System device and method for producing aldehyde compounds through supergravity two-phase hydroformylation

Abstract

The invention discloses a system device and a method for producing aldehyde compounds through supergravity two-phase hydroformylation. The system device comprises a supergravity reactor, a buffer tank, a first circulating pump, a tower kettle heat exchanger, a circulating heat exchanger, a split-phase tank, a second circulating pump, a crude aldehyde transfer pump, a supergravity rectification unit, a tower kettle reboiler, a product extraction pump and a cold and hot all-in-one machine. According to the system device, under the condition that a polar solvent and a surfactant are not added, the two-phase hydroformylation reaction process can be greatly enhanced through the supergravity reactor, the technological process is shortened, and then a product is separated and purified through the supergravity rectification unit to obtain an aldehyde compound; the problems of low two-phase hydroformylation reaction efficiency, serious self-polymerization in a hydroformylation product purification process and the like in the prior art are solved; by utilizing the method, the olefin conversion rate is more than 90%, the aldehyde selectivity of the product is more than 99%, the purity of the purified product is more than 99%, and the loss amount of the catalyst is less than or equal to 0.5 mg / kg.

Description

Technical Field

[0001] This invention relates to the field of olefin hydroformylation technology; specifically, it relates to a system apparatus and method for producing aldehyde compounds by supergravity two-phase hydroformylation. Background Technology

[0002] Hydroformylation is a core process in industrial production for the preparation of aldehydes and alcohols. Its high atom economy makes it widely used in the synthesis of bulk and fine chemicals such as plasticizers and detergents, making it an indispensable key technology in modern chemical industry. Taking butanol and octanol (propylene hydroformylation process) as an example, by the end of 2023, my country's effective production capacity of n-butanol and octanol totaled 5.746 million tons / year, with an estimated annual output value of approximately 32.17 billion yuan based on a 70% operating rate. Currently, low-carbon hydroformylation processes generally employ homogeneous catalysts, resulting in a gas-liquid two-phase reaction. Enhancing gas-liquid mass transfer can improve reaction efficiency to some extent. However, in the production of higher alcohols, due to the high boiling point of the product, using a homogeneous reaction would lead to faster catalyst deactivation due to the high temperature during catalyst-product separation. Therefore, two-phase hydroformylation has significant advantages in higher alcohol production. By employing heterogeneous catalysts, catalyst-product separation is achieved through a phase-separation tank, resulting in a gas-liquid-liquid reaction. Compared to homogeneous reactions, two-phase hydroformylation demands higher mass transfer capabilities, involving not only gas-liquid mass transfer but also liquid-liquid two-phase mixing.

[0003] Traditional stirred tank reactor (SBR) processes for two-phase hydroformylation often employ polar solvents or surfactants to enhance the gas-liquid-liquid reaction, which leads to increased production costs and difficulties in the subsequent separation of solvents, products, and catalysts.

[0004] For example, Chinese patent application No. 202110038259.5 discloses a method for preparing aldehydes by two-phase hydroformylation of olefins. This method uses inexpensive and readily available highly polar formamides, N-methylformamides, N,N-dimethylformamides, etc., as solvents to hydroformylate olefins with H2 / CO synthesis gas to generate aldehydes. Since the solubility of olefins in highly polar organic solvents is much greater than their solubility in water, the reaction activity is greatly improved compared to water-oil two-phase hydroformylation.

[0005] For example, Chinese Patent Application No. 202310817701.3 discloses a composition and method for preparing high carbon aldehydes by hydroformylation in water / oil. This method improves the low solubility of high carbon olefins in water by adding quaternary ammonium salt cationic surfactants to the reaction system, thereby improving the reaction efficiency.

[0006] However, the above technology still has the following drawbacks: 1) low efficiency of two-phase hydroformylation reaction; 2) low separation efficiency of hydroformylation products; 3) severe self-polymerization during the purification process of hydroformylation products. Summary of the Invention

[0007] The first technical problem to be solved by the present invention is to provide a system apparatus for producing aldehyde compounds by two-phase hydroformylation under supergravity.

