Liquid-phase carbonyl synthesis reactor and liquid-phase carbonyl synthesis reaction system
By adopting a multi-fluid stirring device and a gas distribution device in the liquid-phase carbonyl synthesis reactor, uniform distribution and efficient mixing of gas and liquid are solved, and the problem of vibration and sealing of the stirring paddle in the reactor in the prior art is solved, and the temperature is increased Uniformity and production capacity.
Patent Information
- Application Number
- CN202420354137.6
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-02-26
- Publication Date
- 2024-12-10
- Estimated Expiration
- 2034-02-26
AI Technical Summary
The existing liquid-phase carbonyl synthesis reactor has low reaction rate at high methanol concentration, and the stirring paddle vibrates significantly and has difficulty in sealing, resulting in high equipment maintenance costs and poor temperature uniformity, which limits the improvement of production capacity.
Design a liquid-phase carbonyl synthesis reactor, adopting multiple first fluid stirring devices and second fluid stirring devices, combining gas distribution devices, and using nozzles and gas distributors to achieve uniform distribution and mixing of gas and liquids, and the external circulation pump is used for control The liquid flow rate forms uniform gas-liquid distribution and efficient mixing effect, improving temperature uniformity.
It achieves uniform distribution of gas and liquid, good mixing effect, improves temperature uniformity in the reactor, reduces equipment maintenance costs, and increases production capacity. It is especially suitable for the production of acetic acid and carbonylation of methanol, and the production of acetic anhydride. .
Smart Images
Figure CN222131844U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of synthesis reactor preparation, in particular to a liquid phase carbonyl synthesis reactor and a liquid phase carbonyl synthesis reaction system. Background Art
[0002] Acetic acid is an important bulk chemical that can be used to produce hundreds of chemicals including vinyl acetate, terephthalic acid (PTA) and acetic anhydride. It is widely used in the chemical, synthetic fiber and coating industries. Since its production in 1970, the low-pressure carbonyl synthesis of methanol has become the main route for the synthesis of acetic acid, accounting for more than 80% of the production capacity. A large number of experiments have shown that when the methanol concentration is high, the reaction rate of the carbonyl synthesis reaction is independent of the methanol concentration; but when the methanol concentration is low, the reaction rate is proportional to the methanol concentration. Therefore, the methanol concentration in the reactor should be kept in a fully mixed flow state in the zero-order reaction section to ensure that the reaction rate is always maintained at a high level. When there is insufficient CO in the reaction system, the rhodium catalyst complex is gradually converted into RhI 3 The precipitate leads to catalyst deactivation and a decrease in reaction rate. Therefore, the key to ensuring the smooth progress of methanol carbonylation reaction is to maintain a high degree of liquid phase backmixing and CO dissolution rate in the reactor.
[0003] The traditional continuous carbonylation production process in industry generally adopts a kettle reactor with multi-layer stirring paddles. However, this reaction route requires the addition of sufficient lithium iodide to maintain the stability of the rhodium catalyst. Therefore, the iodine concentration in the reaction environment is high, which is highly corrosive to the equipment. The reactor needs to be made of zirconium, which leads to high equipment manufacturing and maintenance costs. In addition, due to the high reaction pressure (2.5-3MPa), the stirring paddle vibrates significantly under high liquid flow, and the sealing is difficult, resulting in frequent equipment shutdowns during high-load production. Therefore, the development of a gas-liquid two-phase reactor based on static equipment is an urgent need for the current methanol low-pressure carbonylation to acetic acid process. This is not only an important means to achieve quality improvement, efficiency enhancement, energy conservation and consumption reduction in the methanol carbonylation reaction process, but can also be promoted and applied to industries such as mineral flotation and aquaculture.
