Olefin hydroformylation homogeneous catalysis continuous reaction process and system

Abstract

The invention relates to an olefin hydroformylation homogeneous catalysis continuous reaction process and system. The process comprises the following steps: mixing raw materials olefin, synthesis gas and a metal catalyst, and then carrying out hydroformylation reaction; removing a light component containing the product aldehyde from the hydroformylation reaction liquid to obtain a heavy component containing the metal catalyst; uniformly mixing the heavy component with a first extraction agent, and performing phase splitting to obtain a first heavy component phase and a first extraction agent phase; a metal catalyst and a second extraction agent are separated from the first extraction agent phase, the metal catalyst is circularly used for the hydroformylation reaction, and the second extraction agent is used as the first extraction agent mixed with the heavy components. Based on the characteristics of solubility difference and specific gravity difference between the metal catalyst and other substances in the heavy components under specific conditions, the heavy components in a reaction system are reacted at a lower temperature on the premise of not additionally adding a reagent which can influence the activity of the catalyst, and the activity of the catalyst can be well maintained within a longer reaction time.

Description

Technical Field

[0001] The present invention relates to the technical field of hydroformylation reaction, and in particular to a homogeneous catalytic continuous reaction process and system for olefin hydroformylation. Background Art

[0002] Hydroformylation is one of the classic reactions for producing aldehydes in the current chemical industry. It is the addition reaction of olefins with synthesis gas composed of hydrogen and carbon monoxide under specific temperature, pressure and catalyst-assisted conditions to produce aldehyde products with a carbon number increased by one. The latter is an important raw material and intermediate for the preparation of various fine chemicals.

[0003] Homogeneous catalytic reactions for higher olefins with more than 5 carbon atoms have attracted widespread attention due to their high reactivity and production efficiency. In homogeneous catalytic systems, the higher aldehydes obtained from the reaction of higher olefins readily condense to form condensates such as dimers and trimers. These condensates have high boiling points and are difficult to separate from the reaction system by heating and evaporation. As the continuous reaction time increases, a large amount of condensates remain in the reaction system as heavy components, seriously affecting the subsequent recovery and processing of the metal catalyst and inhibiting the catalytic activity of the catalyst, resulting in a decrease in the conversion rate and aldehyde yield of the hydroformylation reaction.

[0004] In order to reduce the condensate content in the continuous reaction system. Patent CN114127040B proposes to separate the heavy components by a two-stage high-temperature high-vacuum falling film method, but the high temperature will affect the life of the catalyst and will also produce more heavy components. Patent CN1138742C stabilizes aliphatic aldehydes by adding alkali metal hydroxides, alkaline earth metal hydroxides, alkali metal carbonates, alkaline earth metal carbonates or alkaline earth metal carboxylates to prevent aldehyde self-condensation, but the addition of such stabilizers will inevitably cause base-catalyzed aldol condensation. In addition, patent CN114773172 B proposes adding acid to decompose the heavy components produced by the hydroformylation reaction, but the process involves neutralization with alkaline solution after adding acid, especially the phosphite ligand is easily decomposed under the action of acid, so this method has the risk of catalyst deactivation.

[0005] Therefore, it is necessary to design the existing continuous reaction process and system to reduce the content of heavy components remaining in the reaction system as the continuous reaction time increases, and to improve the conversion rate and aldehyde formation rate of the hydroformylation reaction. Summary of the Invention

[0006] An object of the present invention is to provide a homogeneous catalytic continuous reaction process for olefin hydroformylation. In this process, after a hydroformylation reaction is continuously carried out for a period of time, a heavy component containing a metal catalyst is separated from the hydroformylation reaction liquid obtained by the reaction. Then, by utilizing the difference in solubility between the metal catalyst and other heavy components such as condensates in the heavy component under specific conditions, the metal catalyst is extracted from the heavy component for recycling, and the remaining heavy components are discharged. This significantly reduces the accumulation of heavy components such as condensates in the continuous reaction system, effectively improves the conversion rate of the industrial hydroformylation continuous reaction, and reduces the reaction cost.

[0007] The above-mentioned purpose of the present invention is achieved through the following technical solutions:

[0008] A homogeneous catalytic continuous reaction process for olefin hydroformylation comprises the following steps:

[0009] The raw material olefin, synthesis gas and metal catalyst are mixed and subjected to hydroformylation reaction to obtain a hydroformylation reaction liquid;

[0010] removing light components including product aldehyde from the hydroformylation reaction liquid to obtain heavy components including the metal catalyst;

[0011] The heavy component and the first extractant are mixed uniformly, and phase separation is performed to obtain a first heavy component phase and a first extractant phase;

[0012] A metal catalyst and a second extractant are separated from the first extractant phase. The metal catalyst is recycled for the hydroformylation reaction, and the second extractant is used as the first extractant mixed with the heavy component.

[0013] In this technical solution, the raw olefins, synthesis gas, and metal catalysts are subjected to a continuous hydroformylation reaction. The raw olefins can be internal olefins, terminal olefins, or branched olefins from C5 to C14; the synthesis gas is a gas in which CO and H2 are mixed in a certain volume ratio; and the metal catalyst preferably uses an oil-soluble rhodium catalyst, such as rhodium pike, acetylacetonato carbonyl rhodium, etc. In some preferred embodiments, the catalytic system also uses an oil-soluble phosphorus ligand, such as triphenylphosphine, phosphite, and phosphoramidite-type oil-soluble phosphine ligand. In one or more embodiments, the metal catalyst and phosphorus ligand can also use any existing oil-soluble rhodium metal catalyst and oil-soluble phosphorus ligand.

[0014] In this technical solution, the hydroformylation reaction liquid obtained after the hydroformylation reaction is completed contains light components and heavy components. The light components primarily include olefins, alkanes, and fatty aldehydes, while the heavy components primarily include the metal catalyst and heavy condensation products such as dimers and trimers of the fatty aldehydes. For example, if the product aldehyde in the light components is tetradecanal, the heavy components will contain, in addition to the metal catalyst, heavy condensation products such as dimers and trimers of tetradecanal. The light components, such as olefins, alkanes, and fatty aldehydes, can be removed from the hydroformylation reaction liquid through evaporation, stripping, or other methods to obtain the heavy components containing the metal catalyst.