[0008] The second technical problem this invention aims to solve is to provide a method for producing aldehyde compounds through two-phase hydroformylation under centrifugal force using the aforementioned system. This method can significantly enhance the two-phase hydroformylation reaction process through a centrifugal reactor without adding polar solvents or surfactants, shortening the process flow. The product is then separated and purified using a centrifugal distillation unit to obtain aldehyde compounds. This solves the problems of low efficiency in the two-phase hydroformylation reaction and severe self-polymerization during the purification process of the hydroformylation product in existing technologies. Using the method of this invention, the olefin conversion rate is above 90%, the aldehyde selectivity is above 99%, the purity of the purified product is above 99%, and the catalyst loss is ≤0.5 mg / kg.

[0009] To solve the first technical problem mentioned above, the present invention adopts the following technical solution: A system for producing aldehyde compounds by two-phase hydroformylation under high gravity includes a high gravity reactor, a buffer tank, a first circulating pump, a column bottom heat exchanger, a circulating heat exchanger, a phase separation tank, a second circulating pump, a crude aldehyde transfer pump, a high gravity distillation unit, a column bottom reboiler, a product collection pump, and an integrated heating and cooling unit. The liquid phase outlet of the supergravity reactor 1 is connected to the inlet of the buffer tank via a pipeline. The outlet of the buffer tank is connected to the inlet of the first circulation pump via a pipeline; The outlet of the first circulating pump is connected to the shell-side inlet of the tower bottom heat exchanger via a pipeline; The shell-side outlet of the tower bottom heat exchanger is connected to the inlet of the circulating heat exchanger via a pipeline. The outlet of the circulating heat exchanger is divided into two branches; the first branch is connected to the inlet of the phase separation tank through a pipeline; the second branch is connected to the liquid phase inlet of the hypergravity reactor through a pipeline. One liquid phase outlet of the phase separation tank is connected to the inlet of the second circulation pump via a pipeline; the gas phase outlet of the phase separation tank is vented; the outlet of the second circulation pump is connected to the liquid phase inlet of the hypergravity reactor via a pipeline. The other liquid phase outlet of the phase separation tank is connected to the inlet of the crude aldehyde transfer pump via a pipeline; the outlet of the crude aldehyde transfer pump is connected to the liquid phase inlet of the high gravity distillation unit via a pipeline. The liquid phase outlet of the supergravity distillation unit is connected to the tube side inlet of the reboiler heat exchanger via a pipeline. The tube side outlet of the reboiler heat exchanger is divided into two branches: one branch is connected to the product collection pump to collect the product; the other branch is connected to the reboiler and then returns to the supergravity distillation unit.

[0010] Preferably, the shell of the supergravity reactor is provided with a shell heat exchange jacket; the integrated heating and cooling machine is connected to the inlet of the shell heat exchange jacket through a pipe, and the outlet of the shell heat exchange jacket is connected to the integrated heating and cooling machine through a pipe, forming a heat exchange cycle.

[0011] Preferably, the top light component outlet of the supergravity distillation unit is vented or connected to the gas phase inlet of the supergravity reactor via a pressurized pipeline.

[0012] Preferably, a liquid phase mixer is provided at the liquid phase inlet of the supergravity reactor to ensure that the fresh olefins, the circulating catalyst phase, and the circulating liquid phase are fully mixed before entering the supergravity reactor.

[0013] To solve the second technical problem mentioned above, the present invention adopts the following technical solution: A method for producing aldehyde compounds by two-phase hydroformylation using the above-described system apparatus includes the following steps: S1, fresh olefins, recycled catalyst phase (including aqueous phase and ligands in the system) and recycled liquid phase enter the hypergravity reactor through a liquid phase mixer, and react with syngas in the hypergravity reactor to produce aldehydes. S2. The liquid phase after the reaction enters the buffer tank and is first sent to the bottom heat exchanger of the column by the first circulation pump to exchange heat with the bottom liquid phase of the supergravity distillation unit. Then it enters the circulation heat exchanger for heat exchange again. Part of the liquid phase returns to the supergravity reactor and the other part of the liquid phase enters the phase separation tank. S3. The liquid phase undergoes gas-liquid separation and liquid-liquid phase separation in the phase separation tank. The catalyst phase is returned to the centrifugal reactor via the second circulation pump. The product phase is sent to the centrifugal distillation unit for product purification via the crude aldehyde transfer pump. S4. After the product phase is separated in the supergravity distillation unit, the light component gas phase at the top is vented or repressurized and sent into the supergravity reactor for reaction. The liquid phase in the bottom of the supergravity distillation unit is first heated in the bottom heat exchanger, and then a part of the bottom liquid phase is vaporized through the bottom reboiler and returned to the supergravity distillation unit, while the other part of the bottom liquid phase is collected by the product collection pump to obtain the product aldehyde compounds.