[0004] Patent CN 106187660A provides a device and process for producing cyclohexane by hydrogenating benzene, wherein the reactor adopts top liquid phase feeding, and utilizes the entrainment effect of high-speed jet to break bubbles, thereby achieving high mass transfer efficiency and reaction efficiency. Patent CN 112010746A discloses an enhanced system and method for producing acetic acid by methanol carbonylation using the above reactor. However, the above patent adopts a single nozzle feeding, and its effective action area is very limited. The mixing effect is poor in the wall area of the reactor with a small height-to-diameter ratio, which is difficult to be applied to the temperature-sensitive liquid phase carbonylation reaction.
[0005] Patent CN 115318233A discloses an axial eccentric jet bubbling reactor and its application and a method for strengthening the mass transfer process. The reactor includes a reactor body provided with a gas-liquid outlet, a liquid material introduction component and a gas material introduction component, wherein the liquid material introduction component is arranged at an axial eccentric position. The reactor injects the liquid phase flow through the liquid phase material introduction component; injects the gas phase flow through the gas phase material introduction component; the liquid phase flow contacts the gas phase flow and is discharged through the gas-liquid outlet. The utility model improves the uniform mass transfer, heat transfer and transmission process in the eccentric jet reactor. However, due to the eccentric structure, the flow field it generates is also asymmetric, and there are still flow dead zones or areas with poor mixed mass transfer effects.
[0006] Although the above patents have enhanced the mass transfer and mixing efficiency of the gas-liquid two-phase to a certain extent, it was found in the actual production process that the temperature uniformity in the existing reactor using fluid stirring (temperature difference 8-9°C) is far worse than that of the stirred tank reactor (temperature difference 1-2°C), which greatly limits the increase in the generation load. Utility Model Content
[0007] The purpose of the utility model is to provide a liquid-phase carbonyl synthesis reactor and use the liquid-phase carbonyl synthesis reactor in a liquid-phase carbonyl synthesis reaction system in view of the problems existing in the prior art. The liquid-phase carbonyl synthesis reactor has a simple structure, and the liquid-phase carbonyl synthesis reaction system formed has uniform gas-liquid distribution and good mixing effect; it not only solves the problems of obvious vibration of the stirring paddle in the existing stirred tank reactor, greater sealing difficulty, and high equipment maintenance cost, but also can improve the temperature uniformity in the reactor, thereby improving production capacity. It is particularly suitable for processes such as carbonylation of methanol to produce acetic acid and carbonylation of methyl acetate to produce acetic anhydride.
[0008] In order to achieve the purpose of the above utility model, the technical solution of the utility model is as follows:
[0009] A liquid-phase carbonyl synthesis reactor comprises an upper end cap, a middle barrel and a lower end cap, wherein: at least two first fluid stirring devices with the same structure are arranged on the upper part of the middle barrel, the first fluid stirring devices are evenly distributed along the wall of the liquid-phase carbonyl synthesis reactor, and the outlets are oriented toward the lower end cap; the first fluid stirring device comprises a first liquid inlet connected to the outside and a first nozzle arranged on the first liquid inlet; at least one second fluid stirring device and a gas distribution device are arranged in the lower end cap; the second fluid stirring device comprises a second liquid inlet and a second nozzle, the second nozzle is arranged on the second liquid inlet and is inside the liquid-phase carbonyl synthesis reactor; the gas distribution device comprises a gas distributor and an air inlet, and the gas distributor is connected to the air inlet in a T-shape; a circulating liquid outlet is arranged in the lower end cap; an overflow outlet is arranged on the middle barrel; and a gas phase outlet is arranged in the upper end cap.
[0010] As a preferred implementation in the present application, the number of the first fluid stirring devices is 3; the number of the second fluid stirring devices is 2.
[0011] As a better embodiment of the present application, in the liquid-phase carbonyl synthesis reactor, the angle between the first nozzle and the vertical direction is in the range of 0°-45° (specifically 0°, 5°, 10°, 15°, 20°, 25°, 30°, 35°, 40°, 45°, etc.), more preferably 0°-10°; the outlet direction is toward the axis of the reactor.