[0015] In this technical solution, the metal catalyst is extracted using a first extractant, leveraging the solubility differences between the metal catalyst and other condensed heavy components in the heavy fraction under specific conditions. After extraction, the mixture is allowed to stand, cooled, and separated into phases. The upper first heavy fraction phase is a weakly polar phase containing residual heavy fraction liquid, while the lower first extractant phase is a polar phase containing the majority of the metal catalyst. Next, a second extractant is separated from the first extractant phase through evaporation, stripping, or other methods, leaving a high concentration of metal catalyst, representing the majority of the metal catalyst in the heavy fraction.

[0016] In this technical solution, the separated metal catalyst is recycled to the hydroformylation reaction system for continued use, and the second extractant is also recycled and used as the first extractant to circulate and extract the heavy components, effectively reducing the production cost of the continuous process. Furthermore, more importantly, the first heavy component phase is immediately transferred to a heavy component residual liquid tank for collection after separation, thereby significantly reducing the content of condensates in the continuous reaction system and reducing the impact of accumulated condensates on the activity of the metal catalyst, thereby improving the reaction conversion rate. Furthermore, by utilizing the difference in solubility between the metal catalyst and the condensate to separate heavy components such as the condensate, the heavy components in the reaction system can be reacted at a lower temperature without the addition of additional reagents that would affect the catalyst activity. This helps to maintain the catalyst activity over a longer reaction time, further reducing costs and improving reaction efficiency.

[0017] As a preferred embodiment of the first extractant in the present invention, the first extractant is composed of extractant A and extractant B, wherein the extractant A is N,N-dimethylformamide or formamide, and the extractant B is N-methylpyrrolidone.

[0018] In this technical solution, the first extractant is a combination of extractant A and extractant B, wherein extractant A is DMF or formamide, and extractant B is NMP. This combination of two polar compounds effectively exploits the solubility difference between the metal catalyst and the condensate, extracting the majority of the catalyst from the heavy components. In some embodiments, the ratio of extractant A to extractant B can be 100:1 to 1:100.

[0019] Furthermore, the volume ratio of extractant A to extractant B in the first extractant is 1.2~20; after the second extractant is separated, extractant A and / or extractant B are added so that the volume ratio of extractant A to extractant B in the second extractant is the same as the volume ratio of extractant A to extractant B in the first extractant.

[0020] In this technical solution, through the continuous hydroformylation reaction, it was found that during the second time period T2 of the continuous reaction, the amount of extractant A should be greater than the amount of extractant B. In a preferred embodiment, when the volume ratio of extractant A to extractant B is 1.2 to 20, the total recovery rate of the metal catalyst can be maintained at above 90%. Further preferably, the volume ratio of extractant A to extractant B is 95:5 to 55:45. Even more preferably, extractant A is DMF, extractant B is NMP, and the volume ratio of DMF to NMP is 95:5.

[0021] In this technical solution, within the second time period T2, before the second extractant is mixed with the heavy component or the first heavy component, extractant A and / or extractant B are added to the second extractant to maintain the same composition and ratio as the first extractant. In some embodiments, the second time period T2 can be adjusted based on the accumulated heavy component content in the system. In one or more embodiments, the second time period T2 is 400-550 hours.

[0022] Furthermore, after a certain reaction time, extractant A and / or extractant B are added to the separated second extractant, so that the volume ratio of extractant B to extractant A in the second extractant is 1-1.1.

[0023] In the present technical solution, although most of the condensate heavy components in the continuous reaction system can be discharged through one or two extractions, as the continuous reaction time increases, the heavy components in the continuous reaction system and the amount of polymer in the heavy components will also increase to a certain extent, resulting in an increase in the density of the heavy component phase in the upper layer, thereby making it more difficult to separate the extractant phase and the heavy component phase due to the reduction in density difference. Ultimately, after a longer continuous reaction time, the heavy components are difficult to separate and the recovery rate of the metal catalyst is reduced.

[0024] To address this issue, in the present technical solution, after a certain period of continuous reaction time, for example, greater than or equal to 500 hours, extractant A and / or extractant B are added to the second extractant, so that the volume of extractant B is equal to or slightly greater than that of extractant A. This differs from the continuous reaction before the second time T2, where a larger amount of extractant A is used. By increasing the proportion of extractant B, the specific gravity of the lower extractant phase during phase separation is increased, thereby facilitating the separation of the first extractant phase and the first heavy component phase, as well as the separation of the heavy component residual liquid and the second extractant phase. This allows for the maintenance of a high metal catalyst recovery rate and heavy component removal efficiency even after a long period of continuous reaction.

[0025] By utilizing this solubility difference, the metal catalyst can be separated from the heavy components at a lower temperature without introducing additional reagents, thereby eliminating the first heavy component phase from the continuous reaction system and recycling most of the metal catalyst. For example, 85% of the metal catalyst can be recovered and reused. However, a small amount of the metal catalyst still remains in the first heavy component phase.

[0026] If a small portion of the metal catalyst can be recovered from the first heavy component phase, the recovery rate of the metal catalyst can be increased, further reducing the reaction cost of the continuous reaction process. To this end, a preferred embodiment of the continuous reaction process of the present invention further includes the following steps: uniformly mixing the separated second extractant with the first heavy component phase, performing phase separation to obtain a second heavy component phase and a second extractant phase, wherein the second extractant phase serves as the first extractant mixed with the heavy component, and the second heavy component phase is discharged from the reaction system.

[0027] In this technical solution, the separated second extractant is no longer directly used as the first extractant to mix with the heavy components, but is used to extract a small part of the metal catalyst in the first heavy component phase. After that, the second heavy component phase and the second extractant phase are obtained after phase separation. Among them, the second heavy component phase in the upper layer is a weak polar phase, which is a heavy component residual liquid mainly containing condensates, and can be directly transported to the residual liquid tank for collection, thereby discharging the continuous reaction system. The second extractant phase in the lower layer contains a small part of the metal catalyst. The second extractant phase does not require additional separation of the metal catalyst and the extractant, but is directly circulated to the extraction device, replacing the first extractant to mix with the heavy components. Then, in the subsequent cyclic reaction process, the small part of the metal catalyst contained therein is separated and collected together with the majority of the metal catalyst. This can not only greatly reduce the accumulation of heavy components in the hydroformylation cycle reaction, but also make the total recovery rate of the metal catalyst as high as 98.2%, significantly improving the recovery rate of the metal catalyst.

[0028] Furthermore, light components are stripped from the hydroformylation reaction liquid, aldehydes in the light components are collected after cooling, and non-condensable gas in the light components is used for circulating and stripping the light components in the hydroformylation reaction liquid.