[0014] Preferably, in step S1, the fresh olefin refers to a C2 or higher olefin; more preferably, it is a C5 or higher olefin.

[0015] Preferably, the operating pressure of the supergravity reactor is 0.5MPa-20MPa, the operating temperature is 50-200℃, and the rotation speed is 100-3000r / min; more preferably, the operating pressure is 0.5MPa-5MPa, the operating temperature is 60-110℃, and the rotation speed is 500-1500r / min.

[0016] Preferably, in step S1, the pressure ratio of hydrogen to carbon monoxide in the synthesis gas is 15:1; more preferably, it is 1.05:1.

[0017] Preferably, in step S1, the volume ratio of fresh olefin to recycled catalyst phase is 1:0.1-20, the mass ratio of fresh olefin to catalyst is 100-100000:1, and the molar ratio of catalyst to ligand is 1:1-100; more preferably, the volume ratio of fresh olefin to recycled catalyst phase is 1:1-10, the mass ratio of fresh olefin to catalyst is 200-10000:1, and the molar ratio of catalyst to ligand is 1:5-50.

[0018] Preferably, the circulation ratio of the circulating liquid phase in the supergravity reactor is 10-150; more preferably, it is 10-50.

[0019] Preferably, in step S4, the operating pressure of the supergravity distillation unit is -0.1 to 10 MPa; more preferably -0.1 to 1 MPa.

[0020] Preferably, in step S4, the operating temperature of the supergravity distillation unit is 50-200℃; more preferably, it is 50-150℃.

[0021] Preferably, in step S4, the operating speed of the supergravity distillation unit is 100-3000 r / min, more preferably 200-1000 r / min.

[0022] Preferably, in step S4, the reflux ratio of the supergravity distillation unit is 1-15; more preferably 1-10.

[0023] Any range described in this invention includes the endpoint, any value between the endpoints, and any subrange consisting of the endpoint or any value between the endpoints.

[0024] Unless otherwise specified, all raw materials used in this invention can be obtained commercially, and the equipment used in this invention can be conventional equipment in the relevant field or refer to existing technology in the relevant field.

[0025] Compared with the prior art, the present invention has the following beneficial effects: 1. The present invention discloses a reaction system for producing aldehyde compounds by two-phase hydroformylation under supergravity. The two-phase hydroformylation reaction process is carried out in a supergravity reactor. It does not require the addition of polar solvents or surfactants. The reaction process is simple, the reactor volume is small, the catalyst investment cost is low, and it is easy to scale up industrially.

[0026] 2. The reaction system for producing aldehydes via two-phase hydroformylation under high gravity of this invention employs high gravity distillation technology for the distillation and purification of the aldehyde products, shortening the material residence time, reducing the risk of material self-polymerization, and improving product yield. Simultaneously, heat coupling is implemented, effectively utilizing the heat from the hydroformylation reaction in the distillation process, reducing system energy consumption and achieving efficient integrated utilization of heat within the system.

[0027] 3. The present invention provides a method for producing aldehyde compounds by two-phase hydroformylation under supergravity conditions. The process is simple, highly integrated, and can achieve a high yield of aldehyde compounds. Using the method of the present invention, the olefin conversion rate is above 90%, the selectivity of the product aldehyde is above 99%, the purity of the purified product is above 99%, and the catalyst loss is ≤0.5 mg / kg. Attached Figure Description

[0028] The specific embodiments of the present invention will be further described in detail below with reference to the accompanying drawings. Figure 1 This is a schematic diagram of the system device for producing aldehyde compounds by supergravity two-phase hydroformylation according to the present invention. Detailed Implementation

[0029] To more clearly illustrate the present invention, the following description, in conjunction with preferred embodiments and accompanying drawings, further explains the invention. Similar components in the drawings are indicated by the same reference numerals. Those skilled in the art should understand that the specific description below is illustrative rather than restrictive and should not be construed as limiting the scope of protection of the present invention.