[0012] As a better embodiment of the present application, in the liquid-phase carbonyl synthesis reactor, the angle between the second nozzle and the vertical direction is in the range of 10°-60° (specifically 10°, 15°, 20°, 25°, 30°, 35°, 40°, 45°, 50°, 55°, 60°, etc.), more preferably 30°-45°; the outlet direction is toward the axis of the reactor.
[0013] As a better embodiment of the present application, an external circulation pump is provided outside the liquid-phase carbonyl synthesis reactor; the circulating liquid outlet of the liquid-phase carbonyl synthesis reactor is connected to the external circulation pump, and the external circulation pump is connected to the first feed port of the first fluid stirring device located at the upper head to form an external circulation liquid phase passage.
[0014] As a better embodiment of the present application, in the liquid phase carbonyl synthesis reactor, the structural forms of the first nozzle and the second nozzle include but are not limited to reduced diameter, venturi and embedded swirl guide plates.
[0015] As a better embodiment of the present application, the apparent jet velocity of the first nozzle is 5-20 m / s, more preferably 10-15 m / s; the apparent jet velocity of the second nozzle is not higher than 3 / 4 of the apparent jet velocity of the first nozzle, more preferably 1 / 3-2 / 3 times.
[0016] As a better implementation in the present application, the difference between the liquid velocities at the outlets of the plurality of first nozzles should be no higher than 10% of the average value, and more preferably lower than 5%.
[0017] As a better embodiment of the present application, in the liquid-phase carbonyl synthesis reactor, the height-to-diameter ratio of the middle cylinder is 1-4:1, more preferably 2.5-3.5:1; the middle cylinder is filled with liquid, that is, the reactor liquid level is controlled by the overflow outlet flow rate, and the outlet of the first nozzle is immersed below the liquid level of the liquid in the middle cylinder.
[0018] As a better embodiment of the present application, in the liquid-phase carbonyl synthesis reactor, the form of the gas distributor includes but is not limited to annular, disc, tree-shaped and other types; the gas distributor is evenly opened with the axis of the liquid-phase carbonyl synthesis reactor as the center, and the opening rate is 0.4%-5%, more preferably 0.5%-2%.
[0019] As a better embodiment of the present application, in the liquid-phase carbonyl synthesis reactor, the ratio of the distance between the gas distributor and the bottom of the lower head to the diameter of the middle cylinder is 0.05-0.3:1, and more preferably 0.2:1; the ratio of the diameter of the gas distributor to the diameter of the middle cylinder is 0.2-0.5:1, and more preferably 0.35:1.
[0020] A liquid-phase carbonyl synthesis reaction system comprises a carbonyl synthesis reactor as described above or a combination of the above-mentioned components, a high-pressure separator, a flash-evaporator, and a circulating heat exchanger; wherein the second liquid inlet of the second fluid stirring device of the liquid-phase carbonyl synthesis reactor is connected to the liquid-phase raw material input pipeline to feed the liquid-phase raw material into the liquid-phase carbonyl synthesis reactor; the gas inlet of the gas distribution device of the liquid-phase carbonyl synthesis reactor is connected to the gas-phase raw material input pipeline to feed the gas-phase raw material into the liquid-phase carbonyl synthesis reactor; the overflow outlet of the middle barrel of the liquid-phase carbonyl synthesis reactor is connected to the inlet of the high-pressure separator; the top of the high-pressure separator is provided with an exhaust port, the bottom is provided with a liquid discharge port, and the liquid discharge port is connected to the inlet of the flash-evaporator; the top of the flash-evaporator is provided with a gas-phase product output port, the bottom is provided with a circulating mother liquid outlet, the circulating mother liquid outlet is connected to the liquid-phase circulating pipeline, the liquid-phase circulating pipeline is connected to the circulating heat exchanger, and the circulating heat exchanger and the liquid-phase raw material pipeline are connected to the liquid-phase carbonyl synthesis reactor through the second liquid inlet.