[0029] In this technical solution, gas stripping is used to separate the light components of the hydroformylation reaction liquid. Specifically, the hydroformylation reaction liquid is mixed with a large amount of recycle gas in a first stripping tower. Light components such as unreacted olefins, alkanes, and product aldehydes are removed from the top of the first stripping tower. The light components are then cooled and the product aldehydes are collected. In some preferred embodiments, after the light components are cooled in a cooler, the uncooled gas enters a cryogenic chiller for further cooling. The final non-condensable gas is recirculated back to the first stripping tower via a compressor and used as recycle gas to strip the light components from the hydroformylation reaction liquid.

[0030] Another object of the present invention is to provide a homogeneous catalytic continuous reaction system for olefin hydroformylation. The system comprises a catalyst recovery unit for treating heavy components of the hydroformylation reaction liquid, extracting a metal catalyst from the heavy components for recycling, and discharging the remaining heavy components such as condensates. This significantly reduces the accumulation of heavy components and enables the recovery and reuse of the metal catalyst, thereby ensuring the activity of the metal catalyst in the reaction system, effectively improving the conversion rate of the industrial hydroformylation continuous reaction, and reducing the reaction cost. The system has broad promotion value.

[0031] The above-mentioned purpose of the present invention is achieved through the following technical solutions:

[0032] A homogeneous catalytic continuous reaction system for olefin hydroformylation, comprising:

[0033] The hydroformylation reactor is used to carry out a hydroformylation reaction after mixing the raw material olefin, synthesis gas and metal catalyst to obtain a hydroformylation reaction liquid;

[0034] a first separation device for removing light components including product aldehydes from the hydroformylation reaction liquid to obtain heavy components including the metal catalyst;

[0035] A light component collection unit, used for cooling and collecting the product aldehyde in the light component;

[0036] a catalyst recovery unit for mixing the heavy component with the first extractant and performing phase separation to obtain a first heavy component phase and a first extractant phase, and separating the metal catalyst and the second extractant from the first extractant phase, recycling the metal catalyst to the hydroformylation reactor for reaction, mixing the second extractant with the heavy component as the first extractant, and discharging the first heavy component phase;

[0037] The first extractant consists of extractant A and extractant B, wherein the extractant A is N,N-dimethylformamide or formamide, and the extractant B is N-methylpyrrolidone.

[0038] In this technical solution, the hydroformylation reactor can be any of a stirred tank reactor, a tower reactor, a jet reflux reactor, or a microinterface reactor. The olefin feedstock and synthesis gas enter the hydroformylation reactor at a specific flow rate, where they are mixed with a metal catalyst and subjected to a hydroformylation reaction at a specific temperature and pressure. In one or more embodiments, the olefin feedstock, synthesis gas, and metal catalyst are mixed and reacted in the hydroformylation reactor for a material residence time of 1 to 8 hours.

[0039] In this technical solution, the hydroformylation reaction liquid obtained after the reaction is completed enters a first separation device. This first separation device can be either an evaporator or a stripping tower. The first separation device removes light components from the hydroformylation reaction liquid to obtain heavy components. The light components enter a subsequent light component collection unit, where the product aldehyde is collected after cooling. The heavy components enter a catalyst recovery unit to remove the condensate and recover the metal catalyst.

[0040] In this technical solution, the heavy component entering the catalyst recovery unit is first mixed uniformly with the first extractant and then separated into two phases, yielding a first heavy component phase and a first extractant phase. The first heavy component phase contains a large amount of condensates and can be directly discharged. Simultaneously, the metal catalyst and the second extractant are separated from the first extractant phase. The metal catalyst is recycled back into the hydroformylation reactor, while the second extractant is recycled and used as the first extractant to further extract the heavy component.

[0041] In the present technical solution, the first extractant is composed of extractant A and extractant B, wherein the extractant A is N,N-dimethylformamide or formamide, and the extractant B is N-methylpyrrolidone.

[0042] Furthermore, the catalyst recovery unit comprises:

[0043] a first extraction device, configured to extract the heavy component with a first extractant to obtain a first heavy component phase and a first extractant phase;

[0044] a second separation device for separating the metal catalyst and the second extractant from the first extractant phase;

[0045] The heavy component residual liquid tank is used to collect the first heavy component phase.

[0046] As a preferred structure of the continuous reaction system, the catalyst recovery unit further comprises:

[0047] The second extraction device is used to extract the first heavy component phase with a second extractant to obtain a second heavy component phase and a second extractant phase. The second extractant phase is returned to the first extraction device and used as the first extractant to extract the heavy component. The second heavy component phase enters the heavy component residual liquid tank for recovery.

[0048] In this technical solution, the second extractant separated from the second separation device is not directly recycled to the first extraction device as the first extractant. Instead, the second extractant is used to extract the first heavy component phase in the second extraction device, extracting a small portion of the metal catalyst contained in the first heavy component phase to obtain a second heavy component phase. After the metal catalyst is removed, the second heavy component phase can be directly discharged to a heavy component residual liquid tank for collection. The second extractant phase, carrying a small portion of the metal catalyst, is recycled to the first extraction device and used as the first extractant to extract the heavy components, thereby significantly improving the recovery rate of the metal catalyst.

[0049] Compared with the prior art, the present invention has the following advantages and beneficial effects:

[0050] 1. The present invention is based on the characteristics of the difference in solubility and specific gravity between the metal catalyst and other substances in the heavy component under specific conditions. The metal catalyst is extracted and recycled by the first extractant, which effectively reduces the production cost of the continuous process. At the same time, the residual liquid of the heavy component after the metal catalyst is separated can be discharged, which significantly reduces the content of condensates in the continuous reaction system and reduces the impact of accumulated condensates on the activity of the metal catalyst, which is conducive to restoring the conversion rate of the continuous reaction.

[0051] 2. Unlike traditional methods for separating heavy components, the present invention can react heavy components in the system at a lower temperature without adding additional reagents that may affect the activity of the catalyst, which is beneficial for maintaining the activity of the catalyst over a longer reaction time, further reducing costs and improving reaction efficiency.