[0030] For ease of description, the terms "first," "second," etc., used in this invention are for descriptive purposes only and should not be construed as indicating or implying their relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined with "first" or "second" may explicitly or implicitly include at least one of that feature. Furthermore, the technical solutions of various embodiments can be combined with each other, but this must be based on the ability of a person skilled in the art to implement them. If the combination of technical solutions is contradictory or impossible to implement, such a combination should be considered non-existent and not within the scope of protection claimed by this invention.

[0031] See Figure 1As shown, as one aspect of the present invention, a system apparatus for producing aldehyde compounds by two-phase hydroformylation under supergravity includes a supergravity reactor 1, a buffer tank 2, a first circulating pump 3, a column bottom heat exchanger 4, a circulating heat exchanger 5, a phase separation tank 6, a second circulating pump 7, a crude aldehyde transfer pump 8, a supergravity distillation unit 9, a column bottom reboiler 10, a product collection pump 11, and a combined cooling and heating unit 12. The liquid phase outlet of the supergravity reactor 1 is connected to the inlet of the buffer tank 2 via a pipeline; The outlet of the buffer tank 2 is connected to the inlet of the first circulating pump 3 via a pipeline; The outlet of the first circulating pump 3 is connected to the shell-side inlet of the tower bottom heat exchanger 4 via a pipeline; The shell-side outlet of the tower bottom heat exchanger 4 is connected to the inlet of the circulating heat exchanger 5 via a pipeline. The outlet of the circulating heat exchanger 5 is divided into two branches; the first branch is connected to the inlet of the phase separation tank 6 through a pipe; the second branch is connected to the liquid phase inlet of the supergravity reactor 1 through a pipe. One liquid phase outlet of the phase separation tank 6 is connected to the inlet of the second circulation pump 7 via a pipeline; the gas phase outlet of the phase separation tank 6 is vented; the outlet of the second circulation pump 7 is connected to the liquid phase inlet of the hypergravity reactor 1 via a pipeline. The other liquid phase outlet of the phase separation tank 6 is connected to the inlet of the crude aldehyde transfer pump 8 via a pipeline; the outlet of the crude aldehyde transfer pump 8 is connected to the liquid phase inlet of the supergravity distillation unit 9 via a pipeline. The liquid phase outlet of the supergravity distillation unit 9 is connected to the tube side inlet of the reboiler heat exchanger 4 via a pipeline. The tube side outlet of the reboiler heat exchanger 4 is divided into two branches. One branch is connected to the product collection pump 11 to collect the product. The other branch is connected to the reboiler reboiler 10 and then returns to the supergravity distillation unit 9.

[0032] The hypergravity reactor 1 used in this invention is a commonly used external circulation hypergravity reactor. This external circulation hypergravity reactor is equipped with conventional components such as a liquid phase inlet, a liquid phase outlet, a gas phase inlet, and a gas phase outlet.

[0033] In some embodiments of the present invention, the shell of the supergravity reactor 1 is provided with a shell heat exchange jacket; the integrated heating and cooling machine 12 is connected to the inlet of the shell heat exchange jacket through a pipe, and the outlet of the shell heat exchange jacket is connected to the integrated heating and cooling machine 12 through a pipe to form a heat exchange cycle.

[0034] In some embodiments of the present invention, the top light component outlet of the supergravity distillation unit 9 is vented or connected to the gas phase inlet of the supergravity reactor 1 via a pressurized pipeline.

[0035] In some embodiments of the present invention, a liquid phase mixer is provided at the liquid phase inlet of the supergravity reactor 1 to ensure that the fresh olefins, the circulating catalyst phase, and the circulating liquid phase are fully mixed before entering the supergravity reactor 1.

[0036] As another aspect of the present invention, a method for producing aldehyde compounds by two-phase hydroformylation using the above-described system apparatus includes the following steps: S1, fresh olefins, recycled catalyst phase (including aqueous phase and ligands in the system) and recycled liquid phase enter the hypergravity reactor 1 through a liquid phase mixer, and react with the syngas in the hypergravity reactor 1 to produce aldehydes. S2. The liquid phase after the reaction enters the buffer tank 2, and is first sent to the bottom heat exchanger 4 of the tower by the first circulation pump 3 to exchange heat with the bottom liquid phase of the supergravity distillation unit 9. Then it enters the circulation heat exchanger 5 for heat exchange again. Part of the liquid phase returns to the supergravity reactor 1, and the other part of the liquid phase enters the phase separation tank 6. S3. The liquid phase undergoes gas-liquid separation and liquid-liquid phase separation in the phase separation tank 6. The catalyst phase is sent back to the supergravity reactor 1 through the second circulation pump 7. The product phase is sent to the supergravity distillation unit 9 through the crude aldehyde transfer pump 8 for product purification. S4. After the product phase is separated in the supergravity distillation unit 9, the light component gas phase at the top is vented or repressurized and sent to the supergravity reactor 1 for reaction. The bottom liquid phase of the supergravity distillation unit 9 is first heated in the bottom heat exchanger 4, and then a part of the bottom liquid phase is vaporized through the bottom reboiler 10 and returned to the supergravity distillation unit 9. The other part of the bottom liquid phase is collected by the product collection pump 11 to obtain the product aldehyde compound.