[0021] As a better implementation mode in the present application, in the liquid-phase carbonyl synthesis reaction system, a first external circulation pump is provided between the liquid-phase circulation pipeline and the circulation heat exchanger.
[0022] Compared with the existing technology, the beneficial effects of the utility model are:
[0023] (I) The liquid-phase carbonyl synthesis reactor in the utility model has a simple structure, and the formed liquid-phase carbonyl synthesis reaction system has uniform gas-liquid distribution and good mixing effect. It not only solves the problems of obvious vibration of the stirring paddle in the existing stirred tank reactor, greater sealing difficulty, and high equipment maintenance cost, but also improves the temperature uniformity in the reactor, thereby increasing production capacity. It is particularly suitable for processes such as carbonylation of methanol to produce acetic acid and carbonylation of methyl acetate to produce acetic anhydride.
[0024] (II) During the production process, the external circulating liquid is divided into multiple streams and injected into the reactor from the top by immersion. The large bubbles generated by the gas distributor are broken into small bubbles by the entrainment and shearing action of the high-speed liquid jet, which increases the mass transfer area of the bubble two-phase while promoting the dispersion and mixing of the gas-liquid two-phase, ensuring the concentration uniformity in the reactor; in addition, the circulating mother liquor from the evaporator and the fresh liquid raw material are injected into the reactor from the bottom, effectively avoiding the problem of weak turbulence of the liquid phase at the bottom head of the reactor and the existence of a flow dead zone. Under certain production capacity conditions, the temperature difference of the liquid phase carbonyl synthesis reactor proposed by the utility model is 2-3°C, which is much better than the conventional fluid stirring reactor. BRIEF DESCRIPTION OF THE DRAWINGS
[0025] Figure 1 It is a schematic structural diagram of the liquid phase carbonyl synthesis reactor described in the utility model;
[0026] Figure 2 It is a schematic diagram of the structure of the liquid phase carbonyl synthesis reaction system in the utility model;
[0027] Among them, 01-liquid phase carbonyl synthesis reactor, 02-high pressure separator, 03-flash-evaporator, 04-circulating heat exchanger, 05-liquid phase raw material source, 06-gas phase raw material source, 07-high pressure separator exhaust port, 08-high pressure separator discharge port, 09-flash-evaporator gas phase product outlet, 010 flash-evaporator circulating mother liquor outlet, 011-liquid phase circulation pipeline, 012-first external circulation pump, 11-reactor gas phase outlet, 21-first fluid stirring device, 211-first liquid inlet, 212-first nozzle, 22-reactor overflow outlet, 31-fluid stirring device in reactor, 311-second liquid inlet, 312-second nozzle, 32-gas distribution device, 321-gas distributor, 322-gas inlet, 33-circulating liquid outlet, 41-external circulation pump. DETAILED DESCRIPTION
[0028] All features disclosed in this specification, or steps in all methods or processes disclosed, except mutually exclusive features and / or steps, can be combined in any manner.
[0029] Any feature disclosed in this specification (including claims and abstract), unless otherwise stated, may be replaced by other equivalent or alternative features having similar purposes. That is, unless otherwise stated, each feature is only an example of a series of equivalent or similar features.
[0030] The features and performance of the present invention are further described in detail below in conjunction with the embodiments.
[0031] Embodiment 1:
[0032] like Figure 1 - Figure 2 As shown, a liquid phase carbonyl synthesis reaction system includes a liquid phase carbonyl synthesis reactor, a high-pressure separator 02, a flash evaporator 03, and a circulating heat exchanger 04.