[0052] 3. By rationally adjusting the composition and ratio of the first extractant, the present invention can better utilize the solubility difference between the metal catalyst and the condensate to extract most of the catalyst from the heavy components, so that the total recovery rate of the metal catalyst can be maintained at above 90%;

[0053] 4. The present invention adjusts the volume ratio of extractant A and extractant B in the second extractant after a period of continuous reaction, thereby increasing the specific gravity of the extractant phase in the continuous reaction system, thereby solving the problem of difficulty in separating the heavy component phase from the extractant phase caused by the increase of heavy components in the system after a long reaction period;

[0054] 5. The present invention utilizes a separated second extractant to extract the first heavy component phase. After extracting a small portion of the metal catalyst contained in the first heavy component phase, the extracted second extractant is directly used as the first extractant for subsequent extraction of heavy components. This allows the small portion of the metal catalyst contained therein to be separated and collected together with the majority of the metal catalyst. This not only significantly reduces the accumulation of heavy components in the hydroformylation cycle reaction, but also enables the total recovery rate of the metal catalyst to be as high as 98.2%, significantly improving the recovery rate of the metal catalyst.

[0055] 6. The present invention adopts a first stripping tower to separate the light components, which can effectively protect the reaction activity of the metal catalyst. At the same time, after separating the light components, the product aldehyde is recovered through secondary cooling, and the non-condensable gas is used as circulating gas to strip the light components, thereby improving the utilization efficiency of the circulating gas and further reducing production costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0056] The drawings described herein are used to provide a further understanding of the embodiments of the present invention, constitute a part of this application, and do not constitute a limitation of the embodiments of the present invention. In the drawings:

[0057] Figure 1 A flow chart of a continuous reaction process in a specific embodiment of the present invention;

[0058] Figure 2 Another flow chart of a continuous reaction process according to a specific embodiment of the present invention;

[0059] Figure 3 This is a structural block diagram of a continuous reaction system in a specific embodiment of the present invention;

[0060] Figure 4 It is a flow chart of the catalyst recovery unit in a specific embodiment of the present invention. DETAILED DESCRIPTION

[0061] In order to make the objectives, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below in conjunction with examples and drawings. The exemplary embodiments of the present invention and their descriptions are only used to explain the present invention and are not intended to limit the present invention.

[0062] All raw materials of the present invention are not particularly limited in their sources and can be purchased commercially or prepared according to conventional methods well known to those skilled in the art. All raw materials of the present invention are not particularly limited in their purity; analytically pure materials or those conventionally required in the field of hydroformylation reactions are preferably used. All raw materials of the present invention have conventional designations and abbreviations in the art, and each designation and abbreviation is clear and unambiguous within the field of its relevant application. Those skilled in the art can purchase them commercially or prepare them by conventional methods based on the designation, abbreviation, and corresponding application.

[0063] The present invention has no particular limitation on the expression of the substituents, and all expressions familiar to those skilled in the art are adopted. Based on common sense, those skilled in the art can correctly understand the meaning of the substituents according to the expressions.

[0064] Example 1:

[0065] like Figure 1 The homogeneous catalytic continuous reaction process for olefin hydroformylation shown comprises the following steps:

[0066] The raw material olefin, synthesis gas and metal catalyst are mixed and subjected to hydroformylation reaction to obtain a hydroformylation reaction liquid;

[0067] removing light components including product aldehyde from the hydroformylation reaction liquid to obtain heavy components including the metal catalyst;

[0068] The heavy component and the first extractant are mixed uniformly, and phase separation is performed to obtain a first heavy component phase and a first extractant phase;

[0069] A metal catalyst and a second extractant are separated from the first extractant phase. The metal catalyst is recycled for the hydroformylation reaction, and the second extractant is used as the first extractant mixed with the heavy component.

[0070] In one or more embodiments, the reaction temperature of the hydroformylation reaction is 60-120 °C, the pressure is 1.0-3.0 MPa, and the rhodium concentration is 60-300 ppm.

[0071] In one or more embodiments, the raw olefins, synthesis gas, and metal catalyst are mixed and reacted in a hydroformylation reactor, and the material residence time is 1 to 8 hours.

[0072] In one or more embodiments, the separated second extractant is supplemented to maintain the same or similar composition and ratio as the first extractant. In some embodiments, the second extractant can also be adjusted to a different ratio than the first extractant as the hydroformylation reaction continues for a longer period of time.

[0073] In some preferred embodiments, to further reduce production costs, the heavy components separated from the hydroformylation reaction liquid before the continuous reaction reaches the first time T1 are directly recycled to the hydroformylation reaction system for reuse without extraction. After the continuous reaction reaches the first time T1, the separated heavy components are extracted to separate the metal catalyst and condensate from the heavy components. In one or more embodiments, the first time T1 can be adjusted based on the heavy component content obtained after sampling and analysis. In one or more embodiments, the first time T1 is 80 to 160 hours.

[0074] In some embodiments, the first extractant may be at least one of N,N-dimethylformamide (DMF), N,N-diethylformamide, acetonitrile, N-methylpyrrolidone (NMP), and formamide.

[0075] In some preferred embodiments, light components are stripped from the hydroformylation reaction liquid, the aldehydes in the light components are cooled and collected, and the non-condensable gas in the light components is recycled to strip the light components from the hydroformylation reaction liquid. In one or more embodiments, the recycle gas can be at least one of nitrogen, argon, carbon monoxide, hydrogen, and synthesis gas. In some embodiments, the temperature for stripping the hydroformylation reaction liquid and the recycle gas is 40-160°C, preferably 60-120°C. In some embodiments, the standard volume of the recycle gas is 10-10,000 times the volume of the hydroformylation reaction liquid, preferably 100-5,000 times.

[0076] Example 2:

[0077] On the basis of Example 1, Figure 2 The homogeneous catalytic continuous reaction process for olefin hydroformylation shown further includes the following steps: uniformly mixing the separated second extractant with the first heavy component phase, phase separation to obtain a second heavy component phase and a second extractant phase, the second extractant phase being used as the first extractant mixed with the heavy component, and the second heavy component phase being discharged from the reaction system.

[0078] In this embodiment, the separated second extractant is no longer directly used as the first extractant to mix with the heavy components, but is used to extract a small portion of the metal catalyst in the first heavy component phase. After phase separation, a second heavy component phase and a second extractant phase are obtained. Among them, the second heavy component phase in the upper layer is a weakly polar phase, which is a heavy component residual liquid mainly containing condensates and can be directly transported to a residual liquid tank for collection, thereby being discharged from the continuous reaction system. The second extractant phase in the lower layer contains a small portion of the metal catalyst. The second extractant phase does not require additional separation of the metal catalyst and the extractant, but is directly recycled to the extraction device, replacing the first extractant to mix with the heavy components. Then, in the subsequent cyclic reaction process, the small portion of the metal catalyst contained in it is separated and collected together with the majority of the metal catalyst. This not only significantly reduces the accumulation of heavy components in the hydroformylation cycle reaction, but also increases the total recovery rate of the metal catalyst to as high as 98.2%, significantly improving the recovery rate of the metal catalyst.

