous stream separated in Step 3 is processed by Cooler 4 and Gas-Liquid Separator 5 to separate syngas and butyraldehyde.

[0036] The rhodium content in butyraldehyde was found to be 20 ppb (graphite furnace atomic absorption spectrometry, A3), the rhodium catalyst recovery rate was 99.98%, and the butyraldehyde yield was 98%.

[0037] Example 2:

[0038] A method for separating and recovering an olefin hydroformylation reaction solution, such as... Figure 1 and Figure 2 As shown, it includes the following steps:

[0039] Step 1: Introduce the olefin hydroformylation reaction solution into evaporator 1 and heat it to 120°C;

[0040] Step 2: The gas and liquid streams flowing out of the evaporator 1, together with the synthesis gas composed of hydrogen and carbon monoxide, are transported to the cyclone separator 2. The molar ratio of hydrogen to carbon monoxide in the synthesis gas is 2:1. The flow rate of the synthesis gas is 0.08 of the molar amount of the liquid stream in the olefin hydroformylation reaction. An overflow weir 7 is provided on the inner wall of the inlet channel of the cyclone separator 2. An outlet is opened on the overflow weir 7. The liquid stream flows into the overflow weir 7 through the inlet channel and flows downward along the inner wall of the cone through the outlet. Under the action of the rotation of the cyclone separator 2, it is discharged from the bottom along the liquid guide channel 6. The gas stream is separated into a liquid stream containing catalyst under the cooling action of the cooling pipe 8 on the outer wall of the cyclone separator 2 and discharged from the bottom of the cyclone separator 2 along the liquid guide channel 6 for recycling back to the reactor for continued use. The gas stream is discharged from the top of the cyclone separator 2.

[0041] Step 3: The gaseous stream separated in Step 2 is transported to the demister 3. The demister 3 is equipped with a cooling device. After demisting and cooling, the gas is separated into a gaseous stream and a liquid stream containing trace amounts of catalyst. The gaseous stream includes heptanal and synthesis gas. The liquid stream containing trace amounts of catalyst is recovered into the reactor for continued use.

[0042] Step 4: The gaseous stream separated in Step 3 is processed by Cooler 4 and Gas-Liquid Separator 5 to separate syngas and heptanal.

[0043] The rhodium content in heptanal was found to be 18 ppb (graphite furnace atomic absorption spectrometry, A3), the rhodium catalyst recovery rate was 99.9998%, and the yield of heptanal was 99%.

[0044] Example 3:

[0045] A method for separating and recovering an olefin hydroformylation reaction solution, such as... Figure 1 and Figure 2 As shown, it includes the following steps:

[0046] Step 1: Introduce the reaction solution obtained from the olefin hydroformylation unit into evaporator 1 and heat it to 110°C;

[0047] Step 2: The gas and liquid streams flowing out of the evaporator 1, together with the synthesis gas composed of hydrogen and carbon monoxide, are transported to the cyclone separator 2. The molar ratio of hydrogen to carbon monoxide in the synthesis gas is 1.01:1, and the flow rate of the synthesis gas is 0.001 of the molar amount of the liquid stream in the olefin hydroformylation reaction. An overflow weir 7 is provided on the inner wall of the inlet channel of the cyclone separator 2, and a liquid outlet is opened on the overflow weir 7. The liquid stream flows into the overflow weir 7 through the inlet channel and flows downward along the inner wall of the cone through the liquid outlet. Under the action of the rotation of the cyclone separator 2, it is discharged from the bottom along the liquid guide channel 6. The gas stream is separated into a liquid stream containing catalyst under the cooling action of the cooling pipe 8 on the outer wall of the cyclone separator 2 and discharged from the bottom of the cyclone separator 2 along the liquid guide channel 6 for recycling back to the reactor for continued use. The gas stream is discharged from the top of the cyclone separator 2.