[0033] The liquid-phase carbonyl synthesis reactor comprises an upper end cap, a middle barrel and a lower end cap. Three first fluid stirring devices 21 with the same structure are arranged on the upper part of the middle barrel. The first fluid stirring devices 21 are evenly distributed along the reactor wall, and the outlets are toward the lower end cap. The first fluid stirring device comprises a first liquid inlet 211 and a first nozzle 212 arranged at the upper part, and the outlet direction of the first nozzle is toward the axis of the reactor; two second fluid stirring devices 31 and a gas distribution device 32 are arranged in the lower end cap. The second fluid stirring device 31 faces the upper end cap, comprises a second liquid inlet 311 and a second nozzle 312, and the outlet direction of the second nozzle 312 is toward the axis of the reactor; the gas distribution device 32 comprises a gas distributor 321 and a gas inlet 322; a circulating liquid outlet 33 is arranged in the lower end cap; an overflow outlet 22 is arranged on the middle barrel; and a gas phase outlet 11 is arranged in the upper end cap 1.
[0034] An external circulation pump 41 is provided outside the liquid-phase carbonyl synthesis reactor 01; the circulating liquid outlet 33 of the liquid-phase carbonyl synthesis reactor 01 is connected to the external circulation pump 41, and the external circulation pump 41 is connected to the first liquid inlet 211 of the first fluid stirring device 21 located at the upper head, forming an external circulation liquid phase passage.
[0035] The liquid-phase carbonyl synthesis reaction system comprises the carbonyl synthesis reactor 01, the high-pressure separator 02, the flash-evaporator 03, and the circulating heat exchanger 04; the second liquid inlet 311 of the second fluid stirring device 31 of the liquid-phase carbonyl synthesis reactor 01 is connected to the liquid-phase raw material input pipeline 05, and the liquid-phase raw material is fed into the liquid-phase carbonyl synthesis reactor 01; the gas inlet 322 of the gas distribution device 32 of the liquid-phase carbonyl synthesis reactor 01 is connected to the gas-phase raw material input pipeline 06, and the gas-phase raw material is fed into the liquid-phase carbonyl synthesis reactor 01; the overflow outlet of the middle section of the cylinder of the liquid-phase carbonyl synthesis reactor 01 22 is connected to the inlet of the high-pressure separator 02, the high-pressure separator 02 is provided with an exhaust port 07 at the top and a drain port 08 at the bottom, the drain port 08 of the high-pressure separator 02 is connected to the inlet of the flash-evaporator 03; the flash-evaporator 03 is provided with a gas phase product outlet 09 at the top and a circulating mother liquor outlet 010 at the bottom, the circulating mother liquor passes through the circulating mother liquor outlet 010 at the bottom of the flash-evaporator 03, the liquid phase circulation pipeline 011 and the circulating heat exchanger 04 in sequence, and returns to the liquid-phase carbonyl synthesis reactor 01 together with the liquid-phase raw material through the second liquid inlet 311 of the second fluid stirring device 31 of the liquid-phase carbonyl synthesis reactor 01.
[0036] The circulating mother liquid outlet of the flash evaporator 03 is provided with a first external circulation pump 012 .
[0037] The first nozzle structure is a reduced diameter, the ratio of the nozzle outlet diameter to the nozzle inlet diameter is 1:2, the angle between the first nozzle and the vertical direction is 29.8°, and the apparent jet velocity is 13.7m / s; the second nozzle structure is an embedded swirl guide plate, the number of guide plate blades is 4, the angle is 120°, the angle between the second nozzle and the vertical reverse direction is 34.3°, and the apparent jet velocity is 9.4m / s. The height-to-diameter ratio of the middle section of the reactor cylinder is 2.4:1. The gas distributor is in the form of a ring, the pore diameter is 4mm, and the porosity is 1.2%. The ratio of the distance from the gas distributor to the bottom of the lower head to the diameter of the middle section cylinder is 0.2:1; the ratio of the gas distributor diameter to the diameter of the middle section cylinder is 0.3:1.