[0079] In some preferred embodiments, the volume ratio of the first extractant to the heavy component is 1:1 to 3:1, and the volume ratio of the second extractant to the first heavy component phase is 1:1 to 3:1. Using too little extractant can affect the overall recovery of the metal catalyst, but too much extractant can also cause miscibility between the polar and less polar phases, similarly reducing catalyst recovery. Therefore, in more preferred embodiments, the volume ratios of the extractant to the heavy component, and the second extractant to the first heavy component phase, range from 1:1 to 3:1, and more preferably, range from 1:1 to 2:1.

[0080] In some embodiments, the extraction temperature of the first extractant and the heavy component is 40-60°C, and the extraction temperature of the second extractant and the first heavy component is 40-60°C.

[0081] In some embodiments, the temperature for phase separation after extraction is -10 to 20° C. In one or more embodiments, the phase separation time is 10 to 180 minutes.

[0082] Example 3:

[0083] On the basis of the above embodiment, the first extractant is composed of extractant A and extractant B, wherein the extractant A is N,N-dimethylformamide or formamide, and the extractant B is N-methylpyrrolidone.

[0084] In some preferred embodiments, the volume ratio of extractant A to extractant B in the first extractant is 1.2-20; after separation to obtain the second extractant, extractant A and / or extractant B are added so that the volume ratio of extractant A to extractant B in the second extractant is the same as the volume ratio of extractant A to extractant B in the first extractant.

[0085] In some preferred embodiments, after a certain reaction time, extractant A and / or extractant B are added to the separated second extractant, such that the volume ratio of extractant B to extractant A in the second extractant is 1 to 1.1. In this embodiment, after a certain period of continuous reaction time, for example, greater than or equal to 500 hours, extractant A and / or extractant B are added to the second extractant, such that the volume of extractant B is equal to or slightly greater than that of extractant A. This differs from the continuous reaction before the second time T2, where a larger amount of extractant A is used. By increasing the proportion of extractant B, the lower extractant phase has a higher specific gravity during phase separation, thereby facilitating the separation of the first extractant phase and the first heavy component phase, as well as the separation of the heavy component residue and the second extractant phase. This allows for maintaining a high metal catalyst recovery rate and heavy component removal efficiency even after a long period of continuous reaction. In some embodiments, the second time T2 can be adjusted based on the accumulated heavy component content in the system. In one or more embodiments, the second time T2 is 400 to 550 hours.

[0086] Example 4:

[0087] like Figure 3 and Figure 4 The present invention provides a homogeneous catalytic continuous reaction system for olefin hydroformylation, comprising:

[0088] The hydroformylation reactor is used to carry out a hydroformylation reaction after mixing the raw material olefin, synthesis gas and metal catalyst to obtain a hydroformylation reaction liquid;

[0089] a first separation device for removing light components including product aldehydes from the hydroformylation reaction liquid to obtain heavy components including the metal catalyst;

[0090] A light component collection unit, used for cooling and collecting the product aldehyde in the light component;

[0091] a catalyst recovery unit for mixing the heavy component with the first extractant and performing phase separation to obtain a first heavy component phase and a first extractant phase, and separating the metal catalyst and the second extractant from the first extractant phase, recycling the metal catalyst to the hydroformylation reactor for reaction, mixing the second extractant with the heavy component as the first extractant, and discharging the first heavy component phase;

[0092] The first extractant consists of extractant A and extractant B, wherein the extractant A is N,N-dimethylformamide or formamide, and the extractant B is N-methylpyrrolidone.

[0093] Wherein, the catalyst recovery unit comprises:

[0094] a first extraction device, configured to extract the heavy component with a first extractant to obtain a first heavy component phase and a first extractant phase;

[0095] a second separation device for separating the metal catalyst and the second extractant from the first extractant phase;

[0096] The heavy component residual liquid tank is used to collect the first heavy component phase.

[0097] In some preferred embodiments, the catalyst recovery unit further includes: a second extraction device for extracting the first heavy component phase with a second extractant to obtain a second heavy component phase and a second extractant phase; the second extractant phase is returned to the first extraction device and used as the first extractant to extract the heavy component; and the second heavy component phase enters a heavy component residual liquid tank for recovery.

[0098] In one or more embodiments, the hydroformylation reactor may be any one of a stirred tank reactor, a tower reactor, a jet reflux reactor, and a microinterface reactor.

[0099] In one or more embodiments, the hydroformylation reaction liquid is transferred to a low-pressure tank before stripping to release unreacted gas.

[0100] In some preferred embodiments, Figure 3As shown, the first separating device adopts a stripping tower, and the light component output end of the stripping tower is connected to a light component collecting unit. The light component collecting unit includes a cooler, an aldehyde collecting tank, a cryogenic refrigerator, a condensate tank, and a compressor connected in sequence, wherein the cooler and the cryogenic refrigerator are used for secondary recovery of the light component and can be condensed into a liquid product aldehyde. For non-condensable gas that cannot be condensed, the compressor circulates to the first stripping tower to strip the light component again. Compared to an evaporator, the stripping tower can further reduce the impact on the activity of the metal catalyst by stripping. In one or more embodiments, the temperature in the first stripping tower is 40~160°C, and preferably, the temperature of stripping is 60~120°C. In one or more embodiments, the pressure of the first stripping tower is 0~0.1 MPa, preferably 0.001~0.05 MPa.

[0101] In some preferred embodiments, Figure 4 As shown, the first extraction device includes a first extraction kettle and a first phase separator, the first extraction kettle is used to mix and extract the first extractant and the heavy component, and the first phase separator is used to separate the phases to obtain a first heavy component phase and a first extractant phase; the second extraction device includes a second extraction kettle and a second phase separator, the second extraction kettle is used to mix and extract the first heavy component phase and the second extractant, and the second phase separator is used to separate the phases to obtain a second heavy component phase and a second extractant phase.

[0102] In some embodiments, the extraction temperature in the first and second extraction kettles is typically 40-60°C. The extraction kettles can be any conventional extraction kettle. In one or more embodiments, the first and second extraction kettles are jacketed or equipped with internal coils and agitators, providing stirring, mixing, heating, and cooling functions. After extraction, the reaction mixture is transferred to a phase separator for further phase separation, typically at a temperature between -10 and 20°C.