[0037] In some embodiments of the present invention, in step S1, the fresh olefin refers to a C2 or higher olefin; preferably a C5 or higher olefin.

[0038] In some embodiments of the present invention, the operating pressure of the supergravity reactor is 0.5MPa-20MPa, the operating temperature is 50-200℃, and the rotation speed is 100-3000r / min; preferably, the operating pressure is 0.5MPa-5MPa, the operating temperature is 60-110℃, and the rotation speed is 500-1500r / min.

[0039] In some embodiments of the present invention, in step S1, the pressure ratio of hydrogen to carbon monoxide in the synthesis gas is 15:1; preferably 1.05:1.

[0040] In some embodiments of the present invention, in step S1, the volume ratio of the fresh olefin to the recycled catalyst phase is 1:0.1-20, the mass ratio of the fresh olefin to the catalyst is 100-100000:1, and the molar ratio of the catalyst to the ligand is 1:1-100; preferably, the volume ratio of the fresh olefin to the recycled catalyst phase is 1:1-10, the mass ratio of the fresh olefin to the catalyst is 200-10000:1, and the molar ratio of the catalyst to the ligand is 1:5-50.

[0041] In some embodiments of the present invention, the circulation ratio of the circulating liquid phase in the supergravity reactor is 10-150; preferably 10-50.

[0042] In some embodiments of the present invention, the operating pressure of the supergravity distillation unit is -0.1-10 MPa; preferably -0.1-1 MPa.

[0043] In some embodiments of the present invention, the operating temperature of the supergravity distillation unit is 50-200°C; preferably 50-150°C.

[0044] In some embodiments of the present invention, the operating speed of the supergravity distillation unit is 100-3000 r / min, preferably 200-1000 r / min.

[0045] In some embodiments of the present invention, the reflux ratio of the supergravity distillation unit is 1-15; preferably 1-10. Example 1

[0046] Utilize Figure 1 The system shown performs a two-phase hydroformylation reaction, including the following steps: S1, fresh olefins, recycled catalyst phase (aqueous phase, containing ligands) and recycled liquid phase enter the hypergravity reactor 1 through a liquid phase mixer. The ratio of olefins to catalyst is 1000:1, and the ratio of catalyst to ligand is 1:10. They react with syngas in the hypergravity reactor 1 to produce aldehydes. The pressure ratio of hydrogen to carbon monoxide in the syngas is 1.05:1, the pressure in the hypergravity reactor is 2 MPa, and the reaction temperature is 100℃. S2. The liquid phase after the reaction enters the buffer tank 2, and is first sent to the bottom heat exchanger 4 of the tower by the first circulation pump 3 to exchange heat with the bottom liquid phase of the supergravity distillation unit 9. Then it enters the circulation heat exchanger 5 for heat exchange again. Part of the liquid phase returns to the supergravity reactor 1, and the other part of the liquid phase enters the phase separation tank 6. S3. The liquid phase undergoes gas-liquid separation and liquid-liquid phase separation in the phase separation tank 6. The catalyst phase is sent to the supergravity reactor through the catalyst circulation pump 7. The product phase is sent to the supergravity distillation unit 9 through the crude aldehyde transfer pump 8 for product purification. S4. The product phase is separated by the supergravity distillation unit 9. The light component gas phase at the top is vented or repressurized and sent to the supergravity reactor 1 for reaction. The liquid phase at the bottom of the supergravity distillation unit 9 first exchanges heat with the bottom heat exchanger 4. Then, a part of the bottom liquid phase is vaporized through the bottom reboiler 10 and returned to the supergravity distillation unit 9. The other part of the bottom liquid phase is collected by the product collection pump 11 to obtain the product aldehyde compound.