[0048] Step 3: Take the gaseous stream separated in Step 2. The gaseous stream is discharged from the top of the cyclone separator 2 and transported to the demister 3. The demister 3 is equipped with a cooling device. The gas is separated by demisting and cooling to obtain a gaseous stream and a liquid stream containing trace amounts of catalyst. The gaseous stream includes butyraldehyde and synthesis gas. The liquid stream containing trace amounts of catalyst is recovered into the reactor for continued use.

[0049] Step 4: The gaseous stream separated in Step 2 is processed by Cooler 4 and Gas-Liquid Separator 5 to separate syngas and butyraldehyde.

[0050] The rhodium content in butyraldehyde was 17 ppb (graphite furnace atomic absorption spectrometry, A3), the rhodium catalyst recovery rate was 99.9998%, and the butyraldehyde yield was 99%.

[0051] Example 4:

[0052] A method for separating and recovering an olefin hydroformylation reaction solution, such as... Figure 1 and Figure 2 As shown, it includes the following steps:

[0053] Step 1: Introduce the reaction solution obtained from the olefin hydroformylation unit into evaporator 1 and heat it to 100°C;

[0054] Step 2: The gas and liquid streams flowing out of the evaporator 1, together with the synthesis gas composed of hydrogen and carbon monoxide, are transported to the cyclone separator 2. The molar ratio of hydrogen to carbon monoxide in the synthesis gas is 1.1:1. The flow rate of the synthesis gas is 0.05 of the molar amount of the liquid stream in the olefin hydroformylation reaction. An overflow weir 7 is provided on the inner wall of the inlet channel of the cyclone separator 2. An outlet is opened on the overflow weir 7. The liquid stream flows into the overflow weir 7 through the inlet channel and flows downward along the inner wall of the cone through the outlet. Under the action of the rotation of the cyclone separator 2, it is discharged from the bottom along the liquid guide channel 6. The gas stream is separated into a liquid stream containing catalyst under the cooling action of the cooling pipe 8 on the outer wall of the cyclone separator 2 and discharged from the bottom of the cyclone separator 2 along the liquid guide channel 6 for recycling back to the reactor for continued use. The gas stream is discharged from the top of the cyclone separator 2.

[0055] Step 3: Take the gaseous stream separated in Step 2. The gaseous stream is discharged from the top of the cyclone separator 2 and transported to the demister 3. The demister 3 is equipped with a cooling device. The gas is separated by demisting and cooling to obtain a gaseous stream and a liquid stream containing trace amounts of catalyst. The gaseous stream includes pentanal and synthesis gas. The liquid stream containing trace amounts of catalyst is recovered into the reactor for continued use.

[0056] Step 4: The gaseous stream separated in Step 2 is processed by Cooler 4 and Gas-Liquid Separator 5 to separate syngas and pentanal.

[0057] The rhodium content in pentanal was found to be 16 ppb (graphite furnace atomic absorption spectrometry, A3), the rhodium catalyst recovery rate was 99.9998%, and the pentanal yield was 99%.

[0058] Example 5:

[0059] A method for separating and recovering an olefin hydroformylation reaction solution, such as... Figure 1 and Figure 2 As shown, it includes the following steps:

[0060] Step 1: Introduce the reaction solution obtained from the olefin hydroformylation unit into evaporator 1 and heat it to 70°C;