[0103] Example 5:

[0104] In this embodiment, the experiment was carried out using FT-C7 olefins (Fischer-Tropsch olefins: 75% 1-heptene, 25% heptane) and synthesis gas as raw materials. In the experiment, the FT-C7 olefin feed rate was 180 mL / h, the synthesis gas (volume ratio CO:H2=1:1.02) was 3.96 L / h, the rhodium catalyst was acetylacetonato carbonyl rhodium, the rhodium catalyst concentration was 150 ppm, and the phosphorus ligand was the binaphthol di(indolyl)bisphosphine ligand L1 disclosed in Example 3 of patent CN113333028B, and its concentration was 1 wt%.

[0105] After the feeding, the reaction temperature in the hydroformylation reactor (effective volume 1 L) was controlled to be 70 °C and the reaction pressure gauge pressure was 2.5 MPa. After the reaction, a hydroformylation reaction liquid was generated, and the unreacted gas was released from the top of the hydroformylation reactor.

[0106] The hydroformylation reaction liquid from the hydroformylation reactor is decompressed and enters a low-pressure tank. It then enters the first stripping tower at a controlled flow rate (5 mL / min) along with nitrogen. The temperature of the first stripping tower is 85°C, and the nitrogen flow rate is 18 L / min. 60% of the hydroformylation reaction liquid is stripped out and subjected to two-stage cooling. The non-condensable nitrogen is compressed and recycled back to the first stripping tower as circulating gas. The hydroformylation reaction liquid containing the rhodium catalyst, i.e., the heavy component, exits the bottom of the stripping tower and is directly recycled back to the hydroformylation reactor.

[0107] After 100 hours of continuous experimentation, the hydroformylation catalytic activity remained relatively stable. The total heavy component content in the hydroformylation reaction liquid from the rhodium-containing catalyst at the bottom of the first stripping column was 12.8%. Sample analysis from the low-pressure tank revealed a 90% FT-C7 olefin conversion, 90% C8 aldehyde selectivity, a C8 aldehyde normal-to-iso ratio of 40, and approximately 0.5% new condensation heavy component formation.

[0108] After 150 hours of continuous experimentation, the total content of heavy components in the rhodium-catalyzed hydroformylation reaction liquid at the bottom of the first stripping column reached 19.3%. Analysis of samples taken from the low-pressure tank revealed FT-C7 olefin conversion of 84%, C8 aldehyde selectivity of 90%, and a C8 aldehyde normal-to-iso ratio of 40, with the conversion slowly decreasing.

[0109] Subsequently, the hydroformylation reaction liquid containing the rhodium catalyst at the bottom of the first stripping tower is transported to a catalyst recovery unit, the second heavy component containing most of the condensate is phase separated, and the rhodium catalyst is recycled back to the hydroformylation reactor.

[0110] Specifically, the first extractant is DMF and NMP, with a volume ratio of 95:5. The heavy component containing the rhodium catalyst at the bottom of the first stripper is mixed with the first extractant or the second extractant from the lower layer of the second extraction kettle, then stirred and extracted in the first extraction kettle. Extraction conditions are 60°C, 0.1 MPa nitrogen atmosphere, stirring for 30 minutes, and then cooled to 0°C and allowed to stand for 2 hours in the first phase separator. The rhodium-containing first extractant phase from the lower layer of the first phase separator is transferred to the second stripper to remove the second extractant. The metal catalyst-containing solution at the bottom is recycled back to the hydroformylation reactor. The second stripper is operated at 90°C, with a gas flow rate of 8 L / min and an extract phase flow rate of 2 mL / min. The first heavy component phase from the upper layer of the first phase separator and the removed second extractant are stirred in a second extraction kettle, with the conditions in the second extraction kettle being the same as those in the first extraction kettle. After extraction, the second heavy component phase is transferred to a heavy component residual liquid tank, and the second extractant phase is recycled to the first extraction kettle.

[0111] Sampling analysis from the bottom of the second stripping column revealed a calculated rhodium recovery rate of 98% and a heavy component removal rate of 67%. After the heavy components were partially removed, continuous operation revealed an FT-C7 olefin conversion rate of 88%, a C8 aldehyde selectivity of 90%, a C8 aldehyde normal-to-iso ratio of 40, and a slowly recovering catalyst activity.

[0112] When the experiment was continued for 500 h, DMF and / or NMP were added to the second extractant so that the volume ratio of NMP to DMF in the second extractant was 1.1.

[0113] Example 6 to Example 13:

[0114] In order to further explore the effects of the composition and ratio of the first extractant on the rhodium catalyst recovery test, rhodium catalyst recovery tests were carried out in Examples 6 to 13.

[0115] Example 6:

[0116] 200 ml of the hydroformylation reaction liquid, the components of which are shown in Table 1 below, was taken and passed through a first separation device, such as evaporation under reduced pressure to remove light components. 110 ml of the remaining rhodium-containing heavy component was mixed with 110 ml of a first extractant (DMF:NMP=95:5) in a 500 ml first extraction kettle. After stirring at 60 degrees for 30 minutes, the mixture was cooled to -5 to 5 degrees in a first phase separator and allowed to stand for 2 hours for phase separation. About 110 ml of the upper heavy component phase (first heavy component phase) was taken out and mixed with 110 ml of a second extractant having the same composition and ratio as the first extractant in a 500 ml second extraction kettle. After stirring at 60 degrees for 30 minutes, the mixture was cooled to -5 to 5 degrees in a second phase separator and allowed to stand for 2 hours for phase separation. The second extractant phase containing rhodium catalyst in the lower layer was taken out and combined with the first heavy component phase in the lower layer of the first extraction kettle, and the extractant phase was removed by evaporation under reduced pressure. The rhodium content was analyzed, and the rhodium recovery rate was calculated to be 98.2%.