[0047] The results showed that the olefin conversion rate was over 90%, the aldehyde selectivity was over 99%, the purity of the purified product was over 99%, and the catalyst loss was less than or equal to 0.5 mg / kg. Comparative Example 1

[0048] Example 1 was repeated, except that a conventional stirred tank reactor was used instead of a supergravity reactor; a polar solvent was used instead of water used in Example 1; and a common packed column was used for the distillation process.

[0049] The results showed that the olefin conversion rate was about 80%, the aldehyde selectivity was about 90%, the purity of the purified product was about 95%, the overall energy consumption was about 130% of that in Example 1, and the catalyst loss was greater than or equal to 1 mg / kg. Comparative Example 2

[0050] Example 1 was repeated, except that a conventional stirred tank reactor was used instead of a supergravity reactor; a polar solvent was used instead of water used in Example 1; a common packed column was used for the distillation process; and a quaternary ammonium salt cationic surfactant was added to the reaction system, with a molar ratio of surfactant to rhodium catalyst of 50:1.

[0051] After testing, the conversion rate of olefins was about 80%, the selectivity of aldehydes was about 90%, the purity of the purified product was about 95%, the overall energy consumption was about 120% of that in Example 1, and the catalyst loss was greater than or equal to 2 mg / kg.

[0052] As can be seen from the above embodiments and comparative examples, the reaction system and method for producing aldehydes by two-phase hydroformylation under supergravity proposed in this patent can achieve high conversion rate of olefins without adding polar solvents and surfactants. At the same time, by combining supergravity distillation technology and system thermal integration technology, high yield of aldehydes, low loss of catalyst, and lower overall energy consumption of the system are achieved, which has important industrial application significance.

[0053] Of course, the above scenario is merely an example. This device can be applied to various olefin hydroformylation reaction processes. The substitution of the reaction system based on the concept of this invention, although not necessarily one of the olefin hydroformylation processes, still falls within the scope defined by this application.

[0054] Obviously, the above embodiments of the present invention are merely examples for clearly illustrating the present invention, and are not intended to limit the implementation of the present invention. Those skilled in the art can make other variations or modifications based on the above description. It is impossible to exhaustively list all embodiments here. All obvious variations or modifications derived from the technical solutions of the present invention are still within the protection scope of the present invention.

Claims

1. A system apparatus for producing aldehyde compounds by two-phase hydroformylation under high gravity, characterized in that: It includes a supergravity reactor, buffer tank, first circulation pump, tower bottom heat exchanger, circulation heat exchanger, phase separation tank, second circulation pump, crude aldehyde transfer pump, supergravity distillation unit, tower bottom reboiler, product collection pump, and integrated heating and cooling unit; The liquid phase outlet of the supergravity reactor 1 is connected to the inlet of the buffer tank via a pipeline. The outlet of the buffer tank is connected to the inlet of the first circulation pump via a pipeline; The outlet of the first circulating pump is connected to the shell-side inlet of the tower bottom heat exchanger via a pipeline; The shell-side outlet of the tower bottom heat exchanger is connected to the inlet of the circulating heat exchanger via a pipeline. The outlet of the circulating heat exchanger is divided into two branches; the first branch is connected to the inlet of the phase separation tank through a pipeline; the second branch is connected to the liquid phase inlet of the hypergravity reactor through a pipeline. One liquid phase outlet of the phase separation tank is connected to the inlet of the second circulation pump via a pipeline; the gas phase outlet of the phase separation tank is vented; the outlet of the second circulation pump is connected to the liquid phase inlet of the hypergravity reactor via a pipeline. The other liquid phase outlet of the phase separation tank is connected to the inlet of the crude aldehyde transfer pump via a pipeline; the outlet of the crude aldehyde transfer pump is connected to the liquid phase inlet of the high gravity distillation unit via a pipeline. The liquid phase outlet of the supergravity distillation unit is connected to the tube side inlet of the reboiler heat exchanger via a pipeline. The tube side outlet of the reboiler heat exchanger is divided into two branches: one branch is connected to the product collection pump to collect the product; the other branch is connected to the reboiler and then returns to the supergravity distillation unit.