[0061] Step 2: The gas and liquid streams flowing out of the evaporator 1, together with the synthesis gas composed of hydrogen and carbon monoxide, are transported to the cyclone separator 2. The molar ratio of hydrogen to carbon monoxide in the synthesis gas is 1.06:1, and the flow rate of the synthesis gas is 0.04 of the molar amount of the liquid stream in the olefin hydroformylation reaction. An overflow weir 7 is provided on the inner wall of the inlet channel of the cyclone separator 2, and a liquid outlet is opened on the overflow weir 7. The liquid phase stream flows into the overflow weir 7 through the inlet channel and flows down the inner wall of the cone through the liquid outlet. Under the action of the rotation of the cyclone separator 2, the gaseous material is discharged from the bottom along the liquid guide channel 6. Inside the cyclone separator 2, the gaseous material is separated into a liquid material containing the catalyst under the cooling action of the cooling pipe 8 on the outer wall of the cyclone separator 2 and discharged from the bottom of the cyclone separator 2 along the liquid guide channel 6 and recycled to the reactor for continued use. The gaseous material is discharged from the top of the cyclone separator 2. The movement trajectory of the liquid material containing the catalyst during the separation process is the same as the movement trajectory of the gas inside the cyclone separator 2.

[0062] Step 3: Take the gaseous stream separated in Step 2. The gaseous stream is discharged from the top of the cyclone separator 2 and transported to the demister 3. The demister 3 is equipped with a cooling device. The gas is separated by demisting and cooling to obtain a gaseous stream and a liquid stream containing trace amounts of catalyst. The gaseous stream includes pentanal and synthesis gas. The liquid stream containing trace amounts of catalyst is recovered into the reactor for continued use.

[0063] Step 4: The gaseous stream separated in Step 2 is processed by Cooler 4 and Gas-Liquid Separator 5 to separate syngas and pentanal.

[0064] The rhodium content in pentanal was found to be 16 ppb (graphite furnace atomic absorption spectrometry, A3), the rhodium catalyst recovery rate was 99.9998%, and the pentanal yield was 99%.

[0065] Example 6:

[0066] A method for separating and recovering an olefin hydroformylation reaction solution, such as... Figure 1 and Figure 2 As shown, it includes the following steps:

[0067] Step 1: Introduce the reaction solution obtained from the olefin hydroformylation unit into evaporator 1 and heat it to 150°C;

[0068] Step 2: The gas and liquid streams flowing out of the evaporator 1, together with the synthesis gas composed of hydrogen and carbon monoxide, are transported to the cyclone separator 2. The molar ratio of hydrogen to carbon monoxide in the synthesis gas is 1.5:1. The flow rate of the synthesis gas is 0.1 times the molar amount of the liquid stream in the olefin hydroformylation reaction. An overflow weir 7 is provided on the inner wall of the inlet channel of the cyclone separator 2. An outlet is opened on the overflow weir 7. The liquid stream flows into the overflow weir 7 through the inlet channel and flows downward along the inner wall of the cone through the outlet. Under the action of the rotation of the cyclone separator 2, it is discharged from the bottom along the liquid guide channel 6. In the cyclone separator 2, the gas stream is separated into a liquid stream containing the catalyst under the cooling action of the cooling pipe 8 on the outer wall of the cyclone separator 2 and discharged from the bottom of the cyclone separator 2 along the liquid guide channel 6 and recycled to the reactor for continued use. The gas stream is discharged from the top of the cyclone separator 2.

[0069] Step 3: Take the gaseous stream separated in Step 2. The gaseous stream is discharged from the top of the cyclone separator 2 and transported to the demister 3. The demister 3 is equipped with a cooling device. The gas is separated by demisting and cooling to obtain a gaseous stream and a liquid stream containing trace amounts of catalyst. The gaseous stream includes nonanal and synthesis gas. The liquid stream containing trace amounts of catalyst is recovered to the reactor for continued use.

[0070] Step 4: The gaseous stream separated in Step 2 is processed by Cooler 4 and Gas-Liquid Separator 5 to separate syngas and nonanal.

[0071] The nonanal was found to contain 18 ppb of rhodium (graphite furnace atomic absorption spectrometry, A3), with a rhodium catalyst recovery rate of 99.9998% and a nonanal yield of 99%.