[0117] Table 1:

[0118]

[0119] Example 7:

[0120] 200 ml of the hydroformylation reaction solution, the components of which are shown in Table 2 below, was taken and evaporated under reduced pressure in an evaporator to remove light components. The remaining rhodium-containing heavy component, 110 ml, was mixed with 110 ml of a first extractant (DMF:NMP=55:45) in a 500 ml first extraction kettle and stirred at 60 degrees for 30 minutes. The mixture was then cooled to -5-5 degrees in a first phase separator and allowed to stand for 2 hours for phase separation. About 110 ml of the upper heavy phase (first heavy phase) was taken out and mixed with 110 ml of a second extractant in a 500 ml second extraction kettle. The second extractant had the same composition and ratio as the first extractant. The mixture was stirred at 60 degrees for 30 minutes. The mixture was then cooled to -5-5 degrees in a second phase separator and allowed to stand for 2 hours for phase separation. The second extractant phase containing rhodium catalyst in the lower layer was taken out and combined with the first heavy phase in the lower layer of the first extraction kettle to remove the extractant phase by reduced pressure evaporation. The rhodium content was analyzed, and the calculated rhodium recovery rate was 97.6%.

[0121] Table 2:

[0122]

[0123] Example 8:

[0124] 200 ml of the hydroformylation reaction liquid, the components of which are shown in Table 3 below, was taken and evaporated under reduced pressure in an evaporator to remove light components. The remaining rhodium-containing heavy component, 110 ml, was mixed with 110 ml of a first extractant (formamide:NMP=10:1) in a 500 ml first extraction kettle and stirred at 60 degrees for 30 minutes. The mixture was then cooled to -5-5 degrees in a first phase separator and allowed to stand for 2 hours for phase separation. About 110 ml of the upper heavy phase (first heavy phase) was taken out and mixed with 110 ml of a second extractant in a 500 ml second extraction kettle. The second extractant had the same composition and ratio as the first extractant. The mixture was stirred at 60 degrees for 30 minutes. The mixture was then cooled to -5-5 degrees in a second phase separator and allowed to stand for 2 hours for phase separation. The second extractant phase containing rhodium catalyst in the lower layer was taken out and combined with the first heavy phase in the lower layer of the first extraction kettle to remove the extractant phase by reduced pressure evaporation. The rhodium content was analyzed, and the calculated rhodium recovery rate was 95.2%.

[0125] Table 3:

[0126]

[0127] Example 9:

[0128] 200 ml of the hydroformylation reaction liquid was taken, the components of which are shown in Table 4 below. Light components were removed by evaporation under reduced pressure in an evaporator. The remaining rhodium-containing heavy component, 110 ml, was mixed with 220 ml of a first extractant (DMF:NMP=10:1) in a 500 ml first extraction kettle and stirred at 60 degrees for 30 minutes. The mixture was then cooled to -5 to 5 degrees in a first phase separator and allowed to stand for 2 hours for phase separation. About 110 ml of the upper heavy phase (first heavy phase) was taken out and mixed with 220 ml of a second extractant in a 500 ml second extraction kettle. The second extractant had the same composition and ratio as the first extractant. The mixture was stirred at 60 degrees for 30 minutes. The mixture was then cooled to -5 to 5 degrees in a second phase separator and allowed to stand for 2 hours for phase separation. The second extractant phase containing rhodium catalyst in the lower layer was taken out and combined with the first heavy phase in the lower layer of the first extraction kettle to remove the extractant phase by reduced pressure evaporation. The rhodium content was analyzed, and the calculated rhodium recovery rate was 92.5%.

[0129] Table 4:

[0130]

[0131] Example 10:

[0132] 200 ml of the hydroformylation reaction liquid, the components of which are shown in Table 5 below, was taken and evaporated under reduced pressure in an evaporator to remove light components. The remaining rhodium-containing heavy component 110 ml was mixed with 330 ml of the first extractant (DMF:NMP=10:1) in a 500 ml first extraction kettle and stirred at 60 degrees for 30 minutes. The mixture was then cooled to -5-5 degrees in a first phase separator and allowed to stand for 2 hours for phase separation. About 110 ml of the upper heavy phase (first heavy phase) was taken out and mixed with 330 ml of the second extractant in a 500 ml second extraction kettle. The second extractant had the same composition and ratio as the first extractant. The mixture was stirred at 60 degrees for 30 minutes. The mixture was then cooled to -5-5 degrees in a second phase separator and allowed to stand for 2 hours for phase separation. The second extractant phase containing rhodium catalyst in the lower layer was taken out and combined with the first heavy phase in the lower layer of the first extraction kettle, and the extractant phase was removed by reduced pressure evaporation. The rhodium content was analyzed, and the rhodium recovery rate was calculated to be 89.0%.

[0133] Table 5:

[0134]

[0135] Example 11:

[0136] 200 ml of the hydroformylation reaction liquid, the components of which are shown in Table 6 below, was taken and evaporated under reduced pressure in an evaporator to remove light components. The remaining rhodium-containing heavy component, 110 ml, was mixed with 110 ml of a first extractant (DMF:NMP=10:1) in a 500 ml first extraction kettle and stirred at 50 degrees for 30 minutes. The mixture was then cooled to -5-5 degrees in a first phase separator and allowed to stand for 2 hours for phase separation. About 110 ml of the upper heavy phase (first heavy phase) was taken out and mixed with 110 ml of a second extractant in a 500 ml second extraction kettle. The second extractant had the same composition and ratio as the first extractant. The mixture was stirred at 50 degrees for 30 minutes. The mixture was then cooled to -5-5 degrees in a second phase separator and allowed to stand for 2 hours for phase separation. The second extractant phase containing rhodium catalyst in the lower layer was taken out and combined with the first heavy phase in the lower layer of the first extraction kettle to remove the extractant phase by reduced pressure evaporation. The rhodium content was analyzed, and the rhodium recovery rate was calculated to be 90.0%.

[0137] Table 6:

[0138]

[0139] Example 12:

[0140] 200 ml of the hydroformylation reaction liquid, the components of which are shown in Table 7 below, was taken and evaporated under reduced pressure in an evaporator to remove light components. The remaining rhodium-containing heavy component, 110 ml, was mixed with 110 ml of the first extractant (DMF:NMP=9:1) in a 500 ml first extraction kettle and stirred at 60 degrees for 30 minutes. The mixture was then cooled to -5-5 degrees in a first phase separator and allowed to stand for 2 hours for phase separation. About 110 ml of the upper heavy phase (first heavy phase) was taken out and mixed with 110 ml of the second extractant, which had the same composition and ratio as the first extractant, in a 500 ml second extraction kettle. The second extractant phase containing rhodium catalyst in the lower layer was taken out and combined with the first heavy phase in the lower layer of the first extraction kettle, and the extractant phase was removed by reduced pressure evaporation. The rhodium content was analyzed, and the rhodium recovery rate was calculated to be 95.2%.