2. The system apparatus for producing aldehyde compounds by two-phase hydroformylation under supergravity according to claim 1, characterized in that: The shell of the supergravity reactor is equipped with a shell heat exchange jacket; the integrated heating and cooling machine is connected to the inlet of the shell heat exchange jacket through a pipe, and the outlet of the shell heat exchange jacket is connected to the integrated heating and cooling machine through a pipe, forming a heat exchange cycle.

3. The system apparatus for producing aldehyde compounds by two-phase hydroformylation under supergravity according to claim 1, characterized in that: The top light component outlet of the supergravity distillation unit is vented or connected to the gas phase inlet of the supergravity reactor after being pressurized through a pipeline.

4. The system apparatus for producing aldehyde compounds by two-phase hydroformylation under supergravity according to claim 1, characterized in that: A liquid phase mixer is installed at the liquid phase inlet of the supergravity reactor to ensure that the fresh olefins, the circulating catalyst phase, and the circulating liquid phase are fully mixed before entering the supergravity reactor.

5. A method for producing aldehyde compounds by two-phase hydroformylation using any one of the system apparatuses described in claims 1-4, characterized in that, Includes the following steps: S1, fresh olefins, recycled catalyst phase (aqueous phase, with ligands in the system) and recycled liquid phase enter the hypergravity reactor through a liquid phase mixer, and react with syngas in the hypergravity reactor to produce aldehydes. S2. The liquid phase after the reaction enters the buffer tank and is first sent to the bottom heat exchanger of the column by the first circulation pump to exchange heat with the bottom liquid phase of the supergravity distillation unit. Then it enters the circulation heat exchanger for heat exchange again. Part of the liquid phase returns to the supergravity reactor and the other part of the liquid phase enters the phase separation tank. S3. The liquid phase undergoes gas-liquid separation and liquid-liquid phase separation in the phase separation tank. The catalyst phase is returned to the centrifugal reactor via the second circulation pump. The product phase is sent to the centrifugal distillation unit for product purification via the crude aldehyde transfer pump. S4. After the product phase is separated in the supergravity distillation unit, the light component gas phase at the top is vented or repressurized and sent into the supergravity reactor for reaction. The liquid phase in the bottom of the supergravity distillation unit is first heated in the bottom heat exchanger, and then a part of the bottom liquid phase is vaporized through the bottom reboiler and returned to the supergravity distillation unit, while the other part of the bottom liquid phase is collected by the product collection pump to obtain the product aldehyde compounds.

6. The method for producing aldehyde compounds by two-phase hydroformylation according to claim 5, characterized in that: In step S1, the fresh olefin refers to a C2 or higher olefin; preferably a C5 or higher olefin.

7. The method for producing aldehyde compounds by two-phase hydroformylation according to claim 5, characterized in that: The operating pressure of the supergravity reactor is 0.5MPa-20MPa, the operating temperature is 50-200℃, and the rotation speed is 100-3000r / min; preferably, the operating pressure is 0.5MPa-5MPa, the operating temperature is 60-110℃, and the rotation speed is 500-1500r / min.

8. The method for producing aldehyde compounds by two-phase hydroformylation according to claim 5, characterized in that: In step S1, the pressure ratio of hydrogen to carbon monoxide in the synthesis gas is 15:1; preferably 1.05:

1.

9. The method for producing aldehyde compounds by two-phase hydroformylation according to claim 5, characterized in that: In step S1, the volume ratio of fresh olefin to recycled catalyst phase is 1:0.1-20, the mass ratio of fresh olefin to catalyst is 100-100000:1, and the molar ratio of catalyst to ligand is 1:1-100; preferably, the volume ratio of fresh olefin to recycled catalyst phase is 1:1-10, the mass ratio of fresh olefin to catalyst is 200-10000:1, and the molar ratio of catalyst to ligand is 1:5-50.

10. The method for producing aldehyde compounds by two-phase hydroformylation according to claim 5, characterized in that: The circulation ratio of the circulating liquid phase in the supergravity reactor is 10-150; preferably 10-50. Preferably, in step S4, the operating pressure of the supergravity distillation unit is -0.1-10 MPa; more preferably -0.1-1 MPa; preferably, in step S4, the operating temperature of the supergravity distillation unit is 50-200℃; more preferably 50-150℃. Preferably, in step S4, the operating speed of the supergravity distillation unit is 100-3000 r / min, more preferably 200-1000 r / min; Preferably, in step S4, the reflux ratio of the supergravity distillation unit is 1-15; more preferably 1-10.

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