[0072] The present invention provides a method for separating and recovering olefin hydroformylation reaction liquid. In the separation process of the reaction liquid, syngas is introduced and the syngas and the liquid phase containing the catalyst are simultaneously fed into a cyclone separator 2. By modifying the internal structure of the cyclone separator 2, the syngas and the rhodium catalyst are fully contacted, which protects the rhodium catalyst, reduces the deactivation rate of the rhodium catalyst, and enables the recovery and reuse of most of the rhodium catalyst. The recovery rate of the rhodium catalyst is tested to reach 99.9998%, which greatly reduces the loss of rhodium catalyst.

[0073] Although preferred embodiments of the invention have been described, those skilled in the art, upon learning the basic inventive concept, can make other changes and modifications to these embodiments. Therefore, the appended claims are intended to be interpreted as including both the preferred embodiments and all changes and modifications falling within the scope of the invention.

[0074] Obviously, those skilled in the art can make various modifications and variations to this invention without departing from its spirit and scope. Therefore, if these modifications and variations fall within the scope of the claims of this invention and their equivalents, this invention also intends to include these modifications and variations.

Claims

1. A method for separating and recovering an olefin hydroformylation reaction solution, characterized in that: Includes the following steps: Step 1: Introduce the olefin hydroformylation reaction solution into the evaporator and heat it to 60-150°C; Step 2: The gas and liquid streams flowing out of the evaporator, together with the synthesis gas composed of hydrogen and carbon monoxide, are transported to a gas-liquid separator for separation to obtain gaseous and liquid streams.

2. The method for separating and recovering the olefin hydroformylation reaction solution according to claim 1, characterized in that: The gas-liquid separator in step 2 is a cyclone separator.

3. The method for separating and recovering the olefin hydroformylation reaction solution according to claim 1 or 2, characterized in that: It also includes step 3: taking the gaseous stream separated in step 2 and transporting it to a demister, which is equipped with a cooling device, to perform separation treatment to obtain gaseous stream and liquid stream.

4. The method for separating and recovering the olefin hydroformylation reaction solution according to claim 3, characterized in that: It also includes step 4: taking the gaseous stream separated in step 3 and introducing it into a cooler, cooling it, and then introducing it into a gas-liquid separator for processing to separate syngas and aldehydes.

5. The method for separating and recovering the olefin hydroformylation reaction solution according to claim 2, characterized in that: In step 2, the gas and liquid streams and the synthesis gas enter the cone through the inlet pipe of the cyclone separator and rotate. The gas stream is separated into a liquid stream containing the catalyst under the cooling effect of the cooling pipe on the outer wall of the cyclone separator and discharged from the bottom of the cyclone separator. The gas stream is discharged from the top of the cyclone separator.

6. The method for separating and recovering the olefin hydroformylation reaction solution according to claim 5, characterized in that: The inner wall of the cyclone separator cone is spirally surrounded by a liquid guide channel, and the liquid phase material is discharged from the bottom along the liquid guide channel under the action of the rotation of the cyclone separator.

7. The method for separating and recovering the olefin hydroformylation reaction solution according to claim 5 or 6, characterized in that: An overflow weir is provided on the inner wall of the inlet channel of the cyclone separator, and a liquid outlet is provided on the overflow weir. The liquid phase material discharged from the evaporator flows into the overflow weir through the inlet channel and flows downward along the inner wall of the cone through the liquid outlet.

8. The method for separating and recovering the olefin hydroformylation reaction solution according to claim 5, characterized in that: Inside the cyclone separator, the trajectory of the liquid phase containing the catalyst during the separation process is the same as that of the gas within the cyclone separator.

9. The method for separating and recovering the olefin hydroformylation reaction solution according to claim 1, characterized in that: The molar ratio of hydrogen to carbon monoxide in the synthesis gas is 1.0 to 2.

0.

10. The method for separating and recovering the olefin hydroformylation reaction solution according to claim 1, characterized in that: The flow rate of the synthesis gas is 0.001 to 0.1 of the molar amount of the liquid stream in the olefin hydroformylation reaction.

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