[0141] Table 7:

[0142]

[0143] Example 13:

[0144] 200 ml of the hydroformylation reaction liquid, the components of which are shown in Table 8 below, was taken and evaporated under reduced pressure in an evaporator to remove light components. The remaining rhodium-containing heavy component, 110 ml, was mixed with 110 ml of a first extractant (DMF:NMP=20:1) in a 500 ml first extraction kettle and stirred at 60 degrees for 30 minutes. The mixture was then cooled to -5-5 degrees in a first phase separator and allowed to stand for 2 hours for phase separation. About 110 ml of the upper heavy phase (first heavy phase) was taken out and mixed with 110 ml of a second extractant in a 500 ml second extraction kettle. The second extractant had the same composition and ratio as the first extractant. The mixture was stirred at 60 degrees for 30 minutes. The mixture was then cooled to -5-5 degrees in a second phase separator and allowed to stand for 2 hours for phase separation. The second extractant phase containing rhodium catalyst in the lower layer was taken out and combined with the first heavy phase in the lower layer of the first extraction kettle to remove the extractant phase by reduced pressure evaporation. The rhodium content was analyzed, and the rhodium recovery rate was calculated to be 98.0%.

[0145] Table 8:

[0146]

[0147] This demonstrates that the two-stage extraction and recycling of the extractant significantly increases the recovery rate of the rhodium catalyst to 90%, without the addition of additional complexes to react with the catalyst. Furthermore, by adjusting the composition and ratio of the first extractant, the overall recovery rate of the rhodium catalyst can be increased to 98.2%, significantly reducing the cost of continuous hydroformylation production and facilitating industrial production applications.

[0148] The terms "first," "second," and so on (e.g., first separation device, second separation device, first extraction device, second extraction device, etc.) used herein are merely used to distinguish corresponding components for clarity of description and are not intended to limit any order or emphasize importance. Furthermore, the term "connected" used herein, unless otherwise specified, may refer to a direct connection or an indirect connection via other components.

[0149] The specific implementation methods described above further illustrate the objectives, technical solutions and beneficial effects of the present invention in detail. It should be understood that the above description is only a specific implementation method of the present invention and is not intended to limit the scope of protection of the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the scope of protection of the present invention.

Claims

1. A homogeneous catalytic continuous reaction process for olefin hydroformylation, characterized in that: The following steps are involved: The raw material olefin, synthesis gas and metal catalyst are mixed and subjected to hydroformylation reaction to obtain a hydroformylation reaction liquid; removing light components including product aldehyde from the hydroformylation reaction liquid to obtain heavy components including the metal catalyst; The heavy component and the first extractant are mixed uniformly, and phase separation is performed to obtain a first heavy component phase and a first extractant phase; A metal catalyst and a second extractant are separated from the first extractant phase. The metal catalyst is recycled for the hydroformylation reaction, and the second extractant is used as the first extractant mixed with the heavy component.

2. The homogeneous catalytic continuous reaction process for olefin hydroformylation according to claim 1, characterized in that: The first extractant consists of extractant A and extractant B, wherein the extractant A is N,N-dimethylformamide or formamide, and the extractant B is N-methylpyrrolidone.

3. The homogeneous catalytic continuous reaction process for olefin hydroformylation according to claim 2, characterized in that: The volume ratio of extractant A to extractant B in the first extractant is 1.2-20; after the second extractant is separated, extractant A and / or extractant B are added so that the volume ratio of extractant A to extractant B in the second extractant is the same as the volume ratio of extractant A to extractant B in the first extractant.

4. The homogeneous catalytic continuous reaction process for olefin hydroformylation according to claim 3, characterized in that: After a certain reaction time, extractant A and / or extractant B are added to the separated second extractant, so that the volume ratio of extractant B to extractant A in the second extractant is 1-1.

1.

5. A homogeneous catalytic continuous reaction process for olefin hydroformylation according to any one of claims 1 to 4, characterized in that: The following steps are also included: The separated second extractant is evenly mixed with the first heavy component phase, and phase separation is performed to obtain a second heavy component phase and a second extractant phase. The second extractant phase is used as the first extractant mixed with the heavy component, and the second heavy component phase is discharged from the reaction system.

6. A homogeneous catalytic continuous reaction process for olefin hydroformylation according to any one of claims 1 to 5, characterized in that: Light components are stripped from the hydroformylation reaction liquid, aldehydes in the light components are collected after cooling, and non-condensable gas in the light components is used for circulating and stripping the light components in the hydroformylation reaction liquid.

7. A homogeneous catalytic continuous reaction system for olefin hydroformylation, characterized in that: include: The hydroformylation reactor is used to carry out a hydroformylation reaction after mixing the raw material olefin, synthesis gas and metal catalyst to obtain a hydroformylation reaction liquid; a first separation device for removing light components including product aldehydes from the hydroformylation reaction liquid to obtain heavy components including the metal catalyst; A light component collection unit, used for cooling and collecting the product aldehyde in the light component; a catalyst recovery unit for mixing the heavy component with the first extractant and performing phase separation to obtain a first heavy component phase and a first extractant phase, and separating the metal catalyst and the second extractant from the first extractant phase, recycling the metal catalyst to the hydroformylation reactor for reaction, mixing the second extractant with the heavy component as the first extractant, and discharging the first heavy component phase; The first extractant consists of extractant A and extractant B, wherein the extractant A is N,N-dimethylformamide or formamide, and the extractant B is N-methylpyrrolidone.

8. The homogeneous catalytic continuous reaction system for olefin hydroformylation according to claim 7, characterized in that: The catalyst recovery unit comprises: a first extraction device, configured to extract the heavy component with a first extractant to obtain a first heavy component phase and a first extractant phase; a second separation device for separating the metal catalyst and the second extractant from the first extractant phase; The heavy component residual liquid tank is used to collect the first heavy component phase.

9. The homogeneous catalytic continuous reaction system for olefin hydroformylation according to claim 8, characterized in that: The catalyst recovery unit also includes: The second extraction device is used to extract the first heavy component phase with a second extractant to obtain a second heavy component phase and a second extractant phase. The second extractant phase is returned to the first extraction device and used as the first extractant to extract the heavy component. The second heavy component phase enters the heavy component residual liquid tank for recovery.

10. The homogeneous catalytic continuous reaction system for olefin hydroformylation according to claim 8 or 9, characterized in that: The first separation device and the second separation device are stripping towers, and a low-pressure tank is further provided between the hydroformylation reactor and the first separation device.

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