[0038] This embodiment is used as a reactor for the low-pressure carbonylation of methanol to acetic acid. The reaction uses a rhodium complex as a catalyst and lithium iodide as a co-catalyst. After the reaction is stable, it is a continuous feeding and discharging process. The flow rate of the reaction raw material methanol is 6.5 kg / h, and the flow rate of CO is 4.9 Nm 3 / h, the reactor volume is 17L, the reaction temperature is 195℃, and the reaction pressure is 3MPa. The reaction raw material methanol is added to the liquid phase carbonyl synthesis reactor 01 through the second liquid inlet 311. When the set liquid level is reached, the gas phase raw material CO is introduced, and CO enters the reactor through the gas distribution device 32. The product obtained by the reaction leaves the liquid phase carbonyl synthesis reactor 01 through the overflow outlet 22 and enters the high-pressure separator 02. After gas-liquid separation, the liquid phase product enters the flash evaporator 03 from the discharge port 08 at the bottom of the high-pressure separator 02. After flash evaporation in the flash evaporator 03, the product is discharged from the gas phase product outlet 09 at the top of the flash evaporator 03 and transported to the distillation process. The liquid returns to the liquid phase carbonyl synthesis reactor 01 from the circulating mother liquid outlet 010 at the bottom of the flash evaporator 03, the liquid phase circulation pipeline 011, the circulating heat exchanger 04 and the first external circulation pump 012 to participate in the reaction again. Part of the by-product gas is discharged from the gas phase outlet 11 at the top of the liquid phase carbonyl synthesis reactor 01. In order to achieve good gas-liquid mixing and mass transfer, an external circulation pump 41 is used to extract part of the fluid from the bottom of the reactor and pump it into the first fluid stirring device 21 to generate a high-speed jet to break up the bubbles and stir the mixed gas. The experimental results show that when operating under this device, the CO single-pass conversion rate is 93%, and the maximum temperature difference between the upper and lower parts of the liquid phase carbonyl synthesis reactor is 2°C.
[0039] Conventional industrial reactors for synthesizing acetic acid from methanol low-pressure carbonylation use stirred tank reactors or bubbling stirred reactors. Stirred tank reactors mostly use a combination of axial flow and radial flow stirring paddles. The stirring paddles vibrate far under high flow conditions, making sealing difficult and prone to leakage. Bubbling stirred reactors rely heavily on gas-induced disturbances, resulting in very poor gas-liquid mixing effects, uneven temperature distribution, and a general temperature difference of 8-9°C between the upper and lower reactors.
[0040] The above-mentioned embodiments only express the specific implementation methods of the present application, and the descriptions thereof are relatively specific and detailed, but they cannot be understood as limiting the protection scope of the present application. It should be pointed out that, for ordinary technicians in this field, several variations and improvements can be made without departing from the technical solution concept of the present application, and these all belong to the protection scope of the present application.
[0041] This background technology section is provided to generally present the context of the present invention, and the work of the currently named inventors, the work to the extent described in this background technology section, and aspects of this section that did not constitute prior art at the time of application are neither explicitly nor implicitly admitted to be prior art of the present invention.
Claims
1. A liquid phase carbonyl synthesis reactor, comprising an upper end cap, a middle cylinder and a lower end cap, characterized in that: At least two first fluid stirring devices (21) of the same structure are provided on the upper part of the middle section of the cylinder. The first fluid stirring devices (21) are evenly distributed along the wall of the reactor, and the outlets are oriented toward the lower end cap. The first fluid stirring device (21) comprises a first liquid inlet (211) connected to the outside and a first nozzle (212) arranged on the first liquid inlet (211). At least one second fluid stirring device (31) and a gas distribution device (32) are provided in the lower end cap. The second fluid stirring device (31) The device (31) comprises a second liquid inlet (311) and a second nozzle (312), and the second nozzle (312) is arranged on the second liquid inlet (311); the gas distribution device (32) comprises a gas distributor (321) and an air inlet (322), and the gas distributor (321) and the air inlet (322) are connected in a T-shape; a circulating liquid outlet (33) is arranged in the lower end cover; an overflow outlet (22) is arranged on the middle section cylinder; and a gas phase outlet (11) is arranged on the upper end cover (1).
2. The liquid phase carbonyl synthesis reactor according to claim 1, characterized in that: The angle between the first nozzle (212) and the vertical direction is in the range of 0°-45°, and the outlet direction is toward the axis of the reactor.
3. The liquid phase carbonyl synthesis reactor according to claim 1, characterized in that: The angle between the second nozzle (312) and the vertical direction is in the range of 10°-60°, and the outlet direction is toward the axis of the reactor.
4. The liquid phase carbonyl synthesis reactor according to claim 1, characterized in that: An external circulation pump (41) is arranged outside the liquid phase carbonyl synthesis reactor; the circulating liquid outlet (33) is connected to the external circulation pump (41), and the external circulation pump (41) is connected to the first liquid inlet (211).
5. The liquid phase carbonyl synthesis reactor according to claim 1, characterized in that: The first nozzle (212) and the second nozzle (312) are in the form of reduced diameter, Venturi or built-in swirl guide plate.
6. The liquid phase carbonyl synthesis reactor according to claim 1, characterized in that: The height-to-diameter ratio of the middle cylinder is 1-4:1; the middle cylinder is filled with liquid, and the outlet of the first nozzle (212) is immersed below the liquid level in the middle cylinder.
7. The liquid phase carbonyl synthesis reactor according to claim 1, characterized in that: The gas distributor (321) includes, but is not limited to, a ring type, a disc type, and a tree branch type; the gas distributor (321) is evenly perforated with the axis of the liquid phase carbonyl synthesis reactor as the center, and the perforation rate is 0.4%-5%.
8. The liquid phase carbonyl synthesis reactor according to claim 1, characterized in that: The ratio of the distance between the gas distributor (321) and the bottom of the lower end cap to the diameter of the middle cylinder is 0.05-0.3:1; the ratio of the diameter of the gas distributor (321) to the diameter of the middle cylinder is 0.2-0.5:
1.
9. A liquid phase carbonyl synthesis reaction system, characterized in that: The invention comprises a carbonyl synthesis reactor (01) as claimed in any one of claims 1 to 8, a high-pressure separator (02), a flash-evaporator (03), and a circulating heat exchanger (04); wherein the second liquid inlet (311) of the second fluid stirring device (31) of the liquid-phase carbonyl synthesis reactor (01) is connected to the liquid-phase raw material input pipeline (05); the gas inlet (322) of the gas distribution device (32) of the liquid-phase carbonyl synthesis reactor (01) is connected to the gas-phase raw material input pipeline (06); the overflow outlet (22) of the middle cylinder of the liquid-phase carbonyl synthesis reactor (01) is connected to the high-pressure separator (02 ) is connected to the inlet of the high-pressure separator (02); an exhaust port (07) is provided at the top of the high-pressure separator (02), and a liquid discharge port (08) is provided at the bottom, and the liquid discharge port (08) is connected to the inlet of the flash evaporator (03); a gas phase product output port (09) is provided at the top of the flash evaporator (03), and a circulating mother liquid outlet (010) is provided at the bottom, and the circulating mother liquid outlet (010) is connected to the liquid phase circulation pipeline (011), the liquid phase circulation pipeline (011) is connected to the circulation heat exchanger (04), and the circulation heat exchanger (04) and the liquid phase raw material pipeline are connected to the liquid phase carbonyl synthesis reactor (01) through the second liquid inlet (311).
10. The liquid phase carbonyl synthesis reaction system according to claim 9, characterized in that: A first external circulation pump (012) is provided between the liquid phase circulation pipeline (011) and the circulation heat exchanger (04).